Normas TEMA

STANDARDS OF THE

TUBULAR EXCHANGER

MANUFACTURERS ASSOCIATION

EIGHTH EDITION

TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION, INC.25 North Broadway

Tarrytown, New York 10591Richard C. Byrne, Secretary

www.tema.org

NO WARRANTYEXPRESSED OR IMPLIED

The Standards herein are recommended bto assist users, engineers and designers wi:

Inc.o specify, design and install tubular exchangers. These

standards are based upon sound engineering principles, research and field experience in themanufacture, design, installation and use of tubular exchangers, These standards may be subject torevision as further investigation or experience may show is necessary or desirable. Nothing hereinshall constitute a warranty of any kind, expressed or implied, and warranty responsibility of any kind isexpressly denied.

0 Copyright 1968, 1970, 1972, 1974,1978, 1986, 1987, 1988, 1999Tubular Exchanger Manufacturers Association, Inc.

TEMA is a trademark of the Tubular Exchanger Manufacturers Association, Inc

This document may not be copiedelectronic medium or machinereabp

hotocopied, reproduced, translated, modified or reduced to anyable form in whole or in part, without prior written consent of the

Tubular Exchanger Manufacturers Association, Inc.

ALL RIGHTS RESERVED

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I.7

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CONTRIBUTING MEMBERS

TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION, INC.

Comprising Manufacturers of Various Types

of Shell and Tube Heat Exchanger Equipment

API Heat Transfer, Inc . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2777 Walden AvenueBuffalo, NY 14225

Cust-0-Fab, Inc ._._.____.._.__.....................,,...................,................................ 8888 West 21st StreetSand Springs, OK 74063

Energy Exchanger Company . . . . .._.._.______._................................................. 1844 N. Garnett RoadTulsa, OK 74116

Engineers and Fabricators Company .____.__......_.____......... _._._._........__........ 3501 West 1 Ith StreetHouston, TX 77008-60011

Fabsco Shell and Tube, LLC . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O. Box 988Sapulpa, OK 74666

Graham Corporation . . . ..__.............................................................................. 20 Florence AvenueBatavia, NY 14020

Heat Transfer Equipment Co . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O. Box 580638Tulsa, OK 74158

Hughes-Anderson Heat Exchangers, Inc . . . . .._................................ 1001 N. Fulton Avenue~“~~ Tulsa, OK 74115

ITT Standard, IIT fluid Technology Corporation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O. Box 1102Buffalo, NY 14227

Joseph Oat Corporation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2500 BroadwayCamden, NJ 08104

Manning and Lewis Engineering Company .._______.__.................................... 675 Rahway AvenueUnion, NJ 07083

Nooter Corporation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O. Box 451St. Louis, MO 63166

Ohmstede, Inc . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 825 North Main StreetBeaumont, TX 77701

RAS Process Equipment, Inc . . . . . . . . . . . <~..................... 324 Meadowbrook RoadRobbinsville, NJ 08691

Southern Heat Exchanger Corporation ._._......_._...._.............................................. P.O. Box 1850Tuscaloosa, AL 35483

Struthers Industries. Inc . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1500 34th StreetGulfport, MS 39501

Wiegmann and Rose . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O.Box 4187Subsidiary of Xchanger Mfg. Corp. Oakland, CA 94614

Yuba Heat Transfer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . P.O.Box 3158A Division of Connell Limited Partnership Tulsa, OK 74101

. . .111

TECHNICAL COMMITTEEOF THE

TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION

Ken O’Connor ...........................................................................................AP I Heat Transfer, Inc.

Doug Werhane ....................................................................................................Cust-0-Fab. Inc.

Ken Fultz .........................................................................................Energy Exchanger Company

Cris Smelley .......................................................................Engineers and Fabricators Company

Philip Marks ..I ...............................................................................................Graham Corporation

Monte Davis .........................................................................Heat Transfer Equipment Company

Jim Harrison ...............................................................Hughes-Anderson Heat Exchangers, Inc.

Nick Tranquilli ...........................................................................................................In Standard

Michael Holtz.. ......................................................................................Joseph Oat COpOratiOn

Ted Rapczynski ..................................................................Manning and Lewis Engineering Co.

Steve Meierotto..............................................................................................Nooter Corporation

Michael Tmcy ........................................................................................................Ohmstede, Inc.Russell Miller

“, .“.

Todd Allen .,._...........Dan Stenman

.._.......................... Southern Heat Exchanger Corp.

Gary L. Berry . ..__.._.._....._.._...................,,..............,.,.,.,,,.....,,................... Struthers Industries, Inc.

Jack E. Logan ,..__.____,.__._.__,........,.......,...,,,,..,,.....,,...,.,.........,,,..,,...,,.~.......... Wiegmann and ROSSSubsidrary of Xchanger Mfg. Corp.

Larry Brumbaugh . . ..___........ . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ..~..~..~ _......_..._.......... Y$a Heat TransferA Divwon of Connell Lrmrted Partnership

iv

CONTENTS

Symbol &Section Paragraph

1 N1

2

2 F1

2

3

4

3 G

1

2

3

4

5

6

7

4 E1

2

3

4

5 RCB

1

2

3

4

5

6

7

8

9

10

11

6 V

1

2

3

4

5

6

7

8

MEMBERSHIP LIST ................................................................................................................................ iii

TECHNICAL COMMITTEE ..................................................................................................................... iv

PREFACE.. ............................................................................................................................................. ”

NOTES TO USERS.. ............................................................................................................................. viiiNOMENCLATURE

..Size Numbering and Type Deslgnatton-Recommended Practice .......................................................... 1

Nomenclature of Heat Exchanger Components.. ................................................................................... 3

FABRICATION TOLERANCES

External Dimensions, Nozzle and Support Locations.. ........................................................................... 6

Recommended Fabrication Tolerances.. ............................................................................................... 7

Tubesheets, Parttiions, Covers, and Flanges ........................................................................................ 8

Flange Face lmperiections ................................................................................................................... 9

GENERAL FABRICATION AND PERFORMANCE INFORMATION

Shop Operation .................................................................................................................................. 13

Inspection .......................................................................................................................................... 13

Nameplates ....................................................................................................................................... 13

Drawings and ASME Code Data Reports.. .......................................................................................... 13

Guarantees ........................................................................................................................................ 14

Preparation of Heat Exchangers for Shipment.. ................................................................................... 15

General Construction Features of TEMA Standard Heat Exchangers.. ................................................. 15

INSTALLATION, OPERATION, AND MAINTENANCE

Performance of Heat Exchangers ....................................................................................................... 17’

Installation of Heat Exchangers .......................................................................................................... 17

Operation of Heat Exchangers. ........................................................................................................... 18

Maintenance of Heat Exchangers ....................................................................................................... 19

MECHANICAL STANDARD TEMA CLASS RCB HEAT EXCHANGERS

Scope and General Requirements.. .................................................................................................... 23

Tubes ................................................................................................................................................ 27

Shells and Shell Covers ..................................................................................................................... 30

Baffles and Support Plates ............................................ ~,:................................................................... 31

Floating End Construction .................................................................................................................. 38

Gaskets ............................................................................................................................................. 43

Tubesheets ........................................................................................................................................ 45

Flexible Shell Elements ...................................................................................................................... 75

Channels, Covers, and Bonnels.. ....................................................................................................... .88

Nozzles.............................................................................................................................................. 91

End Flanges and Batting.. ................................................................................................................... 93

FLOW INDUCED VIBRATION

Scope and General ............................................................................................................................. 95

Vibration Damage Patterns ................................................................................................................. 95

Failure Regions .......................................................................................................................... ....... .95

Dimensionless Numbers ..................................................................................................................... 96

Natural Frequency.. ............................................................................................................................ 97

Axial Tube Stress.. ........................................................................................................................... 104

Effective Tube Mass.. ....................................................................................................................... 104

Damping .......................................................................................................................................... 107

vi

&“I:r_f?27ec?fy CONTENTS62h._ Symbol &f? Section Paragraph

c 6 V FLOW INDUCED VIBRATION (continued)

r? 9 Shell Side Velocity Distribution ......................................................................................................... 109

??-!10 Estimate of Critical Flow Velocity . .................................................................................................... 112

11 Vibration Amplitude .......................................................................................................................... 114!-z 12 Acoustic Vibration ..................... ..‘ .................................................................................................... 116

0 13 Design Considerations ..................................................................................................................... 121

A14 Selected References.. ...................................................................................................................... 122

07 T THERMAL RELATIONS

1 Scope and Basic Relations ............................................................................................................... 124sz 2 Fouling............................................................................................................................................. 125

h33 Fluid Temperature Relations.. ........................................................................................................... 126

a4 tiean Metal Temperatur& Of Shell and Tubes ............................................ I...:. .................. :.............. 126

6 P PHYSICAL PROPERTIESOF FLUIDSis: 1 Fluid Density .................................................................................................................................... 150

e 2 Specific Heat .................................................................................................................................... 150

63 Heat Content of Petroleum Fractions.. .............................................................................................. 151

4 Thermal Conductivity........................................................................................................................ 151$?? 5 Viscosity .......................................................................................................................................... 151&? 6 Critical Properties.. ........................................................................................................................... 152

@? 7 Properties of Gas and Vapor Mixtures ............................................................................................... 152

c16 Selected References.. ...................................................................................................................... 153

9 D GENERAL INFORMATION

e”l (See detailed Table of Contents] ...................................................................... :................................ 163

h 10 RGP RECOMMENDED GOOD PRACTICE

cG-7.1 1 Horizontal Vessel Supports.. ............................................................................................................. 253

G-7.12 Vertical Vessel Supports ................................................................................................................... 267h”! G-7.2 Lifting Lugs ...................................................................................................................................... 269

?? G-7.3 Wind and Seismic Design.. ............................................................................................................... 273

p? RCB-2 Plugging Tubes in Tube Bundle ........................................................................................................ 273

RCB-4 Entrance and Exit Areas ................................................................................................................... 274Fi RCB-6 Gaskets ........................................................................................................................................... 279c, RCB-7 Tubesheets.. .................................................................................................................................... 279

0 RCB-9 Channels, Covers, and Bonnets ........................................................................................................ 260

#?-% RCB-10 Nozzles ............................................................................................................................................ 261

RCB-11 End Flanges and Bolting.. ................................................................................................................ .261

c1 T-2 Fouling ............................................................................................................................................. 263

r” INDEX. ................................................................................................................................................ 291

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NOTES TO USERS OF

THE TEMA STANDARDS

Three classes of Mechanical Standards, R,C and B, reflecting acceptable designs for various service applications arepresented. The user should refer to the definition of each class and choose the one that best fits the specific need.

Corresponding subject matter in the three Mechanical Standards is covered by paragraphs identically numberedexcept for the prefix letter. Paragraph numbers preceded by RCB indicates that all three classes are identical. Anyreference to a specific paragraph must be preceded by the class designation.

The Recommended Good Practice section has been prepared to assist the designer in areas outside the scope of thebasic Standards. Paragraphs in the Standards having additional information in the RGP section are marked with anasterisk (*). The reference paragraph in the RGP section has the identical paragraph number, but with an “RGP” prefix,

It is the intention of the Tubular Exchanger Manufacturers Association that this edition of its Standards may be usedbeginning with the date of issuance, and that its requirements supersede those of the previous edition six monthsfrom such date of issuance, except for heat exchangers contracted for prior to the end of the six month period. Forthis purpose the date of issuance is June 1, 1999.

Questions on interpretation of the TEMA Standards should be formally addressed to the Secretary at TEMA 25 NorthBroadway, Tarrytown, NY 10591. Questions requiring development of new or revised technical Information will onlybe answered through an addendum or a new edition of the Standards.

Upon agreement between purchaserand fabricator, exceptions to TEMA requirements areacceptable. An exchangermay still be considered as meeting TEMA requirements as long as the exception is documented.

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viii

HEAT EXCHANGER NOMENCLATURE SECTION 1

N-l SIZE NUMBERING AND TYPE DESIGNATION-RECOMMENDED PRACTICE

It is recommended that heat exchanger size and type be designated by numbers and letters as describedbelow.

N-l.1 SIZE

Sizes of shells (and tube bundles) shall be designated by numbers describing shell (and tube bundle)diameters and tube lengths, as follows:

N-l.11 NOMINAL DIAMETER

The nomina! diameter shall be the inside diameter of the shell in inches (mm), rounded off tothe nearest mteger. For kettle reboilers the nominal diameter shall be the port diameterfollowed by the shell diameter, each rounded off to the nearest integer.

N-1.12 NOMINAL LENGTH

The nominal length shall be the tube length in inches (mm). Tube length for straight tubesshall be taken as the actual overall length. For U-tubes the length shall be taken as theapproximate straight length from end of tube to bend tangent.

N-l.2 TYPE

Type designation shall be by letters describing stationary head, shell (omitted for bundles only), andrear head, in that order, as indicated in Figure N-l .2.

N-l.3 TYPICAL EXAMPLES

N-l .31

Split-ring floating head exchanger w,ith removable channel and cover, single pass shell,2323~A~~ mm) insrdedrameter wrth tubes 16 (4877 mm) long. SIZE 23-192 (5914877)

N-l.32

U-tube exchanger with bonnet type stationary head, split flow shell, 19” (483 mm) insidediameter with tubes 7’(2134 mm) straight length. SIZE 19-84 (483-2134) TYPE BGU.

N-l.33

Pull-through floating head kettle type reboiler having stationary head integral with tubesheet,23” (584 mm) port diameter and 37” (940 mm) inside shell diameter with tubes 16’(4877 mm)long. SIZE 23/37-192 (584/940 - 4877) TYPE CKT.

N-l.34

Fixed tubesheet exchanger with removable channel and cover, bonnet type rear head, twopass shell, 33-1 8”(841-2438) T’fP 6

(841 mm) inside diameter with tubes 8’(2438 mm) long. SIZE 33-96AFM.

N-l.35

Fixed tubesheet exchanger having stationary and rear heads integral with tubesheets, singlepass shell, 17” (432 mm) inside diameter with tubes lti’(4877 mm) long. SIZE 17-192(4324877) TYPE NEN.

N-l.4 SPECIAL DESIGNS

Special designs are not covered and may be described as best suits the manufacturer. For example,a single tube pass, fixed tubesheet exchanger with conical heads may be described as “TYPE BEMwith Conical Heads”. A pull-through floating head exchanger with an integral shell cover may bedescribed as “TYPE AET with Integral Shell Cover”.

Standards Of The Tubular Exchanger Manufacturers Association 1

SECTION 1 HEAT EXCHANGER NOMENCLATURE

I

,

I

I

2

A

-

B

-

C

v

-

3

-

E

-

F

-

G

-

H

-

J

-

K

-

X

-

FIGURE N-i.2

IHEU NPES

T

1CROSS FLOW

-

1

H

N

-

P

-

5

i

-

u

-

Y

Standards Of The Tubular Exchanger Manufacturers Association

-,

‘-i

A

A

.A

,-,

.1

h,

17

,-,

-\

?

A

A

-1

,I---.

HEAT EXCHANGER NOMENCLATURE SECTION 1

N-2 NOMENCLATURE OF HEAT EXCHANGER COMPONENTS

For the purpose of establishing standard terminology, Figure N-2 illustrates various types of heatexchangers. Typrcal parts and connections, for illustrative purposes only, are numbered for identfficatfon inTable N-2.

TABLE N-2

1. Stationary Head-Channel2. Stationary Head-Bonnet

21. floating Head Cover-External

3. Stationa4. Channel%

Head Flange-Channel or Bonnet22. Floating Tubesheet Skirt23. Packing Box

over5. Stationary Head Nozzle

24. Packing

7: %&&nary Tubesheet25. Packing Gland26. Lantern Ring

6. Shell27. Tierods and Spacers

9. Shell Cover26. Transverse Baffles or Support Plates

10. Shell Flange-Stationary Head End29. Impingement Plate

11. Shell Flange-Rear Head End30. Longitudinal Baffle31. Pass Partition

12. Shell Nozzle13. Shell Cover Flange

32. Vent Connection33. Drain Connection

14. Expansion Joint 34. Instrument Connection15. Floating Tubesheet16. Floating Head Cover

35. Support Saddle

17. Floating Head Cover Flange36. Lifting Lug

16. Floating Head Backing Device;;: Sue$~~rt Bracket

19. Split Shear Ring20. Slip-on Backing Flange

39. Liquid Level Connection40. Floating Head Support

FiGURE N-2

,~ .,


,_

SECTION 1 HEAT EXCHANGER NOMENCLATURE

FIGURE N-2 (continued)

4 Standards Of The Tubular Exchanger Manufacturers Association

,A.

,-,

”

-,,/

,--\

A

HEAT EXCHANGER NOMENCLATURE

FIGURE N-2 (continued)

SECTION 1

Q ,dAJW


SECTION 2 HEAT EXCHANGER FABRICATION TOLERANCES

F-l EXTERNAL DIMENSIONS, NOZZLE AND SUPPORT LOCATIONS

Standard tolerances for process flow nozzles and support locations and projections are shown in FigureF-l. Dimensions in () are millimeters.

FIGURE F-l

c f1/4”(6.4) I 11/8”(3.2)

CONNECTION NOZZLE ALIGNMENT AND SUPPORTTOLERANCES

STACKED EXCHANGERS

ALLOWABLECENTERLINEROTATION

ROTATIONAL TOLERANdE ON NOZZLE FACESAT BOLT CIRCLE


HEAT EXCHANGER FABRICATION TOLERANCES SECTION 2

F-2 RECOMMENDED FABRICATION TOLERANCES

Fabrication tolerances normally required to maintain process flow nozzle and support locations are shownin Figure F-2. These tolerances may be adjusted as necessary to meet the tolerances shown in Figure F-l.Dimensions in () are millimeters.

f1/4”(6.4) , $2”

FIGURE F-2

f l/4-(6.4)

fl/B”(3.2)


SECTION 2 HEAT EXCHANGER FABRICATION TOLERANCES

F-3 TUBESHEETS, PARTITIONS, COVERS AND FLANGES

The standard clearances and tolerances applying to tubesheets, partitions, covers and Ranges are shown inF igure F-3 . D imensions in ( ) are mi l l imeters .

FIGURE F-3

STANDARD CONLlNED JOINT CONSTRUCTION

STANDARD UNCONflNED PIAIN FACE JOINT CONSlTWCTlON

1. SECllON 2 IS NOT INTENOEO TO PROHlBllUNWINEO NEESHER FACES Ml FIATPDKR F#.XFS~ THFREFDRE N O PLUS__._.. ..-__. ..~ _... .~~.IOLERWCE IS SHOW ON R4.

OMENSIONSII

0,. DI. 0,. II,. D5.O6

TOLERANCES 2. NEWTM TOLERANCES SWILL NOT BEir/4- -f/a- (+6.4 - 3 . 2 ) CIMTRUED TO NUN TK41 FlEUL

*l/32’ (i0.B)DIMENS#)NS CAN BE LESS ItW TMREOUIREO BI DESIGN CWULATIONS.

I *l/16- (*1.6) 3. FOR PERIPHER8.L CASKETS, %DNflNED-R, = S/IS- (4.8)~ +D- -l/32’ (+D -0.6) UEANS %MIFINED ON THE OD’.

R2=1/4’ (6.4) R,=1/4’ (6.4) +1/X’ -0’ (t0.a -0) 4. DEWLS ARE IYFwl AN0 w NO1R,= J/16- (4 .8) -l/32’ (-0.8) (KE NOTE 1) PRECLUOE THE USE OF OTHER OETIULS

WHICH ARE FUNCTIDRALLY EOUNALENI.W,.W?.W, *l/32’ (fO.a)

5. FOR UNITS OVER 60’ (1524) TO 1OD’ (2540)OWWXR. TOLERANCES a’ MD -VI* WY BEINCRWXD IO f1/16’(1.6).


HEAT EXCHANGER FABRICATION TOLERANCES

FIGURE F-4

NPS

,,~ il-1/4l-1/2

2-F/23

3-1 I2

/

PERMISSIBLE IMPERFECTIONS IN FLANGE FACING flNlSHFOR RAISED FACE AND LARGE MALE AND FEMALE FLANGES l-2

Maximum Radial Projection of,mperfections Which Aie No Deeper Than

the Bottom of the Serrations. in. (mm)

Mwimum Depth and Radial Projection ofImperfections Which Are Deeper Than the

Bottom of the Serrations, in. (mm)

NOTES:Imperfections must be separated by at least four times the permissible radial projection.Protrusions above the serrations are not permitted.

FLANGE PERIPHERY

\\ I

bIPE SORE\

Sketch showing Radial Projected Length (RPL) serrated gasket face damage

SECTION 2


1.

2.

3.

4.

5.

6.

7.

8.

9.

10.

11.

12.

13.

14.

15.

16.

1 7 ;

18.

19. Tubesheet Liqament is the shortest distance between edge of adjacent tube holes in the tube pattern

20. Welded Tube Joint is a tube-to-tubesheet joint where the tube is welded to the tubesheet.

GENERAL FABRICATION AND PERFORMANCE INFORMATION SECTION 3

DEFINITIONS

Baffle is a device to direct the shell side fluid across the tubes for optimum heat transfer.

Baffle and Suooort Plate Tube Hole Clearance is the diametral difference between the nominal tube CD andthe nominal tube hole diameter in the baffle or support plate.

Conseauential Damaaes are indirect liabilities lying outside the heat exchanger manufacturer’s statedequipment warranty obligations.

DoubleTubesheet Construction is a type of construction in which two (2) spaced tubesheets or equivalent areemployed in lieu of the single tubesheet at one or both ends of the heat exchanger.

Effective Shell and Tube Side Desian Pressures are the resultant load values expressed as uniform pressuresused in the determination of tubesheet thickness for fixed tubesheet heat exchangers and are functions of thenshell side design pressure, the tube side design pressure, the equivalent differential expansion pressure and,the equivalent bolting pressure. ..,

Eauivalent Boltina Pressure is the pressure equivalent resulting from the effects of bolting loads imposed ontubesheets in a fixed tubesheet heat exchanger when the tubesheets are extended for bolting as flangedconnections.

Eauivalent Differential Exoansion Pressure is the pressure equivalent resulting from the effect of tubesheetloadings in a fixed tubesheet heat exchanger imposed by the restraint of differential thermal expansion betweenshell and tubes.

Exoanded Tube Joint is the tube-to-tubesheet joint achieved by mechanical or explosive expansion of the tubeinto the tube hole in the tubesheet.

Expansion Joint “J” Factor is the ratio of the spring rate of the expansion joint to the sum of the axial springrate of the shell and the spring rate of the expansion joint.

Flanae Load Concentration Factors are factors used to compensate for the uneven application of boltingmoments due to large bolt spacing.

Minimumand Maximum Baffleand Suooott Soacinasaredesignlimitationsforthe spacing of bafflesto providefor mechanical integrity and thermal and hydraulic effectiveness of the bundle. The possibility for inducedvibration has not been considered in establishing these values.

Normal Oaeratina Conditions of a shell and tube heat exchanger are the thermal and hydraulic performancerequirements generally specified for sizing the heat exchanger.

Pulsatino Fluid Conditions are conditions of flow generally characterized by rapid fluctuations in pressure andflow rate resulting from sources outside of the heat exchanger.

Seismic Loadings are forces and moments resulting in induced stresses on any member of a heat exchangerdue to pulse mode or complex waveform accelerations to the heat exchanger, such as those resulting fromearthquakes.

Shell and Tube Mean Metal Temoeratures are the average metal temperatures through the shell and tubethicknesses integrated over the length of the heat exchanger for a given steady state operating condition.

Shut-Down Conditions are the conditions of operation which exist from the time of steady state operating,condftions to the time that flow of both process streams has ceased.

.’ Start-Uo Conditions are the conditions of operation which exist from the timethat flow of either or both processstreams is initiated to the time that steady state operating condtions are achieved.Suooort Mate is a device to support the bundle or to reduce unsupported tube span without consideration for

‘.:heat transfer.


_

r.

GENERAL FABRICATION AND PERFORMANCE INFORMATION SECTION 3

FIGURE G-5.2HEAT EXCHANGER SPECIFICATION SHEET


SECTlOk43 GENERAL FABRICATION AND PERFORMANCE INFORMATION

FIGURE G-5.2MHEAT EXCHANGER SPECIFICATION SHE!3

TYpe

Job No.Reference No.Propcwal No.Date Rev.Inem No.

(HorNeft) Connected in Par&l S.xiasSq m: SheUslUnil Swf,Shell (Grass/Eff.) Sqm

PERFORMANCE OF ONE UNITShell Side Tube Side

kglHr

I I

I I I I

--. ____. _Temp. Max,Min---- -,rShe,,

km%“,._

U-Send

Bundle Enhance

TypeTub&c-Tub&wet JointType

Bundle ExitTube sic


GENERAL FABRICATION AND PERFORMANCE INFORMATION~ SECTION 3

G-t SHOP OPERATION

The detailed melhods of shop operation are left to the discretion of the manufacturer in conformity withthese Standards.

G-2 INSPECTION

G-2.1 MANUFACTURER’S INSPECTION

Inspection and testing of units will be provided by the manufacturer unless otherwise specified. Themanufacturer shall carry out the inspections required by the ASME Code, and also inspectionsrequired by state and local codes when the purchaser specifies the plant location.

G-2.2 PURCHASER’S INSPECTION

The purchaser shall have the right to make inspections during fabrication and to witness any testswhen he has so requested. Advance notification shall be given as agreed between the manufacturerand the purchaser.responsibilities.

Inspection by the purchaser shall not relieve the manufacturer of his

G-3 NAME PLATES

G-3.1 MANUFACTURERS NAME PLATE

A suitable manufacturer’s name piate of corrosion resistant material shall be permanently attached tothe head end or the shell of each TEMA exchanger. Name plates for exchangers manufactured inaccordance with Classes “R” and “B” shall be austenitic (300 series) stainless. When insulationthickness is specified by the purchaser, the name plate shall be attached to a bracket welded to theexchanger.

G-3.11 NAME PtATE DATA

In addition to all data required by the ASME Code, a name plate shall also include thefollowing (if provided):

User’s equipment identificationUser’s order number

G-3.12 SUPPLEMENTAL INFORMATION

The manufacturer shall supply supplemental information where it is pertinent to the operationor testing of the exchanger. This would include information pertaining to differential designand test pressure conditions, restrictions on operating conditions for fixed tubesheet typeexchangers, or other restrictrve conditions applicable to the design and/or operation of theunit or its components. Such information can be noted on the name plate or on asupplemental plate attached to the exchanger at the name plate location.

G-3.2 PURCHASER’S NAME PLATE

Purchaser’s name plates, when used, are, to be supplied by the purchaser and supplement ratherthan replace the manufacturers name plate.

G-3.3 TEMA REGISTRATION PLATE

The TEMA organization has adopted a voluntary registration system for TEMA members only. Whena heat exchanger is registered with TEMA, a unique number is assigned to the heat exchanger. ATEMA registration plate, showing this number, is affixed to the heat exchanger and the ASME Codedata report is placed on file at the TEMA office. By referencing this registration number, a copy ofthe ASME Code data report may be obtained by the purchaser from the TEMA office.

G-4 DRAWINGS AND ASME CODE DATA REPORTS

G-4.1 DRAWINGS FOR APPROVAL AND CHANGE

The manufacturer shall submit for purchaser’s approval three (3) prints of an outline drawingshowing nozzle sizes and locations, overall dimensions, supports and weigM. Other drawings maybe furnished as agreed upon by the purchaser and the manufacturer. It is anticipated that areasonable number of minor drawing changes may be required at that time.receipt of approval ma

Changes subsequent to

approval of drawings dycause additional expense chargeable to the purchaser. Purchaser’s

oes not relieve the manufacturer of responsibility for compliance wkh thisStandard and applicable ASME Code requirements. The manufacturer shall not make any changes


SECTION 3 GENERAL FABRICATION AND PERFORMANCE INFORMATION

on the ap roved drawings without express agreement of the purchaser. Shop detail drawings, whileprimarily or mternal use by the fabricator, may be furnished to the purchaser upon request. WhenP.detail drawings are requested, they will only be supplied after outline drawings have been approved.

G-4.2 DRAWINGS FOR RECORD

After approval of drawings, the manufacturer shall furnish three (3) prints or, at his option, atransparency of all approved drawings.

G-4.3 PROPRIETARY RIGHTS TO DRAWINGS

The drawings and the design indicated by them are to be considered the property of themanufacturer and are not to be used or reproduced without his permission, except by the purchaserfor his own internal use.

G-4.4 ASME CODE DATA REPORTSAfter completion of fabrication and inspection of ASME Code stamped exchangers, the manufacturershall furnish three (3) copies of the ASME Manufacturer’s Data Report.

G-5 GUARANTEES

G-5.1 GENERALThe specific terms of the guarantees should be agreed upon by the manufacturer and purchaser.Unless otherwise agreed upon by the manufacturer and purchaser, the following paragraphs in thissection will be applicable.

G-5.2 PERFORMANCE

The purchaser shall furnish the manufacturer with all information needed for clear understanding ofperformance requirements, including any special requirements. The manufacturer shall guaranteethermal performance and mechanical design of a heat exchanger, when operated at the desi n

1conditions specified by the purchaser in his order, or shown on the exchanger specificatron s eetfurnished by the manufacturer (Figure G-5.2, G-5.2M). This guarantee shall extend for a period oftwelve (12) months after shipping date. The manufacturer shall assume no responsibility forexcessive fouling of the apparatus by material such as coke, silt, scale, or any forergn substance thatmay be deposited. The thermal guarantee shall not be applrcable to exchangers where the thermalperformance rating was made by the purchaser.

G-5.21 THERMAL PERFORMANCE TEST

A performance test shall be made if it is established after operation that the performance ofthe exchanger is not satisfactory, provided the thermal performance rating was made by themanufacturer. Test conditions and procedures shall be selected by agreement between thepurchaser and the manufacturer to permit extrapolation of the test results to the specifieddesign conditions.

G’S22 DEFECTIVE PARTS

The manufacturer shall repair or replace F.O.B. his plant any parts proven defective within theguarantee period. Finished materials and accessories purchased from other manufacturers,including tubes, are warranted only to the extent of the original manufacturer’s warranty to theheat exchanger fabricator.

G-5.3 CONSEQUENTIAL DAMAGES

The manufacturer shall not be held liable for any indirect or consequential damage.

G-5.4 CORROSION AND VIBRATION

The manufacturer assumes no responsibility for deterioration of any part or parts of the equipmentdue to corrosion, erosion, flow induced tube vibration, or any other causes, regardless of when suchdeterioration occurs after leaving the manufacturer’s premises, except as provided for in ParagraphsG-5.2 and G-5.22.


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GENERAL FABRICATION AND PERFORMANCE INFORMATION

G-5.5 REPLACEMENT AND SPARE PARTS

SECTION 3

Whenreplacement or spare tube bundles, shells, or other parts are purchased, the manufacturer isto guarantee satisfactory fit of such parts only if he was the original manufacturer. Parts fabricated todrawings furnished by the purchaser shall be guaranteed to meet the dimensions and tolerancesspecified.

G-6 PREPARATION OF HEAT EXCHANGERS FOR SHIPMENT

G-6.1 CLEANING

Internal and external surfaces are to be free from loose scale and other foreign material that is readilyremovable by hand or power brushing.

G-6.2 DRAINING

Water, oil! or other liquids used for cleaning or hydrostatic testing are to be drained from all unitsbefore shrpment. This is not to imply that the unrts must be completely dry.

G-6.3 FLANGE PROTECTION

All exposed machined contact surfaces shall be coated with a removable rust preventative andprotected against mechanical damage by suitable covers.

G-6.4THREADED CONNECTION PROTECTION

All threaded connections are to be suitably plugged.

G-6.5 DAMAGE PROTECTION

The exchanger and any spare pans are to be suitably protected to prevent damage during shipment.

G-6.6 EXPANSION JOINT PROTECTION

External thin walled expansion bellows shall be equipped with a protective cover which does notrestrain movement.

G-7 GENERAL CONSTRUCTION FEATURES OF TEMA STANDARD HEAT EXCHANGERS

G-7.1 SUPPORTS

All heat exchangers are to be provided with supports.

*G-7.11 HORIZONTAL UNITS

The supports should be designed to accommodate the weight of the unit and contents,including the flooded weight during hydrostatic test.

For units with removable tube bundles, supports should be designed to withstand a pullingforce equal to l-1/2 times the weight of the tube bundle.

For purposes of support design, forces from external nozzle loadings, wind and seismicevents are assumed to be negligible unless the purchaser specifically details therequirements. When these additional loads and forces are required to be considered, thecombinations need not be assumed to occur simultaneously.

The references under Paragraph G-7.1 3 may be used for calculating resulting stresses due tothe saddle supports.

Horizontal units are normally provided with at least two saddle type supports, with holes foranchor bolts. The holes in all but one of the sup arts are to be elongated to accommodateaxial movement of the unit under operating con c!.rtrons. Other types of support may be used ifall design criteria are met, and axial movement is accommodated.

*G-7.12 VERTICAL UNITS

Vertical units are to be provided with supports adequate to meet design requirements. Thesupports may be of the lug, annular ring, leg or skirt type. If the unit is to be located in asupporting structure, the supports should be of sufficient size to allow clearance for the bodyflanges.


INSTALLATION, OPERATION AND MAINTENANCE SECTION 4

E-l PERFORMANCE OF HEAT EXCHANGERS

Satisfactory operation of heat exchangers can be obtained only from units which are properly designed andhave built-in quality. Correct installation and preventive maintenance are user responsibilities.

‘E-i.1 PERFORMANCE FAILURES

The failure of heat exchanger equipment to perform satisfactorily may be caused by one or morefactors, such as:

(1) Excessive fouling.

(2) Air or gas binding resulting from improper piping installation or lack of suitable vents

(3) Operating condftions differing from design conditions.

(4) Maldistribution of flow in the unit.

(5) Excessive clearances between the baffles and shell and/or tubes, due to corrosion.

(6) Improper thermal design

The user’s best assurance of satisfactory performance lies in dependence upon manufacturerscompetent in the design and fabrication of heat transfer equipment.

E-2 INSTALLATION OF HEAT EXCHANGERS

E-2.1 HEAT EXCHANGER SETTINGS

E-2.11 CLEARANCE FOR DISMANTLING

For straight tube exchangers fitted with removable bundles, provide sufficient clearance at thestationary head end tospace beyond the rear R

ermit removal of the bundle from the shell and provide adequateead to permit removal of the shell cover and/or ffoating head cover.

For fixed tubesheet exchangers, provide sufficient clearance at one end to permit withdrawaland replacement of the tubes, and enough space beyond the head at the opposite end topermit removal of the bonnet or channel cover.

For U-tube heat exchangers, provide sufficient clearance at the stationary head end’to permitwithdrawal of the tube bundle, or at the opposite end to permit removal of the shell.

E-2.12 FOUNDATIONS

Foundations must be adequate so that exchangers will not settle and impose excessivestrains on the exchanger. Foundation bolts should be set to allow for setting inaccuracies. Inconcrete footings, pipe sleeves at least one size larger than bolt diameter slipped over thebolt and cast in place are best for this purpose, as they allow the bolt center to be adjustedafter the foundation has set.

E-2.13 FOUNDATION BOLTS

Foundation bolts should be loosened at one end of the unit to allow free expansion of shells.Slotted holes in suppotts are provided for this purpose.

E-2.14 LEVELINGExchangers must be set level and square so that pipe connections may be made withoutforcing.

E-2.2 CLEANLINESS PROVISIONS

E-2.21 CONNECTION PROTECTORS

All exchanger openings should be inspected for foreign material. Protective plugs and coversshould not be removed until just prior to installation.

E-2.22 DIRT REMOVALThe entire system should be clean before starting operation. Under some conditions, the useof strainers in the piping may be required.


SECTION 4 INSTALLATION, OPERATION AND MAINTENANCE

E-Z.23 CLEANING FACILITIES

Convenient means should be provided for cleaning the unit as suggested under “Maintenanceof Heat Exchangers,” Paragraph E-4.

E-2.3 FITTINGS AND PIPING

E-2.31 BY-PASS VALVES

It may be desirable for purchaser to provide valves and by-passes in the piping system topermit inspection and repairs.

E-2.32 TEST CONNECTIONS

When not integral with the exchanger nozzles, thermometer well and pressure gageconnections should be installed close to the exchanger in the inlet and outlet piping.

E-2.33 VENTS

Vent valves should be provided by purchaser so units can be purged to prevent vapor or gasbinding. Special consideration must be given to discharge of hazardous or toxic fluids,

E-2.34 DRAINS

Drains may discharge to atmosphere, lf permissible, or into a vessel at lower pressure. Theyshould not be piped to a common closed manifold.

E-2.35 PULSATION AND VIBRATION

In all installations, care should be taken to eliminate or minimize transmission of fluidpulsations and mechanical vibrations to the heat exchangers.

E-2.36 SAFETY RELIEF DEVICES

The ASME Code defines the requirements for safety relief devices. When specified by thepurchaser, the manufacturer will provide the necessary connections for the safety reliefdevices. The size and ty e of the required connections will be specified by the purchaser.

.sThe purchaser will prow e and tnstall the required relief devices.

E-3 OPERATION OF HEAT EXCHANGERS

E-3.1 DESIGN AND OPERATING CONDITIONS

Equipment must not be operated at conditions which exceed those specified on the name plate(s).

E-3.2 OPERATING PROCEDURES

Before placing any exchanger in operation, reference should be made to the exchanger drawings,specification sheet(s) and name plate(s) for any special instructions. Local safety and healthregulations must be considered. Improper start-up or shut-down sequences, particularly of fixedtubesheet units, may cause leaking of tube-to-tubesheet and/or bolted flanged joints.

E-3.21 START-UP OPERATION

Most exchangers with removable tube bundles may be placed in service by first establishingcirculation of the cold medium, followed by the gradual introduction of the hot medium.During start-up all vent valves should be opened and left open until all passages have beenpurged of air and are completely filled with fluid. For fixed tubesheet exchangers, flutds mustbe introduced in a manner to minimize differential expansion between the shell and tubes.

E-3.22 SHUT-DOWN OPERATION

For exchangers with removable bundles, the units may be shut down by first graduallystopping the flow of the hot medium and then stopping the flow of the cold medium. If it isnecessary to stop the flow of cold medium, the circulation of hot medium through theexchanger should also be stopped. For fixed tubesheet exchangers, the unit must be shutdown in a manner to minimize differential expansion between shell and tubes. When shumngdown the system, all units should be drained completely when there is the possibility offreezing or corrosion damage. To guard against water hammer, condensate should be

‘i 18 Standards Of The Tubular Exchanger Manufacturers Association

INSTALLATION, OPERATION AND MAINTENANCE SECTION 4

drained from steam heaters and similar apparatus during start-up or shut-down. To reducewater retention after drainage, the tube side of water cooled exchangers should be blown out

wi th a i r .

E-3.23 TEMPERATURE SHOCKS

Exchangers normallmust not be

should not be subjected to abrupt temperature fluctuations. Hot fluidsudden y Introduced when the unit is cold, nor cold fluid suddenly introduced7.

when the unit is hot.

E-3.24 BOLTED JOINTS

Heat exchangers are pressure tested before leaving the manufacturer’s shop in accordancewith ASME Code requirements. However, normal relaxing of the gasketed joints may occur inthe interval between testing in the manufacturer’s shop and installation at the jobsite.Therefore, all external bolted joints may require retightening after installation and, ifnecessary, after the exchanger has reached operating temperature.

E-3.25 RECOMMENDED BOLT TIGHTENING PROCEDURE

It is important that all bolted joints be tightened uniformly and in a diametrfcally staggeredpattern, as illustrated in Figure E3.25, except for special high pressure closures when theinstructions of the manufacturer should be followed.

FIGURE E-3.25

S T A R TI I 16

IS I *E-4 MAINTENANCE OF HEAT EXCHANGERS

E-4.1 INSPECTION OF UNIT

At regular intervals and as frequently as experience indicates, an examination should be made of theinterior and exterior condition of the unit. Neglect in keeping all tubes clean may result in completestoppage of flow through some tubes which could cause severe thermal strains, leaking tube joints,or structural damage to other components. Sacrificial anodes, when provided, should be inspected

to determine whether they should be cleaned or replaced.

,E-4.11 INDICATIONS OF FOULING

Exchangers subject to fouling or scaling should be cleaned periodically. A light sludge orscale coating on the tube greatly reduces its efficiency. A marked increase in pressure dropand/or reduction in performance usually indicates cleaning is necessary. The umt should firstbe checked for air or vapor binding to confirm that this is not the cause for the reduction inperformance. Since the difficulty of cleaning increases rapidly as the scale thickness ordeposit increases, the intervals between cleanings should not be excessive.


SECTION 4 INSTALLATION, OPERATION AND MAINTENANCE

E-4.12 DISASSEMBLY FOR INSPECTION OR CLEANING

Before disassembly, the user must assure himsdf that the unit has been depressurized,vented and drained, neutralized and/or purged of hazardous material.

To inspect the inside of the tubes and also make them accessible for cleaning, the followingprocedures should be used:

(1) Stationary Head End

(a) Type A, C, D & N, remove cover only

(b) Type 6, remove bonnet

(2) Rear Head End

(a) Type L, N & P, remove cover only

(b) Type M, remove bonnet

(c) Type S &T, remove shell cover and floating head cover

(d) Type W, remove channel cover or bonnet

E-4.13 LOCATING TUBE LEAKS

The following procedures may be used to locate perforated or split tubes and leaking jointsbetween tubes and tubesheets. In most cases, the entire front face of each tubesheet will beaccessible for inspection. The point where water escapes indicates a defective tube ortube-to-tubesheet joint.

(l)i;;t; ;;$l.removable channel cover: Remove channel cover and apply hydraulic pressure

(2) Unfts with bonnet type head: For fixed tubesheet units where tubesheets are an integralpart of the shell, remove bonnet and apply hydraulic pressure in the shell. For fixedtubesheet units where tubesheets are not an integral part of the shell and for units withremovable bundles, remove bonnet, re-bolt tubesheet to shell or install test flange or gland,whichever is applicable, and apply hydraulic pressure in the shell. See Figure E-4.13-1 fortypical test flange and test gland.

FIGURE E-4.13-1

(3) Units with Type S or T floating head: Remove channel cover or bonnet, shell cover andfloating head cover. Install test ring and bolt in place with gasket and packing. Applyhydraulic pressure in the shell. A typical test ring is shown in Figure E-4.13-2. When a testring is not available t is possible to locate leaks m the floating head end by removing theshell cover and applying hydraulic pressure in the tubes. Leaking tube joints may then belocated by sighting through the tube lanes. Care must be exercised when testing partiallyassembled exchangers to prevent over extension of expansion joints or overloading oftubes and/or tube-to-tubesheet joints.

(4) Hydrostatic test should be performed so that the temperature of the metal is over 60” F(16OC) unless the materials of construction have a lower nil-ductility transition temperature.


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INSTALLATION, OPERATION AND MAINTENANCE

FIGURE E-4.13-2

SECTION 4

FLOATING TUGESHEETSHELL FLANGE- REAR HEAD END

E-4.2 TUBE BUNDLE REMOVAL AND HANDLING

To avoid possible damage during removal of a tube bundle from a shell, a pulling device should beattached to eyebolts screwed into the tubesheet. If the tubesheet does not have tapped holes for

eyebolts, steel rods or cables inserted through tubes and attached to bearing plates may be used.The bundle should be supported on the tube baffles, supports or tubesheets to prevent damage tothe tubes.

Gasket and packing contact surfaces should be protected.

E-4.3 CLEANING TUBE BUNDLES

E-4.31 CLEANING METHODS,~ The heat transfer surfaces of heat exchangers should be kept reasonably clean to assure

satisfactory performance. Convenient means for cleaning should be made available.

Heat exchangers may be cleaned by either chemical or mechanical methods. The methodselected must be the choice of the operator of the plant and will depend on the type ofdeposit and the facilities available in the plant.may be considered:

Following are several cleaning procedures that

(1) Circulating hot wash oil or light distillate through tubes or shell at high velocity mayeffectively remove sludge or similar soft deposits.

(2) Some salt deposits may be washed out by circulating hot fresh water.

(3) Commercial cleaning compounds are available for removing sludge or scale provided hotwash oil or water is not available or does not give satisfactory results.

(4) High pressure water jet cleaning.

(5) Scrapers, rotating wire brushes, and other mechanical means for removing hard scale,coke, or other deposits.


SECTION 4 INSTALLATION, QPERATION AND MAINTENANCE

(6) Employ services of aorganizations will checR

ualified organization that provides cleaning services. Thesethe nature of the deposits to be removed, furnish proper solvents

and/or acid solutions containing inhibitors, and provide equipment and personnel for acomplete cleaning job.

E-4.32 CLEANING PRECAUTIONS

(1) Tubes should not be cleaned by blowing steam through individual tubes since this heatsthe tube and may result in severe expansion strain, deformation of the tube, or looseningof the tube-to-tubesheet joint.

(2)t;;;;b;Fhanically cleaning a tube bundle, care should be exercised to avoid damaging

(3) Cleaning compounds must be compatible with the metallurgy of the exchanger.

E-4.4 TUBE EXPANDING

A suitable tube expander should be used to tighten a leaking tube joint. Care should be taken toensure that tubes are not over expanded.

E-4.5 GASKET REPLACEMENT

Gaskets and gasket surfaces should be thoroughly cleaned and should be free of scratches andother defects. Gaskets should be properly positioned before attempting to retighten bolts. It isrecommended that when a heat exchanger is dismantled for any cause, it be reassembled with newgaskets. This will tend to prevent future leaks and/or damage to the gasket seating stirfaces of theheat exchanger. Composition gaskets become dried out and brittle so that they do not alwaysprovide an effective seal when reused.flow to match their contact surfaces.

Metal or metal jacketed gaskets, when compressed initially:In so doing they are work hardened and, if reused, may prowde

an imperfect seal or result in deformation and damage to the gasket contact surfaces of theexchanger.

Bolted joints and flanges are designed for use with the particular type of gasket specified.Substitution of a gasket of different construction or improper dimensions may result in leakage anddamage to gasket surfaces. Therefore, any gasket substitutions should be of compatible design.

Any leakage at a gasketed joint should be rectified and not permitted to persist as it may result indamage to the gasket surfaces.

Metal jacketed type gaskets are widely used. When these are used with a tongue and groove jointwithout a nubbin, the gasket should be installed so that the tongue bears on the seamless side of thegasket jacket. When a nubbin is used, the nubbin should bear on the seamless side.

E-4.6 SPARE AND REPLACEMENT PARTS

The procurement of spare or re lacement parts from the manufacturer will be facilitated if the correctname for the part, as shown in 8ectlon 1, Table N-2, of these Standards is given, together with theserial number, type, size, and other information from the name plate. Replacement parts should bepurchased from the original manufacturer.

E-4.7 PLUGGING OF TUBES

In U-tube heat exchangers, and other exchangers of special design, it may not be feasible to removeand replace defective tubes. Defective tubes may be plugged using commercially available taperedplugs with ferrules or tapered only plugs which may or may not be seal welded. Excessive tubeplugging may result in reduced thermal performance, higher pressure drop, and/or mechanicaldamage. It is the user’s responsibility to remove plugs and neutralize the bundle prior to sending itto a shop for repairs.


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C B

RCB-1 SCOPE AND GENERAL REQUIREMENTS

RCB-1.1 SCOPE OF STANDARDS

RCB-1.11 GENERAL

The TEMA Mechanical Standards are applicable to shell and tube heat exchangers which donot exceed any of the following criteria:

(1) inside diameters of 100 inches (2540 mm)

(2) product of nominal diameter, inches (mm) and design pressure, psi (kPa) of 100,000(175x106)

(3) a design pressure of 3,OW psi (20664 kPa)

The intent of these parameters is to limit the maximum shell wall thickness to approximately 3inches (76 mm), and the maximum stud diameter to approximately4 inches (102 mm).Criteria contained in these Standards may be applied to units which exceed the aboveparameters.

R-1.12 DEFINITION OF TEMA CLASS “R” EXCHANGERS

The TEMA Mechanical Standards for Class “R” heat exchangers specify design andfabrication of unfired shell and tube heat exchangers for the generally severe requirements ofpetroleum and related processing applications.

C-1.12 DEFINITION OF TEMA CLASS “c” EXCHANGERS

The TEMA Mechanical Standards for Class “c” heat exchangers specify design andfabrication of unfired shell and tube heat exchangers for the generally moderate requirementsof commercial and general process applications.

B-1.12 DEFINITION OF TEMA CLASS “B” EXCHANGERS

The TEMA Mechanical Standards for Class “B” heat exchangers specify design andfabrication of unfired shell and tube heat exchangers for chemical process service.

RCB-1.13 CONSTRUCTION CODESThe individual vessels shall comply with the ASME (American Society of MechanicalEngineers) Boiler and Pressure Vessel Code, Section VIII, Division 1, hereinafter referred toas the Code. These Standards supplement and define the Code for heat exchangerapplications. The manufacturer shall comply with the construction requirements of state andlocal codes when the purchaser specifies the plant location. It shall be the responsibility ofthe purchaser to inform the manufacturer of any applicable local codes. Application of theCode symbol is required, unless otherwise specified by the purchaser.

RCB-1.14 MATERIALS-DEFINITION OF TERMS

For purposes of these Standards, “carbon steel” shall be construed as any steel or low alloyfalling within the scope of Part UCS of the Code. Metals not included by the foregoing (exceptcast iron) shall be considered as “alloys” unless otherwise specifically named. Materials ofconstruction, including gaskets, should be specified by the purchaser. The manufacturerassumes no responsibility for deterioration of parts for any reason.

RCB-1.2 DESIGN PRESSURE

RCEJ-1.21 DESIGN PRESSURE” Designpressures~ftir the shell and tube sides shall be specified separately by the purchaser.

Rc~~1.3 TEST& ~‘.

~~~-1.31 STANDARD TEST

The exchanger shall be hydrostatically tested with water. The test pressure shall be held forat least 30 minutes. The shell side and the tube side are to be tested separately in such amanner that leaks at the tube joints can be detected from at least one side. When the tubeside design pressure is the higher pressure, the tube bundle shall be tested outside of theshell only if specified by the purchaser and the construction permits. Welded joints are to be



sufficiently cleaned prior to tasting the exchanger to permit proper inspection during the test.;;dEinimum hydrostatrc test pressure at room temperature shall be in accordance with the

RCB-1.311 OTHER LIQUID TESTS

Liquids other than water may be used as a testing medium if agreed upon between thepurchaser and the manufacturer.

RCB-1.32 PNEUMATIC TEST

When liquid cannot be tolerated as a test medium the exchanger may be given a pneumatictest in accordance with the Code. It must be recognized that air or gas is hazardous whenused as a pressure testing medium. The pneumatic test pressure at room temperature shallbe in accordance with the Code.

RCB-1.33 SUPPLEMENTARY AIR TEST

When a supplementary air or gas test is specified by the purchaser, it shall be preceded bthe hydrostatic test required by Paragraph RCB-1.31. The test pressure shall be as agreedyupon by the purchaser and manufacturer, but shall not exceed that required by ParagraphRCB-1.32.

RCB-1.4 METAL TEMPERATURES

RCB-1.41 METAL TEMPERATURE LIMITATIONS FOR PRESSURE PARTS

The metal temperature limitations for various metals are those prescribed by the Code.

RCB-1.42 DESIGN TEMPERATURE OF HEAT EXCHANGER PARTS

RCB-1.421 FOR PARTS NOT IN CONTACT WITH BOTH FLUIDS

Design temperatures for the shell and tube sides shall be specified sepurchaser. The Code provides the allowable stress limits for parts to g

arately by the

the specified design temperature.e deslgned at

RCB-1.422 FOR PARTS IN CONTACT WITH BOTH FLUIDS

The design temperature is the design metal temperature and is used to establish theCode stress limits for design. The design metal temperature shall be based on theoperating temperatures of the shellside and the tubeside fluids, except when thepurchaser specffies some other design metal temperature. When the design metalternRCfir

erature is less than the higher of the design temperatures referred to in Paragraph-1.421, the design metal temperature and the affected parts shall be shown on the

manufacturers nameplate(s) as described in Paragraph G-3.1.

RCB-1.43 MEAN METAL TEMPERATURES

RCB-1.431 FOR PARTS NOT IN CONTACT WITH BOTH FLUIDSThe mean metal temperature is the calculated metal temperature, under specifiedoperating conditions, of a part in contact with a fluid. It is used to establish metalproperties under operating conditions. The mean metal temperature is based on thespecified operating temperatures of the fluid in contact with the part.

RCB-1.432 FOR PARTS IN CONTACT WITH BOTH FLUIDS

The mean metal temperature is the calculated metal temperature, under specifiedoperating conditions, of a part in contact with both shellside and tubeside fluids. It isused to establish metal properties under operating conditions. The mean metaltemperature is based on the specified operating temperatures of the shellside andtubeside fluids. In establishing the mean metal temperatures, due consideration shallbe given to such factors as the relative heat transfer coefficients of the two fluidscontacting the part and the relative heat transfer area of the parts contacted by the twofluids.

RCB-1.5 STANDARD CORROSION ALLOWANCES

The standard corrosion allowances used for the various heat exchanger parts are as follows, unlessthe conditions of service make a different allowance more suitable and such allowance is specifiedby the purchaser.


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MECHANICAL STANDARDS TEMA CLASS R C B SECTION 5

9 RCB-1.51 CARBON STEEL PARTS

F3 R-1.511 PRESSURE PARTS

8 All carbon steel pressure parts, except as noted below, are to have a corrosion

c-)allowance of l/5’ (3.2 mm).

0CB-1.511 PRESSURE PARTS

QAll carbon steel pressure parts, except as noted below, are to have a corrosionallowance of l/16” (1.6 mm).

0 RCB-1.512 INTERNAL FLOATING HEAD COVERSQ Internal floating head covers are to have the corrosion allowance on all wetted

dsurfaces except gasket seating surfaces. Corrosion allowance on the outside of theflanged portion may be included in the recommended minimum edge distance.

Q

6 :, ,,,: ., ; ~. ,, y-‘y TUBEsHEETsTubesheets are to have the corrosion allowance on each side with the provision that,

on the grooved side of a grooved tubesheet, the depth of the gasketed groove may be” considered as available for corrosion allowance.

0RCB-1.514 EXTERNAL COVERS

0Where flat external covers are grooved, the depth of the gasketed groove may beconsidered as available for corrosion allowance.

0 RCB-1.515 END FLANGESc Corrosion allowance shall be applied only to the inside diameter of flanges where

fi exposed to the fluids.

0 RCB-1.516 NONPRESSURE PARTS

fl Nonpressure parts such as tie-rods, spacers, baffles and support plates are notrequired to have corrosion allowance.

0

QRCB-1.517TUBES, BOLTING AND FLOATING HEAD BACKING DEVICES

Tubes, bolting and floating head backing devices are not required to have corrosionQ allowance.

Q RCB-1.518 PASS PARTITION PLATES

E? Pass partition plates are not required to have corrosion allowance.

9 RCB-I .52 ALLOY PARTS

n Alloy parts are not required to have corrosion allowance.

fz R-l.53 CAST IRON PARTS

0 Cast iron pressure parts shall have a corrosion allowance of l/8” (3.2 mm).

c CB-1.53 CAST IRON PARTS

c13 Cast iron pressure parts shall have a corrosion allowance of I/l 6” (1.6 mm).

Q RCB-1.6 SERVICE LIMITATIONS

Q RB-1.61 CAST IRON PARTS9 Cast iron shall be used only for water service at pressures not exceeding 150 psi (1034 kPa).$3

C-1.61 CAST IRON PARTSp? Cast iron shall not be used for pressures exceeding I50 psi (1034 kPa), or for lethal or

rflammable fluids at any pressure.

Q

83,F, Standards Of The Tubular Exchanger Manufacturers Association 25m

9


RCB-1.62 EXTERNAL PACKED JOINTS

Packed joints shall not be used when the purchaser specifies that the fluid in contact with thejoint is lethal or flammable.

RCB-1.7 ANODES

Selection and placement of anodes is not the responsibility of the heat exchanger manufacturer. If aheat exchanger is to be furnished with anodes, when requesting a quotation, the purchaser isresponsible for furnishing the heat exchanger manufacturer the following information:

(1) Method of anode attachment.

(2) Quantity of anodes required.

(3) Size and manufacturer of the anodes.

(4) Anode material.

(6) Sketch of anode locations and spacing.

If the heat exchanger manufacturer chooses to install anodes for a customer, the manufacturer is notresponsible for the suitability of the anodes for the service it is installed in, the life of the anodes, thecorrosion protection provided by the anode, or any subsequent damage to the heat exchangerattributed to the anode, the method of anode installation, or the installed location of the anode in theheat exchanger.



*RCB-2 TUBES

RCB-2.1 TUBE LENGTH

The following tube lengths for both straight and U-tube exchangers are commonly used: 96 (2438),120 (3048), 144 (3658), 192 (4877) and 240 (6096) inches (mm). Other lengths may be used. Alsosee Paragraph N-l .12.

RCB-2.2 TUBE DIAMETERS AND GAGES

RCB-2.21 BARE TUBES

Table RCB-2.21 lists common tube diameters and gages for bare tubes of copper, steel andalloy. Other diameters and gages are acceptable.

TABLE RCB-2.21

BARE TUBE DIAMETERS AND GAGES

O.D.Inches(mm)

Copper and Copper Alloys Carbon Steel, Aluminum Other Alloysand Aluminum Alloys

B.W.G. B.W.G. B.W.G.

27 272422 :z

222018 I

20 2018 18

(X, 20 20

:“6

4:

14 ;“6

(zl ) 20 18 16 14 1:16 12 14

:: 14 12 1:14 10 12

Notes:1, Wall thickness shall be specified as either minimum or average.

2. Characteristics of tubing are shown in Tables D-7 and D7M.

RCB-2.22 INTEGRALLY FINNED TUBESThe nominal fin diameter shall not exceed the outside diameter of the unfinned section.Specified wall shall be based on the thickness at the root diameter.



RCB-2.3 U-TUBES

RCB-2.31 U-BEND REQUIREMENTSWhen U-bends are formed, it is normal for the tube wall at the outer radius to thin. Theminimum tube wall thickness in the bent portion before bending shall be:dot,=t, l’z

I 1where

to = Original tube wall thickness, inches (mm)t, = Minimum tuba wall thickness calculated by Coda rules for a straight tube

subjected to the same pressure and metal temperature, inches (mm)do= Outside tube diameter, inches (mm)R= Mean radius of bend, inches (mm)

More than one tuba gage, or dual gage tubes, may be used in a tube bundle.When IJ-bends are formed from tube materials which are rafatively non-work-hardening andof suitable temper, tube wall thinning in the bends should not exceed a nominal 17% oforiginal tube wall thickness.Flattening at the bend shall not exceed 10% of the nominal tube outside diameter.U-bends formed from tube materials having low ductility, or materials which are susceptible towork-hardening, may require special consideration. Also refer to Paragraph RCB-2.33.

RCB-2.32 BEND SPACING

RCB-2.321 CENTER-TO-CENTER DIMENSIONThe center-to-center dimensions between parallel legs of U-tubes shall be such thatthey can be inserted into the baffle assembly without damage to the tubes.

RCB-2.322 BEND INTERFERENCEThe assembly of bends shall be of workmanlike appearance. Metal-to-metal contactbetween bends in the same plane shall not be permitted.

RCB-2.33 HEATTREATMENTCold work in forming U-bends may induce embrittlement or susceptibility to stress corrosionin certain materials and/or environments. Heat treatment to alleviate such conditions may beperformed by agreement between manufacturer and purchaser.

RCB-2.4 TUBE PATTERNStandard tube patterns are shown in Figure RCB-2.4.

FIGURE RCB-2.4

Triangular RotatedTriangular

squareRotatedsquare

Note: Flow arrows are perpendicular to the baffle cut edge.

28 Stantfards Of The Tubular Exchanger Manufacturers Association


RCB-2.41 SQUARE PATTERN

In removable bundle units, when mechanical cleaning of the tubes is specified by thepurchaser, tuba lanes should be continuous.

RCB-2.42 TRIANGULAR PATTERN

Triangular or rotated triangular pattern should not be used when the shell side is to becleaned mechanically.

R-2.5 TUBE PITCH

Tubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameterof the tube. When mechanical cleaning of the tubes is specified by the purchaser, minimum cleaning

lanes of l/4” (6.4 mm) shall be provided.

C-2.5 TUBE PITCHTubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameterof the tube. Where the tube diameters are 5/8” (15.9 mm) or less and tuba-to-tubesheet joints are

” expanded only, the minimum center-to-center distance may be reduced to 1.20 times the outsidediameter.

B-2.5 TUBE PITCH

Tubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameterof the tube. When mechanical cleaning of the tubes is specified by the purchaser and the nominalshell,diameter is 12 inches (305 mm) or less, minimum cleaning lanes of 3/16” (4.8 mm) shall beprovrded. For shell diameters greater than 12 inches (305 mm), minimum cleaning lanes of t/4” (6.4mm) shall be provided.



RCB-3 SHELLS AND SHELL COVERS

RCB-3.1 SHELLS

RCB4.11 SHELL DIAMETERS

It shall be left to the discretion of each manufacturer to establish a system of standard shelldiameters within the TEMA Mechanical Standards in order to achieve the economies peculiarto his individual design and manufacturing facilities.

RCB-3.12 TOLERANCES

RCB-3.121 PIPE SHELLS

The inside diameter of pipe shells shall be in accordance with applicable ASTM/ASMEpipe specifications.

RCB-3.122 PLATE SHELLS

The inside diameter of any plate shell shall not exceed the design inside diameter bymore than l/8” (3.2 mm) as determined by circumferential measurement.

RCB-3.13 MINIMUM SHELL THICKNESS

Shell thickness is determined by the Code design formulas, plus corrosion allowance, but inno case shall the nominal thickness of shells be less than that shown in the applicable table.The nominal total thickness for clad shells shall be the same as for carbon steel shells.

30

TABLE R-3.13MINIMUM SHELLTHICKNESS

Dimensions In Inches (mm)

Minimum Thickness

Nominal Shell Diameter Carbon Steel Alloy *

Pipe Plate

6 11521 SCH. 40

8-12 I 330-737)203:305) SCH. 30 -13-29 SCH. STD 318;:g (762-991) 7116

61 -HO j: ;;:::;:j :i: (12.7)

118 (3.2)

1 112 (t2.7j ) 6/8 (9.5) )

Nominal Shell Diameter

TABLE CB-3.13MINIMUM SHELL THICKNESS


Minimum Thickness

Carbon Steel

lil ;; pEEL&

t 610 737 I24-2930-39 762 1 99140-60 (10161524)61 -80 (1549-2032)81 100 (2057-2540)

Pipe

SCH. 40

Plate

-51165116

7$? (l%It/2 (12.7)‘I2 (12.7)

Alloy *

I-

*Schedule 5s is permissible for 6 inch (152 mm) and 8 inch (203 mm) shell diameters.



RCB-3.2 SHELL COVER THICKNESS

Nominal thickness of shell cover heads, before forming, shall be at least equal to the thickness of theshell as shown in the applicable table.

RCB-4 BAFFLES AND SUPPORT PLATES

RCB-4.1 TYPE OF TRANSVERSE BAFFLES

The segmental or multi-segmental type of baffle or tube support plate is standard. Other type bafflesare permissible. Baffle cut is defined as the segment opening height expressed as athe shell inside diameter or as a percentage of the total net free area inside the shell P

ercentage ofshell cross

sectional area minus total tube area). The number of tube rows that overlap for multi-segmentalbaffles should be adjusted to give approximately the same net free area flow through each baffle.Baffles shall be cut near the centerline of a row of tubes, of a pass lane, of a tube lane, or outside the

tube pattern. Baffles shall have a workmanlike finish on the outside diameter. Typical baffle cuts areillustrated in Figure RCB-4.1. Baffle cuts may be vertical, horizontal or rotated.

FIGURE RCB-4.1BAFFLE CUTS FOR SEGMENTAL BAFFLES

.cJ c3 6BAFFLE CUTS FOR MULTI-SEGMENTAL BAFFLES

DOUBLE SEGMENTAL

RCB-4.2 TUBE HOLESTRIPLE SEGMENTAL

Where the maximum unsupported tube length is 36 inches (914 mm) or less, or for tubes larger indiameter than l-1 /4 inches (31.8 mm) OD, standard tube holes are to be l/32 inch (0.8 mm) over theOD of the tubes. Where the unsupponed tube length exceeds 36 inches (914 mm) for tubes 1 -l/4inches (31.8 mm) diameter and smaller, standard tube holes are to be l/64 inch (0.4 mm) over the

OD of the tubes. For pulsating conditions, tube holes may be smaller than standard. Any burrs shallbe removed and the tube holes given a workmanlike finish. Baffle holes will have an over-toleranceof 0.010 inch (0.3 mm) except that 4% of the holes are allowed an over-tolerance of 0.015 Inch (0.4mm).

RCB-4.3 TRANSVERSE BAFFLE AND SUPPORT CLEARANCEThe transverse baffle and support plate clearance shall be such that the difference between the shelldesign inside diameter and the outside diameter of the baffle shall not exceed that indicated in TableRCB-4.3. However, where such clearance has no significant effect on shell side heat transfercoefficient or mean temperature difference. these maximum clearances may be increased to twicethe tabulated values. (See Paragraph RCS-4.43.)



TABLE RCB-4.3Standard Cross Baffle and Support Plate Clearances


Nominal Shell ID6-17

18-3940-5455-69

;; : &

Design ID of Shell Minus Baffle OD

The design inside diameter of a pipe shell is defined as the nominal outside diameter of the pipe,minus twtce the nominal wall thickness. The design inside diameter of a plate shell is the specifiedinside diameter.inside diameter.

In any case, the design inside diameter may be taken as the actual measured shell

RCB-4.4 THICKNESS OF BAFFLES AND SUPPORT PLATES

RCB-4.41 TRANSVERSE BAFFLES AND SUPPORT PLATESThe following tabfes show the minimum thickness of transverse baffles and support platesapplying to all materials for various shell diameters and plate spacings.The thickness of the baffle or support plates for U-tube bundles shall be based on theunsupported tube length in the straight section of the bundle. The U-bend length shall not beconstdered in determining the unsupported tube length for required plate thickness.

TABLE R-4.41BAFFLE OR SUPPORT PLATE THICKNESS

Dimensions in Inches (mm)

Plate Thickness

Nominal Shell IDUnsupported tube length between central baffles. End spaces between

tubesheets and baffles are not a consideration.

24 (;;;)rand Over 24 (610) Over 36 (914) Over 46 Over 60to 36 (914)

Inclusivetq;;lilj;?t2t) (1219) to 60

l,‘ZZe

(1524)


MECHANICAL STANDARDS TEMA CLASS R’C B SECTCON 5

TABLE CB-4.41

BAFFLE OR SUPPORT PLATE THICKNESS

Dimensions in Inches (mm)

Nominal Shell ID

6 -145-28 (;;::;::19-38I9 - ,60

i 737-985)991.15241

il - 100 (1549-25401

Plate Thickness

Unsupported tube length between central baffles. End spaces betweentubesheets and baffles are not a consideration.

R-4.42 LONGITUDINAL BAFFLES

Longitudinal baffles shall not be less than l/4” (6.4 mm) nominal metal thickness.

CB-4.42 LONGITUDINAL BAFFLES

Longitudinal carbon steel baffles shall not be less than l/4” (6.4 mm) nominal metalthickness.

Longitudinal alloy baffles shall not be less than l/8” (3.2 mrn)~ nominal metal thickness.

RCB-4.43 SPECIAL PRECAUTIONS

(1) Baffles and support plates subjected to pulsations.

(2) Baffles and support plates engaging finned tubes.

(3) Longitudinal baffles subjected to large differential pressures due to high shell side fluidpressure drop.

(4) Support of tube bundles when larger clearances allowed by RCB-4.3 are used.

RCB-4.5 SPACING OF BAFFLES AND SUPPORT PLATES

RCB-4.51 MINIMUM SPACING

Segmental baffles normally should not be spaced.closer than l/5 of the shell ID or 2 inches(51 mm), whichever is greater. However, special design considerations may dictate a closerspacing.

,,., ,. ,,R C B - 4 . 5 2 M A X I M U M S P A C I N G

Tube support plates shall be so spaced that the unsupported tube span does not exceed thevalue indicated in Table RCB-4.52 for the tube material used.



TABLE RCB-4.52

MAXIMUM UNSUPPORTED STRAIGHT TUBE SPANSDimensions in Inches (mm)

1 Tube Materials and Temoerature Limits O F

Tube OD

g9r$on Steel & High Alloy Steel, 759

Low Alloy Steel, 850 (454)Nickel-Copper, 600 (316)Nickel, 850 (464)Nickel-Chromium-Iron, 1000 (538)

26 f660)

(1) Above the metal temperature limits shown, maximum spans shall be reduced in directproportion to the fourth root of the ratio of elastic modulus at temperature to elasticmodulus at tabulated limit temperature.

(2) In the case of circumferentially finned tubes, the tube OD shall be the diameter at the rootof the fins and the corresponding tabulated or interpolated span shall be reduced in directproportion to the fourth root of the ratio of the weight per unit length of the tube, if strippedof fins to that of the actual finned tube.

(3) The maximum unsuppolted tube spans in Table RCB-4.52 do not consider potential flowinduced vibration problems. Refer to Section 6for vibration criteria.

RCB-4.53 BAFFLE SPACING

Baffles normally shall be spaced uniformly, spanning the effective tube length. When this isnot possible, the baffles nearest the ends of the shell, and or tubesheets, shall be located as

dclose as practical to the shell nozzles. The remaining ba les normally shall be spaceduniformly.

ACB-4.54 U-TUBE REAR SUPPORT

The support plates or baffles adjacent to the bends in U-tube exchangers shall be so locatedthat, for any individual bend, the sum of the bend diameter plus the straight lengths measuredalong both legs from supports to bend tangents does not exceed the maximum unsupportedspan determined from Paragraph RCB-4.52. Where bend diameters prevent compliance,special provisions in addition to the above shall be made for support of the bends.

RCB-4.55 SPECIAL CASES

When pulsating conditions are specified by the purchaser, unsupported spans shall be asshort as pressure drop restrictions permit. If the span under these circumstances approachesthe maximum permitted by Paragraph RCE-4.52, consideration should be given to alternativeflow arrangements which would permit shorter spans under the same pressure droprestrictions.

RCB-4.56TUBE BUNDLE VIBRATION

Shell side flow may produce exdation forces which result in destructive tube vibrations.Existing predictive correlations are inadequate to insure that any given design will be free ofsuch damage. The vulnerability of an exchanger to flow induced vibration depends on theflow rate, tube and baffle materials, unsupported tube spans, tube field layout, shell diameter,and inlet/outlet configuration. Section 6 of these Standards contains information which is


,’


intended to alert the designer to potential vibration problems. In any case, and consistent withParagraph G-5, the manufacturer is not responsible or liable for any direct, indirect, orconsequential damages resulting from vibration.

RCB-4.6 IMPINGEMENT BAFFLES AND EROSION PROTECTION

The following paragraphs provide limitations to prevent or minimize erosion of tube bundlecomponents at the entrance and exit areas. These limitations have no correlation to tube vibrationand the designer should refer to Section 6 for information regarding this phenomenon.

RCB-4.61 SHELL SIDE IMPINGEMENT PROTECTION REQUIREMENTS

An impingement plate, or other means to protect the tube bundle against impinging fluids,shall be provided when entrance line values of p I/’ exceed the following: non-abrasive, singlephase fluids, 1500 (2232); all other liquids, including a liquid at its boiling point, 500 (744). Forall other gases and vapors, including all nominally saturated vapors, and for liquid vapormixtures, impingement protection is required. I/ is the linear velocity of the fluid in feet persecond (meters per second) and p is its density in pounds per cubic foot (kilograms per cubicmeter). A properly designed diffuser may be used to reduce line velocities at shell entrance.

*RCB-4.62 SHELL OR BUNDLE ENTRANCE AND EXIT AREAS

In no case shall the shell or bundle entrance or exit area produce a value of p V2 in excess of4,000 (5953) where V is the linear velocity of the fluid in feet per second (meters per second)and P is its density in pounds per cubic foot (kilograms per cubic meter).

*RCB-4.621 SHELL ENTRANCE OR EXIT AREA WITH IMPINGEMENT PLATE

When an impingement plate is provided, the flow area shall be considered theunrestricted area between the inside diameter of the shell at the nozzle and the face ofthe impingement plate.

*RCB-4.622 SHELL ENTRANCE OR EXIT AREA WITHOUT IMPINGEMENT PLATE

For determining the area available for flow at the entrance or exit of the shell wherethere is no impingement plate, the flow area between the tubes within the projection ofthe nozzle bore and the actual unrestricted radial flow area from under the nozzle ordome measured between the tube bundle and shell inside diameter may beconsidered.

‘RCB-4.623 BUNDLE ENTRANCE OR EXIT AR’EA WITH IMPINGEMENT PLATE

When an impingement plate is provided under a nozzle, the flow area shall be theunrestricted area between the tubes within the compartments between baffles and/ortubesheet.

*RCB-4.624 BUNDLE ENTRANCE OR EXIT AREA WITHOUT IMPINGEMENT PLATE

For determining the area available for flow at the entrance or exit of the tube bundlewhere there is no impingement plate, the flow area between the tubes within thecompartments between baffles and/or tubesheet may be considered.

RCB-4.63 TUBE SIDE

Consideration shall be given to the need for special devices to prevent erosion of the tubeends under the following conditions:

(1) Use of an axial inlet nozzle.(2) Liquid p V a is in excess of 6000 (8928) where V is the linear velocity in feet per second

(meter per second), and p is its density in pounds per cubic foot (kilograms per cubicmeter).

RCB-4.7 TIE RODS AND SPACERS

Tie rods and spacers, or other equivalent means of tying the baffle system together, shall beprovided to retain all transverse baffles and tube support plates securely in position.



R-4.71 NUMBER AND SIZE OF TIE RODS

Table R-4.71 shows suggested tie rod count and diameter for various sizes of heatexchangers. Other combinations of tie rod number and diameter with equivalent metal areaare permissible; however, no fewer than four tie rods, and no diameter less than 3/8”(9.5 mm) shall be used. Any baffte segment requires a minimum of three points of support.

TABLE R-4.71TIE ROD STANDARDS

Dimensions in inches (mm)

Nominal Tie RodShell Diameter Diameter

MinimumNumber of Tie

I Rods

1X-4.71 NUMBER AND SIZE OF TIE RODS

Table CB-4.71 shows suggested tie rod count and diameter for various sbes of heatexchangers. Other combinations of tie rod number and diameter with equivalent metal areaare permissible: however, no fewer than four tie rods, and no diameter less than 3/8”(9.5 mm) shall be used above 15 inch (381) nominal shell diameter. Any baffle segmentrequires a minimum of three points of support.

TABLE CB-4.71

TIE RODDimensions

NominalShell Diameter

6 -15 (152-381)

4NDARDSInches (mm)

RCB-4.8 SEALING DEVICES

In addition to the baffles, sealing devices should be installed when necessary to prevent excessive,fluid by-passing around or through the tube bundle. Sealing devices may be seal strips, tre rods wrthspacers, dummy tubes, or combinations of these.

RCB-4.9 KETTLE TYPE REBOILERSFor kettle ty e reboilers, skid bars and a bundle hold-down may be provided. One method is shownin Figure R CpB-4.9. Other methods which satisfy the intent are acceptable. Bundle hold-downs arenot required for fixed tubesheet kettles.


MECHANICAL STANDARDS TEMA CLASS R C B

FIGURE RCB-4.9

SECTION 5

CROSS-SECTION END VIEW OF TUBE BUNDLE AND SHELL


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C I3

RCB-5 FLOATING END CONSTRUCTION

RCB-5.1 INTERNAL FLOATING HEADS (Types S and T)

R-5.1 1 MINIMUM INSIDE DEPTH OF FLOATING HEAD COVERS

For multipass floating head covers the inside depth shall be such that the minimumcross-over area for flow between successive tube passes is at least equal to 1.3 times the flowarea through the tubes of one pass. For single pass floating head covers the depth at nozzlecenterline shall be a minimum of one-third the inside diameter of the nozzle.

CB-5.11 MINIMUM INSIDE DEPTH OF FLOATING HEAD COVERS

For multipass floating~ head covers the inside depth shall be such that the minimumcross-over area for flow between successive tube passes is at least equal to the flow areathrough the tubes of one pass. For single pass floating head covers the depth at nozzlecenterline shall be a minimum of one-third the inside diameter of the nozzle.

RCB-5.12 POSTWELD HEAT TREATMENT

Fabricated floating head covers shall be postweld heat treated when required by the Code orspecified by the purchaser.

RCB-5.13 INTERNAL BOLTING

The materials of construction for internal bolting for floating heads shall be suitable for themechanical design and similar in corrosion resistance to the materials used for the shellinterior.

RCB-5.14 FLOATING HEAD BACKING DEVICES

The material of construction for split rings or other internal floating head backing devices shallbe equivalent in corrosion resistance to the material used for the shell interior.

RCB-5.141 BACKING DEVICE THICKNESS (TyPE S)

The required thickness of floating head backing devices shall be determined by thefollowing formulas or minimum thickness shown in Figure RCB-5.141, using whicheverthickness is greatest.

BENDING

?= (1J)(N)(Y)(B)(S)

I’* gr,stgf”“* Metric ~= (I,J)(N)(Y) “zx1o3 ,mm

inches [ (B)(S) 1

SHEAR

W W

f =(Jo(z)(s*), inches Metric t=(n)(zj(s,jx)06 ,mm

where

A =

B=

c=

H =

Ring OD, inches (mm) w = Design bolt load (as ref. in Code Appendix 2).lb. (kN)

As shown in Fig. Y = From Code Fig. 2-7.1 using K = A/ 5RCB-5.141, inches (mm)

Bolt circle, inches (mm) z = Tubesheet OD, inches (mm)

(C-B)/Z,inches(mm) L = Greater of 7or 1, inches (mm)


,’


S = Code allowable stress in S DT = S of backing ring, psi (kPa)tension (using shell design S l;i = Sof split key ring, psi (kPa)temperature), psi (kPa) S,, = S of tubesheet, psi (kPa)

S, = 0.8s psi (kPa)

NOTES

1. All references above are to ASME Coda Section VIII, Division 1.2. Caution: For styles “A”, “B” & “D” check thickness in shear of the tubesheet if

S,, <St.,

3. Caution: Style”C” check thickness in shear of the tubesheet if S,, < S,,

See Figure RCB-5.141 for illustration of suggested styles. Other styles are permissible.

FIGURE RCB 5.141

ANGLE=4$ (0.8 PAD) MIN, 75 (1.3 RAD) MAX

SiYLE "A" STYLE "B"

t (MN)t t l/64-(0.4)

STYLE "D"

STYLE "C"


SECTION 5 MECHANICAL STANDARDS TEMA CL(GS R C 8

RCBd.lSTUBE BUNDLE SUPPORTS

When a,removable shell cover is utilized, a partial support plate, or other suitable means, shallbe provided to support the floating head end of the tube bundle. If a plate is used, thethickness shall equal or exceed the support plate thickness specified in Table R-4.41 orCB-4.41 as applicable for unsupported tube lengths over 60 inches (1524 mm),

RCB-5.16 FLOATING HEAD NOZZLES

The floating head nozzle and packing box for a single pass exchanger shall comply with therequirements of Paragraphs RCB-5.21, RCB-5.22 and RCB-5.23.

RCB-5.17 PASS PARTITION PLATES

The nominal thickness of floating head pass partitions shall be identical to those shown inRCB-9.13 for channels and bonnets.

RCB-5.2 OUTSIDE PACKED FLOATING HEADS (Type P)

RCB-5.21 PACKED FLOATING HEADS

The cylindrical surface of packed floating head tubesheets and skirts, where in contact withpacking (including allowance for expansion), shall be given a fine machine finish equivalent to63 microinches.

RCB-5.22 PACKING BOXES

A machine finish shall be used on the shell or packing box where the floating tubesheet ornozzle passes through. If packing of braided material is used, a minimum of three rings ofpacking shall be used for 150 PSI (1034 kPa) maximum design pressure and a minimum offour rings shall be used for 300 PSI (2066 kPa) maximum design pressure. For pressures lessthan 150 PSI (1034 kPa), temperatures below 3OO’F (149” C), and non-hazardous service,fewer rings of packing may be used. Figure RCB-5.22 and Table RCB-5.22 show typicaldetails and dimensions of packing boxes.

4 0 Standards Of The Tubular Exchanger Manufacturers Association


FIGURE RCB-5.22

c E FI J/ \

Design Based On Square-I L Pocking of Other SuitableBraided Packing Materials. Dimensions, and

Shape May Be Used

TABLE RCB-5.22

TYPICAL DIMENSIONS FOR PACKED FLOATING HEADS

150 PSl(1034 kPa) AND 300 PSt(2068 kPa) WITH 600 ‘F (316 “C) MAX. TEMP,

Dimensions in Inches

B C D E

(MIN)1

;11

i-i/8i-1/8l-l/8I-114?-1 j4

Dimensions in Millimeters

SIZE

152-203229-330356-432457-533

;;;:::;762-838864-l 092

1118-12951321-1524

A

9.539.539.539.539.53

12.7012.7012.7015.8815.88

B

11.1111.1111.1111.1111.1114.2914.2914.2917.4617.46

C

31.7531.7531.7531.7531.7544.4544.4544.4553.9853.98 i

D I B(NO.

rsSIZE

Ml6Ml6Ml6Ml6Ml6Ml6Ml6Ml6Ml6Ml6

Note: Nominal size of packing is same as dimension ‘A”



RCB-5.23 PACKING MATERIAL

Purchaser shall specify packing material which is compatible with the shell side processconditions.

RCB-5.24 FLOATING TUBESHEET SKIRT

The floating tubesheet skrrt normally shall extend outward. When the skirt must extendinward, a suitable method shall be used to prevent stagnant areas between the shell sidenozzle and the tubesheet.


The nominal thickness of floating head pass partitions shall be identical to those shown inParagraph RCB-9.13 for channels and bonnets.

RCB-5.3 EXTERNALLY SEALED FLOATING TUBESHEET (Type W)

RB-5.31 LANTERN RING

The externally sealed Roating‘tubesheet using square braided packing materials shall be usedonly for water, steam, air, lubricating oil, or similar services. Design temperature shall notexceed 375 0 F (191 o C) Design pressure shall be limited according to Table RB-5.31.

TABLE RB-5.31

MAXIMUM DESIGN PRESSURE FOR EXTERNALLY SEALEDFLOATING TUBESHEETS

Nominal Shell Inside DiameterInches (mm)

6-24 (152610)25 - 42 (635-106743 - 60 (1092-l 52461 100 H644-25Ar-r

Maximum Design PressurePSI (kPa)

300 (2066)150

75I 1034)517)

Fin 13051

42

C-5.31 LANTERN RING

The externally sealed floating tubesheet shall be used only for water, steam, air, lubricating oil,or similar services. Design temperature, pressure and shell diameter shall be limited by theservice, joint configuration, packing material and number of packing rings, to a maximumdesign pressure of 600 psi (4137 kPa).

RCB-5.32 LEAKAGE PRECAUTIONS

The design shall incorporate provisions in the lantern ring so that any leakage past thepacking will leak to atmosphere. When endless packing rings are used, one ring of packingshall be used on each side of the lantern ring. For braided packing materials with a seam, aminimum of two rings of packing shall be used on each side of the lantern ring, with theseams staggered during assembly.

RCB-5.33 PACKING MATERIAL

Purchaser shall specify packing material which is compatible with the process conditions.

RCB-5.34 SPECIAL DESIGNS

Special designs incorporating other sealing devices may be used for the applications inParagraph RB5.31 and C-5.31 or other special service requirements. Provisions for leakdetection shall be considered.


~,~

F,0

r”lCs9e; MECHANICAL STANDARDS TEMA CLASS R C B SECTION 50Q RCB-6 GASKETS

c RCB-6.1 TYPE OF GASKETS

Q ,Gaskets shall be selected which have a continuous periphery with no radial leak paths. This shall not

cexclude gaskets made continuous by welding or other methods which produce a homogeneousbond.

0 R-6.2 GASKET MATERIALSg: Metal jacketed or solid metal gaskets shall be used for internal floating head joints, all joints for

8pressures of 300 psi (2068 kPa) and over, and for all joints in contact with hydrocarbons. Other

Q” ~’ gasket materials may be specified by agreement between purchaser and manufacturer to meet

special service conditions and flange design. When two gasketed joints are cornR

ressedsame bolting, provisions shall be made so that both gaskets seal, but neither gas

by the

c;et is crushed at the

required bolt load.

0 CB-6.2 GASKET MATERIALS

0 For design pressures of 300 psi (2068 kPa) and lower, composition gaskets may be used for external

0joints, unless temperature or corrosive nature of contained fluid indicates otherwise. Metal jacketed,filled or solid metal gaskets shall be used for all joints for design pressures greater than 300 psi (2068

fi kPa) and for internal floating head joints. Other gasket materials may be specified by agreement

Qbetween purchaser and manufacturer to meet special service conditions and flange design. Whentwo gasketed joints are compressed by the same bolting, provisions shall be made so that both

0gaskets seat, but neither gasket is crushed at the required bolt load.

QACE-6.3 PERIPHERAL GASKETS

aRC-6.31

0The minimum width of peripheral ring gaskets for external joints shall be 3/S (9.5 mm) forshell sizes through 23 inches (584 mm) nominal diameter and l/2” (12.7 mm) for all larger

Qshell sizes.

aB-6.31

The minimum width of peripheral ring askets for external joints shall be 3/V (9.5 mm) for0 shell sizes through 23 inches (584 mmB nominal drameter and l/2” (12.7 mm) for all larger

0shell sizes. Full face gaskets shall be used for all cast Iron flanges.

RCB-6.32rQ The minimum width of peripheral ring gaskets for internal joints shall be l/4” (6.4 mm) for all

0 shell sizes.

0 R-6.33

0 Peripheral gasket contact surfaces shall have a flatness tolerance of * l/32” (0.8 mm)

0maximum deviation from any reference plane. This maximum deviation shall not occur in lessthan a 20 o (0.3 Rad) arc.

CBS.33Flatness of peripheral gasket contact surfaces shall be sufficient to meet the requirements ofParagraph RCE-1.3.

RCB-6.4 PASS PARTITION GASKETS

The width of gasket web for pass partitions of channels, bonnets, and floating heads shall be not fessthan l/4” (6.4 mm) for shell sizes through 23 inches (584 mm) nominal diameter and not IeSS than3/8” (9.5 mm) for all larger shell sizes.

R-6.5 GASKET JOINT DETAILS

Gasketed joints shall be of a confined type.



CB6.5 GASKET JOINT DETAILS

Gasket joints shall be of a confined or unconfined type.flGURE RCS-6.5

. -_e__

Confined Gasket Unconfined Gasket

For dimensions and tolerances, see Figure F-3.

Confined Gasket

SPIRAL WOUND GASKET WITH OUTER METAL RING

RCS-6.6 SPARE GASKETS

Unless specifically stated otherwise, spare gaskets include only main body flange gaskets.


”;

A

A


RCB-7 TUBESHEETS

RCB-7.1 TUBESHEETTHICKNESS

RCB-7.11 APPLICATION INSTRUCTIONS AND LIMITATIONS

Subject to the requirements of the Code, the formulas and design criteria contained inParagraphs RCB-7.1 through RCB-7.25 are applicable, with limitations noted, when thefollowing normal design conditions are met:

(1) S&$ pressure are within the scope of the TEMA Mechanical Standards, Paragraph

(2) Tube-to-tubesheet joints are expanded, welded or otherwise constructed such as toeffectively contribute to the support of the tubesheets (except U-tube tubesheets)

(3) Tubes are uniformly distributed (no large untubed areas)

Abnormal conditions of support or loading are considered Special Cases, and are defined inParagraph RCB-7.3 which is referenced, when pertinent, in subsequent paragraphs.

RCB-7.12 EFFECTIVE TUSESHEETTHICKNESS

Except as qualified by Paragraphs RCB-7.121 and 7.122, the effective tubesheet thicknessshall be the thickness measured at the bottom of the tube side pass partition groove and/orshell side longitudinal baffle groove minus corrosion allowance in excess of the groovedepths.

RCB-7.121 APPLIED TUBESHEET FACINGS

The thickness of applied facing material shall not be included in the minimum oreffective tubesheet thickness.

RCB-7.122 INTEGRALLY CLAD TUBESHEETS.,~

The thickness of cladding material in integrally clad plates and cladding deposited bywelding may be included in the effective tubesheet thickness as allowed by the Code.

RCB-7.13 REQUIRED EFFECTIVE TUBESHEETTHICKNESS

The required effective tubesheet thickness for any type of heat exchanger shall be determinedfrom the following paragraphs, for both tube side and shell side conditions, corroded oruncorroded, using whichever thickness is greatest. Both tubesheets of fixed tubesheetexchangers shall have the same thickness, unless the provisions of Paragraph RCB-7.166 aresatisfied.

R-7.13i MINIMUM TUBESHEET THICKNESS WITH EXPANDED TUBE JOINTS

In no case shall the total thickness minus corrosion allowance, in the areas into whichtubes are to be expanded, of any’tubesheet be less than the outside diameter of tubes.In no case shall the total tubesheet thickness, including corrosion allowance, be lessthan 3/4” (19.1 mm).

C-7.i31 MINIMUM TUBESHEETTHICKNESS WITH EXPANDED TUBE JOINTS

In no case shall the total thickness minus corrosion allowance, in the areas into which,tubes are to be expanded, of any tubesheet be less than three-fourths of the tubeoutside diameter for tubes of 1” (25.4 mm) 00 and smaller, 7/8” (22.2 mm) for 1-l /4”(31.8 mm) OD, 1” (25.4 mm) for l-1 /2” (38.1 mm) OD, or l-1 /4” (31.8 mm) for 2” (50.8

~mm) OD.

B-7.131 MINIMUM TUBESHEETTHICKNESS WITH EXPANDED TUBE JOINTS

In no case shall the total thickness minus corrosion allowance, in the areas into whichtubas are to be expanded, of any tubesheet be less than three-fourths of the tubeoutside diameter for tubes of 1” (25.4 mm) OD and smaller, 7/8” (22.2 mm) for l-1 /4”

” 6:31 8 mm) OD, 1” (25.4) for l-1 /2” (38.1 mm) OD, or 1-l /4” (31.8 mm) for 2” (50.8 mm)

D In no case shall the total tubesheet thickness, including corrosion allowance, beless than 3/4” (19.1 mm).

Standards Of The Tubular Exchanger Manufacturers Association 4 5

SECTION 5

46


RCB-7.132 TUBESHEET FORMULA- BENDING

whereT = Effective tubesheet thickness, inches (mm).S = Code allowable stress in tension, psi (kPa), for tubesheet material at design

metal temperatures. (See Paragraph RCB-1.42).

P =

G =

For outside packed floating head exchangers (Type P), Pshall be as defined inParagraph RCB-7.141, psi (kPa).For packed floating end exchangers with lantern ring (Type W), for the floatingtubesheet, Pshall be asdefined in Paragraph RCB-7.142, psi (kPa).For fixed tubesheet exchangers, Pshall be as defined in ParagraphRCB-7.163, RCB-7.164 or RCB-7.166, psi (kPa).For other type exchangers, Pshall be the design pressure, shell side or tubeside, corrected for vacuum when present on the oppressure when specified by the purchaser, psi (kPaP

osite side, or differential

For U-tube tubesheets (Type U), where the tubesheet is extended as a flange forbolting to heads or shells with ring type gaskets, P = P 5 + P b or P t + P ,,depending upon the side under consideration.

where

Pb=- 6 . 2 Mf

F2 G3and M *is defined in Paragraph RCB-7.1342, psi (kPa).

For floating tubesheets (Type T), where the tubesheet is extended for bolting toheads with ring type gaskets, the effect of the moment acting upon the extensionis defined in Paragraph RCB-7.162 in terms of equivalent tube side and shell sidebolting pressures except G shall be the gasket G of the floating tubesheet. P psi(kPa) is given by the greatest absolute value of the followlng:

P=P,+P,,

orP=P,-PBSorP- P,OrP=P,

G shall be either in the corroded or uncorroded condition, dependent uponwhich condition is under consideration.For fixed tubesheet exchangers, G shall be the shell inside diameter.For kettle type exchangers, G shall be the port inside diameter.For any floating tubesheet (except divided), Gshall be the Gused for thestationary tubesheet using the Pas defined for other type exchangers.TypeT tubesheets shall also be checked using the pressure P defined abovewith bolting and using the actual gasket G of the floating tubesheetFor a divided~floating tubesheet, G shall be 1.41(d) where d is the length of theshortest span measured over centerlines of gaskets.For other type exchangers, G shall be the diameter, inches (mm), over which thepressure under consideration is acting. (e.g.: Pressure acting on the gasketedside of a tubesheet. G = the diameter at the location of the gasket load reactionas defined in the Code. Pressure acting on an integral side of a tubesheet, G =the inside diameter of the integral pressure part.)

Standards Of The Tubular Exchanger ManufWurers Association


F =

0.785

SECTION 5

for square or rotated square tube patterns

1 -!“s,‘R: 2 for triangular or rotated triangular tube patterns

For integrally finned tubes, the CD of the tube in the tubesheet shall be used.

\or unsupported tubesheets (e.g.: U-tube tubesheets) gasketed bothides, F = 1.25.

:or supposed tubesheets (e.ubesheets) gasketed both SI3

.: fixed tubesheets and Roating typees, F = 1 .O.

‘or unsuprr both SI8

orted tubesheets (e.g.: U-tube tubesheets) integral with eitheres, F shall be the value determined bv the curve U in

:igure RCB-7.132.

letermined by the curve H in Figure RCB-7.i32

FIGURE RCB-7.1321 . 3 01 . 2 61 . 2 01 . 1 51 . 1 01 . 0 5

, 1 . 0 00 . 9 50 . 9 00 . 6 60 . 6 00 . 7 5

0 . 0 0 0 . 0 1 0 . 0 2 0 . 0 3 0 . 0 4 0 . 0 5 0 . 0 6 0 . 0 7 0 . 0 6 0 . 0 9 0 . 1 0

Wall Thickness/ID Ratio For Integral Tubesheets

4OTE: If the tubesheet is integral with both the tube side and shell side,Wall Thickness and ID are to be based on the side yieldingthe smaller value of F.

See Table RCB-7.132 for illustration of the application of the above equations.



TABLE RCB - 7.132

Design pressure, psi (kPa),

Nate: F Max = I.0

inside diameter

Table RCB - 7.132 continued next page



TABLE I?(

F

See Figure RCE7.132

Jy!~)lNote: F Max = 1.25

F Min = 1.00

1.0

1.0

1.0

1.0

1.0

7.132 (Continued)

nket Gell side

Channel ID

e note 1

lell ID or port Channel IDiide diameter‘kettle typel-changers

P

Design pressure, psi (kPa),shell side, or tube side, perParaaraoh X8-7.132con&d for vacuum whenpresent on opposite side, ordifferential pressure whenspecified by customer.

Same C as used for stationarytubesheet

Design pressure, psi (kPa),shell side, or tube side, perParaaraoh RCS-7.132corre&d for YBCUU~ whenpresent on opposite side, ordifferential pressure whenspecified by customer.

Same C as used for stationary See Paragraph RCB-7.132Ibesheet Also check using gasket

G of the floating tubesheetsee note 1

_ 1.41(d) Design pressure, psi (kPa),- Shortest span measured over shell side, ortube side, per

center lines of gaskets. Paragraph RCE7.132corrected for vacuum whenpresent on opposite side, ordifferential pressure whenspecified by customer.

Same Gas used for stationarytubesheet

Design pressure, psi (kPa),tube side per paragraphRCS-7.132 corrected forvacuum when present on theshell side.

Gasket G = the diameter at the location of the gasket load reaction as defined in the Code.


SECTION5 MECHANICAL STANDARDS TEMA CLASS R C B

i

RCB-7.133 TUBESHEET FORMULA - SHEAR

where

T = Effective tubesheat thickness, inches (mm)

DL = y = Equivalent diameter of the tube center limit perimeter, inches(mm)

c= Perimeter of the tube layout measured stepwise in increments of onetube pitch from center-to-center of the outermost tubes, inches (mm).Figure RCB-7.133 shows the application to typical triangular and souaretube patterns

FIGURE RCB-7.133

,,. ., ,,.,

A =

d,=

’ C” (perimeter) is the length of the heavy line

Total area enclosed by perimeter C, square inches (mm 2,

Pitch =

Outside tube diameter, inches (mm), for integrally finned tubes, the OD ofthe tube in the tubesheet shall be used.Tube center-to-center spacing, inches (mm)

For outside packed floating head exchangers (Type P), P shall be asdefined in Paragraph RCB-7.141. psi &Pa).

P = For fixed tubesheet exchangers, Pshall be as defined in ParagraphsRCB-7.163, RCB-7.164 or RCB-7.165, psi (kPa).

For other type exchangers, Pshall be the design pressure, psi (kPa),shell side or tube side, corrected for vacuum when present on theopposite side, or differential pressure when specified by the purchaser.

s= Code allowable stress in tension, psi (kPa), for tubesheet material atdesign metal temperature. (See Paragraph RCB-1.42.)

NOTE: Shear will not control when

See Table RCB-7.133 for illustration of the application of the above equations.


_--,

A

r_

r?

7

II-,

,_


TABLE RCB-7.133

TUBESHEET THICKNESS FOR SHEARNote: Must be calculated for shell side or

tube side pressure, whichever isoontmlling.

do = Outside tube diameter, Pitch = Tube spacing,inches (mm). For integrally center-to-center, inchesfinned tubes, the OD of thetube in the tubesheet shall be

(mm).

I P

Design pressure, psi (kPa), shell side or tubeside, corrected for vacuum when present onopposite side, or differential pressure whenspecified by customer

?-‘) Design pressure, psi (kPa), shell side or tubeside, corrected for vacuum when present onopposite side, or differential pressure whenspecified by customer

Design pressure, psi (kPa), shell side or tubeside, corrected for vacuum when present onopposite side, or differential pressure whenspecified by customer, or for fixed tubesheett pe units, as defined rn paragraphs RCB-7.163txru WE-7.165

TABLE RCB-7.133 Continued fleXI page

=Code allowable stress intension, psi (kPa). Fortubesheet material at designmetal temperature.(Seeparagraph RCS-1.42.)

D,

Perimeter of tube layoutmeasured stepwise inincrements 0‘ onetube-to-tube pitchoenter-to-center of theoutermost tubes, ininches (mm). See FigureRCS-7.133

total area enclosed by Cin sSee?=

“are inches (mm 2).igure RCS-7.133



52

TABLE RCB-7.133 Continued

P


Design pressure, psi (kPa). Shell side or tubeside, corrected for vacuum when present onopposite side, or differential pressure whenspecified by customer


Design pressure, psi (kPa), tube side, correctedfor vacuum when present on the shell side

Defined in Paragraph RCB-7.1412

D,

= Perimeter of tube layoutmeasured stepwise inincrements of onetube-to-tube pitchcenter-to-center of theoutermost tubes, ininches (mm). See FigureRCS-7.133

= total area endosed by Cin square inches (mm2).See Figure RCS-7.133



IKE-7.134 TUBESHEET FORMULA - TUBESHEET FLANGED EXTENSION

This paragraph is applicable only when bolt loads are transmitted, at the bolt circle, tothe extended portion of a tubesheet. The peripheral portion extended to form a flangefor bolting to heads or shells with ring type gaskets may differ in thickness from thatportion inside the shell calculated in Paragraph RCB-7.132. The minimum thickness ofthe extended portion may be calculated from the following paragraphs.

RCB-7.1341 FIXED TUBESHEET OR FLOATING TUBESHEET EXCHANGERS

7-,=0.98 rA4 (r*- 1+3.71r2 2n r,l””

.--L s (A-G)(1+1.86 i-2) J

where

T,=

A=

r=

Minimum thickness of the extended portion, inches (mm)

Outside diameter of the tubesheet, inches (mm)

AG

M = the larger of M I or M 2 as defined in Paragraph RCB-7.162

Note: The moments may differ from the moments acting on the attached flange

.S and Gare defined in Paragraph RCB-7.132

RCB-7.1342 U-TUBE TUBESHEET EXCHANGERS

T,= 1 . 3 8M*+M+0.39 P G2 w "'

(A-G) S 1where

7 r = Minimum thickness of the extended portion, inches (mm)

M'=~u#PG~(;)~-MG-O.~~WPG~

G+!$($

T = Effective tubesheet thickness calculated fromParagraph RCB-7.132, inches (mm)

(A-G)u)= 2

M = the larger of M I or M, as dafined in Paragraph RCB-7.162

Note: The moments may differ from the moments acting on the attached flange.

I:, G and n are defined in Paragraph RCB-7.132

P = P s or P r or maximum differential pressure, as applicable.

Note: See Paragraph RCB-7.13421 for procedure.


S E C T I O N 5

_ 54

,_


FINE-7.13421 ITERATIVE CALCULATION M E T H O D S

Method 1

(1) Calculate M * assuming T I = T.

(2) Calculate P, then P from Paragraph RCB-7.132.

(3) Calculate Tfrom Paragraph RCB-7.132.

(4) Calculate T r from Paragraph RCB-7.1342.

(5) Compare T and T ?; if T is greater than T I, calculation is terminated. Use T ,calculated. Do not proceed to Step (6).

(6) If T r is greater than T, or if it is desired to reduce T r below T, select a new ratio ofT r 1 T that is less than 1 and repeat Steps (I) through (5). (Note: T, IT ratio iscalculated using actual corroded thickness of the part).

Method 2 - (ALTERNATIVE METHOD)

(l)SetM*=-M

(2) Calculate P ,, then P from Paragraph RCB-7.132.

(3) Calculate 7’from Paragraph RCB-7.132.

(4) Calculate T r from Paragraph RCB-7.1342.

(5) Recalculate M * = - Musing values of T and T , obtained in Steps (3) and (4) andas defined in Paragraph RCB-7.1342. (Note 7 ~/T must be 2 1).

(6) If I M* I obtained in Step (5) is less than I A4 lfrom Step (l), calculation isterminated. Use T, calculated in Step (4). Do not proceed to Step (7).

(7) If I A4 * 1 obtained from Step (5) is greater than I M 1 from Step (l), repeat Step (2)using M * calculated in Step (5). Then repeat Steps (3) through (5).

(8) If last calculated I M * I is less than the previous I A4 * I used to calculate P D,calculation is terminated. Use last calculated value of T,.

(9) If last calculated I M * I is greater than the previous I M * I used to calculate P D ,repeat Step (2) using last calculated M *. Then repeat Steps (3) through (5).Continue this process until Step (8) is satisfied.



RCB-7.14 PACKED FLOATING TUBESHEET TYPE EXCHANGERS EFFECTIVE PRESSURE

RCB-7.141 OUTSIDE PACKED FLOATING HEAD (TYPE P)The thickness of tubesheets in exchangers whose ffoating heads are packed at theoutside diameter of the tubesheet or a cylindrical extension thereof shall be calculatedlike stationary tubesheets using the formulas for Pas defined below.

RCB-7.1411 EFFECTIVE DESIGN PRESSURE - BENDINGThe effective design pressure to be used with the formula shown in ParagraphRCE-7.132 is given by:

p=p,+p 1.25(D2-Dc *)(D-0,)P

DF2G2 I,,,

whereP,=

P,=

D =

Design pressure, psi (kPa), tube side(For vacuum design, PI is negative.)

Design pressure, psi (kPa), shell side(For vacuum design, PI is negative.)

Outside diameter of the floating tubesheet, inches (mm)

D,= Equivalent diameter of the tube center limit perimeter, inches(mm), using Aas defined in Paragraph RCB-7.133

F and Gare as defined in Paragraph RCB-7.132

RCB-7.1412 EFFECTIVE DESIGN PRESSURE-SHEARThe effective design pressure to be used with the formula shown in ParagraphRCB-7.133 is given by:

using terms as defined in Paragraph RCB-7.1411.

RCB-7.142 PACKED FLOATING TUBESHEET WITH LANTERN RING (TYPE W)The thickness of floating tubesheets in exchangers whose floating tubesheets arepacked at the outside diameter with return bonnet or channel bolted to the shellflange, shall be calculated as for gasketed stationary tubesheet exchangers, using Pdefined as the tube side design pressure, psi (kPa), corrected for vacuum whenpresent on the shell side. It is incorrect to utilize the shell side pressure.

” RCB-7.15 DOUBLE TUBESHEETSDouble tubesheets may be used where the operating conditions indicate their desirability.The diversity of construction types makes it impractical to specify design rules for all cases.Paragraphs RCB-7.154, RCB-7.155 and RCB-7.156 provide the design rules for determiningthe thickness of double tubesheets for some of the most commonly used construction types.RCB-7.151 MINIMUM THICKNESS

Neither component of a double tubesheet shall have a thickness less than thatrequired by Paragraph RCB-7.131.



RCE7.152VENTS AND DRAINSDouble tubesheets of the edge welded type shall be provided with vent and drainconnections at the high and low points of the enclosed space.


When double tubesheets are used, special attention shall be given to the ability of thetubes to withstand, without damage, the mechanical and thermal loads imposed onthem by the construction.

RCB-7.154 INTEGRAL DOUBLE TUBESHEETS

The tubesheets are connected in a manner which distributes axial load and radialthermal expansion loads between tubesheets by means of an interconnecting elementcapable of preventing individual radial growth of tubesheets. It is assumed that theelement is rigid enough to mutually transfer all thermal and mechanical radial loadsbetween the tubesheets. Additionally, it is understood that the tubes are rigid enoughto mutually transfer all mechanical and thermal axial loads between the tubesheets.

__=_-_-__-----_____

_t2 9 Tt- -

FIGURE RCB-7.154

RCS 7.1541 TUBESHEET THICKNESS

Calculate the total combined tubesheet thickness (7) per Paragraph RCB-7.13.

where

T = Greater of the thickness, inches (mm), resulting fromParagraphs RCB-7.132 or RCB-7.133 using the followingvariable definitions:

G =

S=

F =

Per Paragraph RCB-7.13, inches (mm), using worst case valuesof shell side or tube side tubesheets at their respective designtemperature.

Lower of the Code allowable stress, psi (kPa), for eithercomponent tubesheet at its respective design temperature.

Per Paragraph RCB-7.13, using worst case values of shell sideor tube side tubesheets at their respective design temperature.

All other variables are per Paragraph RCB-7.13

Establish the thickness of each individual tubesheet so that tZ + tL 2 Tand theminimum individual tubesheet thicknesses ( t , and t .) shall be the greater ofParagraphs RCB-7.13 or RCB.7.134. as applicable.

where

t , = Thickness of tube sidetubesheet, inches (mm).

t, = Thickness of shell side tubesheet, inches (mm).



RCB-7.1542 INTERCONNECTING ELEMENT DESIGN -SHEAR

The radial shear stress (-c), psi (kPa), at attachment due to differential thermalexpansion of tubesheets shall not exceed 80% of the lower Code allowablestress (.S) of either of the tubesheet materials or the interconnecting element attheir respective design temperature. The shear is defined as:

.+O.HS

(Metric) Z=Fx 106<0.8S

I, = Thickness of interconnecting element, inches (mm).

where

where

F, =

E,=

E,=

a, =

a2 =

AT, =

AT, =

Force per unit measure due to differential radial expansion, Ibf/in(kN/mm).Modulus of Elasticity of tubesheet 1 at mean metal temperature,psi (kPa).Modulus of Elasticity of tubesheet 2 at mean metal temperature,psi (kPa).

Coefficient of thermal expansion for tubesheet 1 at mean metaltemperature, inches/inch/ a F (mm/mm/ a C).

Coefficient of thermal expansion for tubesheet 2 at mean metaltemperature, inches/inch/O F (mm/mm/ OC).

Difference in temperature from ambient conditions to meanmetal temperature for tubesheet 1, o F (” C).

Difference in temperature from ambient conditions to meanmetal temperature for tubesheet 2, o F e C).

RCB-7.1543 INTERCONNECTING ELEMENT DESIGN - BENDING AND TENSILE

The combined stresses from bending due to differential thermal expansion oftubesheets and axial tension due to thermal expansion of tubes shall notexceed 1.5 times the Code allowable stress (S) of the interconnecting element.The combined total stress of interconnecting element (0 d, psi (kPa), is givenby:

0,=0,+0,,~1.5.s

Stancizirds Of The Tubular &changer Manufacturers Association 57

S E C T I O N 5 MECHANICAL STANDARDS TEMA CLASS R C B

5 8

The stress due to axial thermal expansion of tubes (0 TE) , psi (kPa), is definedas:

urE=

(Metric) 0 r6 =

FTEn,F,,-AE

x lo6

(Metric) F TE =(a,ATT-u,AT,)(E,A,)(E,AB)X *o.6

(E*AT)+(EsAE)

The stress due to bending caused by differential thermal expansion oftubesheets CI B, psi (kPa), is defined as:

~MB(Metric) flg=~x lo6

The bending moment is defined as:

where

MB=

g=

(YT =

(xE =

AT’r =

Bending moment per unit measure acting on interconnecting element,inch-pounds per inch (mm-kN/mm).Spacing between tubesheets, inches (mm). The spacing betweentubesheets for an integral double tubesheet is left to the discretion ofthe manufacturer. For other types of double tubesheets, the minimumspacing is determined in accordance with Paragraphs RCB-7.1552 orRCB-7.1562, as applicable.Coefficient of thermal expansion of tubes at mean metal temperature,inches/inch/ 0 F (mm/mm/ ’ C).

Coefficient of thermal expansion of interconnecting element at meanmetal temperature, inches/inch/ “F (mm/mm/ 0 C).

Difference in temperature from ambient conditions to mean metaltemperature for tubes, o F e C).

ATs = Difference in temperature from ambient conditions to mean metaltemperature for interconnecting element, o F e C).

E ~ = Modulus of Elasticity of tubes at mean metal temperature, psi (kPa).

E E = Modtilus of Elasticity of interconnecting element at mean metaltemperature, psl (kPa).

,J r = Total cross sectional area of tubes between tubesheets, square inches(mm2).

A E = Total cross sectional area of interconnecting element, square inches(mm2).

F TB = Resultant force due to the difference in thermal expansion betweentubes and element, Ibf (kN).


RCB-7.1544 TUBE STRESS CONSIDERATION -AXIAL STRESS

The axial stresses in the tubes due to thermal expansion and pressure load” shall not exceed the Code allowable stress (S) of the tubes at design

temperature.

The total combined stress of the tubes (a r), psi (kPa), is given by:

a,=u,+a,,~S

The axial stress due to pressure (up), psi (kPa), is defined as:

d _Pn(G*-NC!:)P

4~4,

where

P= Greater of shell side or tube side design pressure, psi (kPa).

G = Per Paragraph RCB-7.13, inches (mm).

N- Number of tubes.

do = Tube OD between tubesheets, inches (mm).

The stress due to axial thermal expansion of tubes (0 &, psi (kPa). is definedby:

,,(Metric) cTT = xx lo6

RCB-7.155 CONNECTED DOUBLE TUBESHEETS

The tubesheets are connected in a manner which distributes axial load betweentubesheets by means of an interconnecting cylinder. The effect of the differential radialgrowth between tubesheets is a major factor rn tube stresses and spacing betweentubesheets. It is assumed the interconnecting cylinder and tubes are rigid enough tomutually transfer all mechanical and thermal axial loads between the tubesheets.

FIGURE RCB-7.155

RCB-7.1551 TUBESHEET THICKNESS

Calculate the total combined tubesheet thickness (7) per Paragraph RCB-7.13.


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C 6

where

T= Greater of the thickness, inches (mm), resulting from ParagraphsRCB-7.132 or RCB-7.133 using variables as defined in ParagraphRCB-7.1541.

Establish the thickness of each individual tubesheet so that t, + t , 2 T and theminimum individual tubesheet thickness (t , and t 2) shall be the greater ofParagraph RCB-7.13 or RCB-7.134. when applicable.

where

t , = Thickness of tube side tubesheet, inches (mm).

t, = Thickness of shell side tubesheet, inches (mm),

RCB-7.1552 MINIMUM SPACING BETWEEN TUBESHEETS

The minimum spacing (g), inches (mm), between tubesheets required to avoidoverstress of tubes resulting from differential thermal growth of individualtubesheets is given by:

J d,ArE,!J= 0.27YT

where

d, =

Y,=

Al-=

A4

?,

A

h

/7

,,_,r,

,T-,

Tube OD between tubesheets, inches (mm).?

,.‘7;;‘;)strength of the tube material at maximum metal temperature, psi

,,,---

Differential radial expansion between adjacent tubesheets, inches (mm).(Measured from center of tubesheet to D rL).

AJ-=l

/7.

,-

?

_. *where

D,, = Outer tube limit, inches (mm)

RCB-7.1553 INTERCONNECTING ELEMENT DESlGN -AXIAL STRESS

The interconnecting element axial stress (0 rE), psi (kPa), due to the thermalexpansion of the tubes shall not exceed the Code allowable stress (.S) of theinterconnecting element at design temperature. The axial stress is defined as:

FTEOr&=-

AE

(Metric) drE = 2x lo6


!3andards Of The Tubular Exchanger Manufacturers Association

I.


RCB-7.1554 TUBE STRESS CONSIDERATIONS -AXIAL STRESS

SECTION 5

The axial stresses in the tubes due to thermal expansion and pressure loadshall not exceed the Code allowable stress (5) of the tubes at designtemperature.

The total combined stress of tubes (or), psi (kPa), is given by:

b,=U,+br,<S

The axial stress due to pressure (d p), psi (kPa), is defined as:

dP

= Pn(G'-Nd.*)

4Ar

where

P = Greater of shell side or tube side design pressure, psi (kPa)

G = Per Paragraph RCB-7.13, inches (mm).

N = Number of tubes.~;, I ,.

d, = Tube OD between tubesheets. inches (mm).

The stress due to axial’thermal expansion of tubes (d TT), psi (kPa), isdetermined by:

FTE(Metric) crr=flrX lo6

RCB-7.156 SEPARATE DOUBLE TUBESHEETS

The tubesheets are connected only by the interconnecting tubes. The effect ofdifferential radial growth between tubesheets is a major factor in tube stresses andspacing between tubesheets. It is assumed that no loads are transferred between thetubesheets.

w= -- -_-- = -- --(2 9 rrFIGURE RCB-7.156

,,

61


RCB-7.1561 TUBESHEET THICKNESS

Calculate tube side tubesheet thickness per Paragraph RCB-7.13. Useall variables as defined per TEMA, neglecting all considerations of shellside design conditions.

Calculate shell side tubesheet thickness per Paragraph RCB-7.13. Useall variables as defined per TEMA, neglecting all considerations of tubeside design conditions.

RCB-7.1562 MINIMUM SPACING BETWEEN TUBESHEETS

The minimum spacing (g), inches (mm), between tubesheets required toavoid overstress of tubes resulting from differential thermal growth ofindividual tubesheets is given by:

g=d&-E,

rO.27Yr

RCB-7.16 FIXED TUBESHEET EFFECTIVE PRESSURE

This paragraph shall apply to exchangers having tubesheets fifed to both ends of the shell,with or without a shell expansion joint except as required or permitted by Paragraph RCB-7.3.Both tubesheets of fixed tubesheet exchangers shall have the same thickness, unlessthe provisions of Paragraph RCB-7.166 are satisfied.

For fixed tubesheet exchangers, the mutually interdependent loads exerted on thetubesheets, tubes, and shell are defined in terms of equivalent and effective design pressuresin Paraaraohs RCB-7.161 throuah RCB-7.165for use in Paraoraohs RCB-7.132 andRCB-7.733’. These pressures shall also be used (with J = 1) in Paragraphs RCB-7.22,RCB-7.23 and RCB-7.25 to assess the need for an expansion joint. The designer shallconsider the most adverse operating conditions specified by the purchaser. (See ParagraphE-3.2.)

RCB-7.161 EQUIVALENT DIFFERENTIAL EXPANSION PRESSURE

The pressure due to differential thermal expansion, psi (kPa), is given by:

4 J F, r* (Y)

P”=(D,-3t,) (l+JKF,)

Note: Algebraic sign must be retained for use in Paragraphs RCB-7.163 throughRCB-7.166, RCB-7.22 and RCB-7.23.

where

J = 1 .O for shells without expansion joints

J= S/LSjL+n(D,-t.)f,E,

for shells with expansion joints. See Note (1)

S j = Spring rate of the expansion joint, Ibs/inch (kN/mm)

K= E, t, (Do-t,)

E, t, N cd,-t,)

F,=O.Z5+(F-0.6)

(Use the calculated value of F 9 or 1 .O, whichever is greater.)Fand Gare asdefined in Paragraph RCB-7.132.



T = Tubesheet thickness used, but not less than 98.5% of the greater of the valuesdefined by Paragraph RCB-7.132 or X6-7.133. (The value assumed in evalu-ating F 4 must match the final computed value within a tolerance of * 1.5%)See Note (2).

Tube length between inner tubesheet faces, inches (mm).Differential thermal growth (shell -tubes), inches (mm) (See Section 7,Paragraph T-4.5).Tube length between outer tubesheet faces, inches (mm).Elastic modulus of the shell material at mean metal temperature, psi (kPa). (SeeParagraph RCB-1.431). See Note (3).Elastic modulus of the tube material at mean metal temperature, psi (kPa). (SeeParagraph RCB-1.432).Elastic modulus of the tubesheet material at mean metal temperature, psi(kPa). (See Paragraph RCB-1.432).Number of tubes in the shell.Outside diameter of the shell or port for kettle type exchangers, inches (mm).Outside diameter of the tubes (for integrally finned tubes, d D is root diameter offin), inches (mm).Tube wall thickness (for integrally finned tubes, t, is wall thickness under fin),inches (mm).

L =A L =

L, =E, =

E , =

E =

A: =

D,=d,=

t, =

t,=Notes:

RCB-7

Shell wall thickness, inches (mm).

(1) Jean be assumed equal to zero for shells with expansion joints where

&&-t&E*/ 1OL

(2) Tubesheets thicker than computed are permissible provided neither shall nor tubesare overloaded. See Paragraph RCB-7.2.

(3) For Kettle type,

E’ = (2L,)+[(4L,T,D,)/((DESHL

,+D,)T,)l+[(L,7pDp)/(D,T,)Iwhere

E sn = Elastic modulus of the shell material at mean metal temperature, psi(kPa). (See Paragraph RCB-1.431).

L = Tube length between inner tubesheet faces, inches (mm).

L p = Length of kettle port cylinder, inches (mm).

7 p = Kettle port cylinder thickness, inches (mm).

D p = Mean diameter of kettle port cylinder, inches (mm)

L, = Length of kettle cylinder, inches (mm).

7 x = Kettle cylinder thickness, inches (mm).

D, = Mean diameter of kettle cylinder, inches (mm).

L, = Axial length of kettle cone, inches (mm)

7 c = Kettle cone thickness, inches (mm).

.I62 EQUIVALEMT BOLTIt& PfiESSU’REWhen fixed tubesheets are extended for bolting to heads with ring type gaskets, theextension and that portion of the tubesheets inside the shell may differ in thickness.The extension shall be designed in accordance with Paragraph RCB-7.134. The effect



of the moment acting upon the tubesheet extension shall be accounted for insubsequent paragraphs in terms of equivalent tube side and shell side boltingpressures which are defined as:

Pm =6 . 2 M ,FZ G3

Plh=6 . 2 M,

F* G3

where

FandG

M,=

are defined in Paragraph RCB-7.132.

Total moment acting upon the extension under operating conditions, definedby the Code as MD under flange design, inch-pounds (mm-kN).

Total moment acting upon the extension under bolting-up conditions, definedby the Code as M o under fiange design, inch-pounds (mm-kN).

Equivalent bolting pressure when tube side pressure is acting, psi (kPa).

Equivalent bolting pressure when tube side pressure is not acting, psi (kPa).

RCB-7.163 EFFECTIVE SHELL SIDE DESIGN PRESSURE

The effective shell side design pressure is to be taken as the greatest absolute value ofthe following:

or

or

or

or

or

where

P =P,‘-P,

2

P - P , ’

P=P&

P =P, ,-P,-P,,

2

P =pas+pir

2

P=P,‘-P&

~,1.5+.,l.s+.,*,1-[(~)(~-~)~

l+J K F, I

P 5 = Shell side design pressure, psi (kPa) (For vacuum design, PI is negative)

2

G = Inside diameter of the shell, inches (mm)

D, = Maximum expansion joint inside diameter, inches (mm) (D, = G when noexpansion joint is present).

Other symbols are as defined under Paragraphs RCB-7.161 and RCB-7.162

64 Standards &The Tubular Exchanger Manufacturers Assbtiiation


Notes:

(1) Algebraic sign of P, ’ must be used above, and must be retained for use inParagraphs RCB-7.164, RCB-7.165, RCB-7.166, RCB-7.22 and RCB-7.23.

(2) When J = 0, formulae containing P, will not control.

(3) Delete the term P Br in the above formulae for use in Paragraph RCB-7.133.

(4) For kettle type, G = port inside diameter.

RCB-7.164 EFFECTIVE TUBE SIDE DESIGN PRESSURE

The effective tube side design pressure is to be taken as the greatest absolute value ofthe following:

P =P,‘+P,,+Pd

2

orP=P;+P8,When P o ’ is positive

p=Pt’-P*‘+P8t+Pd2 When PI ’ is negative

orP=P;-P;+P,,where

p ,=p 1+0.4JK(1.5+,+,)I t

[ 1 +JKF, 1

P, = Tube side design pressure, psi (kPa) (For vacuum design, P t isnegative).

G = Inside diameter of the shell, inches (mm).

Other symbols are as defined under Paragraphs RCB-7.161, X5-7.162, andRCB-7.163.

Notes:

(1) Algebraic sign of P t ’ must be used above, and must be retained for use inParagraphs RCB-7.165, RCB-7.166, BCB-7.22 and RCB-7.23.

(2)When J=O:

a) Formulae containing P d will not control.

b) When PI and P t are both positive the following formula is controlling:

(3) Delete the term P,, in the above formulae for use in Paragraph RCB-7.133,

(4) For kettle type, G = port inside diameter.

RCB-7.165 EFFECTIVE DIFFERENTTAL DESIGN PRESSUREUnder certaln’circumstances the Code and other regulatory bodies permit design onthe basis of simultaneous action of both shell and tube side pressures. The effectivedifferential design pressure for fixed tubesheets under such circumstances is to betaken as the greatest absolute value of the following:


S E C T I O N 5 MECHANICAL STANDARDS TEMA CLASS R C B

; 66

‘I

P=P,'-P,'+P,,

orP=

P,'-P,'+PB,iPd

,, 2

or P=P,,

or P=P,‘-P;

P,'-P,'+P,or P=

2

or P=P,,

where

P,,P*,,P St s PI ‘and PI ’ are as defined in Paragraphs RCB-7.161,RCB-7.162, RCB-7.163 and RCB-7.164.

Notes:

(1)

(2)

(3)

It is not permissible to use (P, - Pt) in place of P, to calculateP, ’in Paragraph RCB-7.163, and it is not permissible to use (P j - P.-) inplace of PI to calculate P,’ in Paragraph RCB-7.164.

”

,. .,r-k

When J = 0, the formulae containing P dwill not control.

Delete the terms P B( and P Br in the above formulae for use in ParagraphRCB-7.133.

RCB-7.166 FIXED TUBESHEETS OF DIFFERING THICKNESSES

The rules presented in Paragraphs RCB-7.161 through RCB-7.165 and RCB-7.2are intended for fixed tubesheet exchangers where both tubesheets are thesame thickness. Conditions can exist where it is appropriate to use tubesheetsof differing thicknesses. These conditions may result from significantly differingelastic moduli and/or allowable stresses. The-following procedure may beused for such cases:

(1) Separate the design parameters as defined in previous paragraphs foreach tubesheet system by assigning subscripts A and B to each of thefollowing terms:Tas7.andT.

LasL,andL,whereL,+L,=ZL

EasE,andE~‘,

F.asF,,andF.,

Note: Thevaluesofn/i,,M,,F,G,aL,L,,D.,t,,d.,2,E,,E,,Nand S i must remain constant throughout this analysis. If a fixedtubesheet exchanger has different bolting moments at eachtubesheet, the designer should use the values of M , and M zthatproduce the conservative design.

(2) Calculate 7, per Paragraphs RCB-7.161 through RCB-7.165 assuming thatboth tubesheets have the properties of subscript A and L n L L.



(3)

(4)

(5)

(6)

(7)

(8)

(9)

Note:

Calculate T,per Paragraphs RCB-7.161 through RCB-7.165 assuming thatboth tubesheets have the properties of subscript Band L, = LCalculate L A and LB as follows:L=L,-T,-T,

L”=[, +(;g?,y

L,=2L-L,Recalculate T, per Paragraphs RCB-7.161 through RCB-7.165 using theproperties of subscript A and L n from step 4.RecalculateT,per Paragraphs RCB-7.161 through RCB-7.165 using theproperties of subscript Band LB from step 4.Repeat steps 4 through 6 until values assumed in step 4 are within 1.5% ofthe values calculated in step 5 for T n and step 6 for T B.Round T n and T B up to an appropriate increment and recalculate L A andLB per step 4.Calculate the shell and tube stresses and the tube-to-tubesheet joint loadsper Paragraph RCB-7.2 for each tubesheet svstem using the appropriatebubscrip~ed’properties.

The shell and tube stresses and tube-to-tubesheet joint loads for eachtubesheet system should theoretically~be identical. Small differences mayexist, however, because of rounding the calculated tubesheet thicknessesin step 8. The tube stress and the tube-to-tubesheet joint loads from thetwo systems should be averaged before comparing these values to theallowablevalues as calculated in Paragraph RCB-7.2.

* RCB-7.2 SHELL AND TUBE LONGITUDINAL STRESSES - FIXED TUBESHEET EXCHANGERS

Shell and tube longitudinal stresses, which depend upon the equivalent and effective pressuresdetermined by Paragraphs RCB-7.161 through RCB-7.164, shall be calculated for fixed tubesheetexchangers with or without shell expansion joints by using the following paragraphs. The designershall consider the most adverse operating conditions specified by the purchaser. (See ParagraphE-3.2.)

Note: The formulae and design criteria presented in Paragraphs RCB-7.23 through RCB-7.25consider only the tubes at the periphery of the bundle, which are normally the most highlystressed tubes. Additional consideration of the tube stress distribution throughout the bundlemay be of interest to the designer under certain conditions of loading and/or geometry. Seethe “Recommended Good Practice” section of these Standards for additional information.

RCB-7.21 HYDROSTATIC TEST

Hydrostatic test conditions can impose excessive shell and/or tube stresses. These stressescan be calculated by substituting the pressures and temperatures at hydrostatic test for theappropriate design pressures and metal temperatures in the paragraphs that follow and inParagraphs RCB-7.161 through RCB-7.164 where applicable.

RCB-7.22 SHELL LONGITUDINAL STRESS

The effective longitudinal shell stress is given by:

s = c,(Do-~,)p,*s 4t.

where

c,= 1.0 except as noted below

p,*=p, Note (2)



orP,*=P,’

orp,*=-P,

OrP,*=P,+P,’

Note (2)

Note (1)

orP.‘=P,-P, Notes (1) and (2)

orP,+=P,‘-Pd Notes (1) and (2)

orP,*=P,+P,‘-P, Note (1)

where

P, = P , - P , ’

Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, usingactual shell and tubesheet thicknesses and retaining algebraic signs.

Notes:

(1) If the algebraic sign of P, * is positive, C, = 0.5.

(2);;;_F;;;la is not applicable for differential pressure design per Paragraph

A condition of overstress shall be presumed to exist when the lar est absolute value of S Iexceedsthe Code allowable stress in tension for the shell matena at design temperature, or.990% of

Yteld

Code alstress at hydrostattc test, or when the greatest negative value of S ,exceeds the

owable stress in compression at design temperature.

RCB-7.23 TUBE LONGITUDINAL STRESS - PERIPHERY OF BUNDLE

66

The maximum effective longitudinal tube stress, psi (kPa), at the periphery of the bundle isgiven by:

C, /;q P,* G2‘I=4 N t,(d,-t,)

where

c, = 1 .o except as noted below

P,* = P, Note (2)

orP,*=-P, Note (2)

orP,* = P, Notes (1) and (2)

orP,* = P, - P,

orP,* = Pz+ P, Notes (1) and (2)

orp,* = -P3+Pa”~’ Notes (1) and (2)

orP,*=P,-P,+P, Note (1)

where

P,=P,‘- $5( 1p,=p;- +( 1v

Other symbols are asdefined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, usingactual shell and tubesheet thicknesses and retaining algebraic signs.



Notes:

(1) If the algebraic sign of P, * is positive, C, = 0.5.

(2)T$l;_l;;;,la is not applicable for differential pressure design per Paragraph

A condition of overstress shall be presumed to exist when the largest positive value of S,exceeds the Code allowable stress in tension for the tube material at design temperature, or90% of yield stress at hydrostatic test, or when the greatest negative value of .S, exceeds theallowable compressive stress as determined in accordance with Paragraph RCB-7.24.

RCB-7.24 ALLOWABLE TUBE COMPRESSIVE STRESS - PERIPHERY OF BUNDLE

The’allowable tube compressive stress, psi (kPa), for the tubes at the periphery of the bundleis given by:

w h e n c,>’r

S, = Yield stress, psi (kPa), of the tube material at the design metal temperature.(See Paragraph RCB-1.42).

r = Radius of gyration of the tube, inches (mm), given by:

r=6.25 o, 2+(d0_2fr)z (SeeTableD-7).

h-l = Equivalent unsupported buckling length of the tube, inches (mm). The largestvalue considering unsupported tube spans shall be used.

1= Unsupported tube span, inches (mm).

0.6 for unsupported spans between two tubesheetsk = OBfor unsupported spans between a tubesheet and a tube support

1 .O for unsupported spans between two tube supports

F I = Factor of safety given by:

F,=3.25-OSF,

Note: FE shall not be less than 1.25 and need not be taken greater than 2.0.

Other symbols are as defined in Paragraph RCB-7.161.

Note: The allowable tube compressive stress shall be limited to the smaller of the Codeallowable stress in tension for the tube material at the design metal temperature(see Paragraph RCB-1.42) or the calculated value of S,

RCB-7.25 TUBE-TO-TUBESHEET JOINT LOADS - PERIPHERY OF BUNDLE

The maximum effective tube-to-tubesheet joint load, Ibs. (kN), at the periphery of the bundleis given by:



where

P,‘= P, Note (1)

orp,* =-Ps Note (1)

orP,*=P2-P3

P, and P, are as defined in Paragraph RCB-7.23. Other symbols are as defined inParagraphs RCB-7.161, RCB-7.163 and RCB-7.164, using the actual shell and tubesheetthicknesses.

Note: (1) This formula is not applicable for differential pressure design per ParagraphRCB-7.165.

The allowable tube-to-tubesheet joint loads as calculated by the Code or other means may beused as a guide In evaluating W,

The tube-to-tubesheet joint loads calculated above consider only the effects of pressureloadings. The tube-to-tubesheet joint loads caused by restrained differential thermalexpansion between shell and tubes are considered to be within acceptable limits if therequirements of Paragraph RCB-7.23 are met.

RCB-7.3 SPECIAL CASES

Special consideration must be given to tubesheet designs with abnormal conditions of support orloading. Following are some typical examples:

(1) Tubesheets with portions not adequately stayed by tubes, or with wide untubed rims.

(2) Exchangers with large differences in shell and head inside diamr8ers;~e.g. fixed tubesheets withkettle type shell.

(3) The adequacy of the statypes S and T, or types J

ing action of the tubes during hydrostatic test; e.g., with test rings forand W.

(4) Vertical exchangers where weight and/or pressure drop loadings produce significant effectsrelative to the design pressures.

(5) Extreme interpass temperature differentials.

Consideration may also be given to special design configurations ad/or methods of analysis whichmay justify reduction of the tubesheet thickness requirements.

RCB-7.4 TUBE HOLES IN TUBESHEETS

RCB-7.41 TUBE HOLE DIAMETERS AND TOLERANCES

Tube holes in tubesheets shall be finished to the diameters and tolerances shown in TablesRCB-7.41 and RCB7.41M, column (a). To minimize work hardening, a closer fit between tubeOD and tube ID as shown in column (b) may be provided when specified by the purchaser.

RCB-7.42 TUBESHEET LIGAMENTS

Tables RCB-7.42 and RCB-7.42M give permissible tubesheet ligaments, drill drift andrecommended maximum tube wall thicknesses.

*RCB-7.43 TUBE HOLE FtNlSH

The inside edges of tube holes in tubesheets shall be free of burrs to prevent cutting of thetubes. Internal surfaces shall be given a workmanlike finish.



TABLE RCB-7.41TUBE HOLE DIAMETERS AND TOLERANCES

(All Dimensions in Inches)Nominal Tube Hole Diameter and Under Tolerance

Nominal

Tube OD

114

3/3

Stan4”;d Fita

Specia\C&ose Fit

Nominal Under Nominal UnderDiameter TOlWanCe Diameter TC+Xa”Ce

a.259 0.004 0.257 0.002

0.384 0.004 0.382 0.002

Over Tolerance: 96% of tubeholes must meet value in column

(c). Remainder may not exceedvalue in column (d)

(C) (d)0.002 0.007

0.002 0.007

1-l/2 1.513 I 0.007 I 1.514 0.003 I 0.003 0.010

2 2.022 0.007 2.018 0.003 o.cO3 0.010

TABLE RCB-7.41 MTUBE HOLE DlA&lETERS AND TOLERANCES

(All Dimensions in mm)

Over Tolerance: 96% of tubeSpecial Close Fit

25.4 25.70 0.10 25.65 0.05 0.05 0.25

31.8 32.11 0.15 32.03 0.08 0.08 0.25

38.1 33.56 0.18 38.46 0.08 0.08 0.25

50.8 51.35 0.18 51.26 0.03 0.08 0.25

FIB-7.44TUBE HOLE GROOVINGTube holes for expanded joints for tubes 5/8” (15.9mm) OD and larger shall be machined with atleast two grooves, for additional longitudinal load resistance, each approximately i/8” (3.2mm) wideby l/64” (0.4mm) deep. When integrally clad or applied tubesheets facings are used, all groovesshould be in the base material unless otherwise specified by the purchaser. Strength welded tubasdo not require grooves. Tubesheets with thicknesses less than 1” (25.4mm) may be provided with

:~: one groove. When utilizing hydraulic expansion, grooves shall be l/4” (64mm) wide.

C-7.44 TlJ@E HOLE GROOVING

For design pressures over 300 psi (2068 kPa) and/or temperatures in excess of 350 a F (177 o C), thetube holes for expanded joints for tubes 5/8” (15.9 mm) OD and larger shall be machined with atleast two grooves, for additional longitudinal load resistance, each approximately i/8” (3mm) wideby l/64” (0.4 mm) deep. When integrally clad or applied tubesheet facings are used, all groovesshould be in the base material unless otherwise specified by the purchaser. Strength welded tubesdo not require grooves. Tubesheets with thicknesses less than 1” (25.4mm) may be provided withone groove. When utilizing hydraulic expansion, grooves shall be l/4” (6.4mm) wide.



Tube TubeDia. Pitch

da P

1/4

3/8

1/2

5/8

3/4

-716

-i-

11/4

11/2-

2

TABLE RCB-7.42

TABLE OF TUBESHEET LIGAMENTS AND RECOMMENDED HEAVIEST TUBE GAGES

(All Dimensions in Inches)

Minimum Std. Ligaments (96% of ligaments must equal orexceed va,“es tabulated below)

H e a v i e s t T u b e Nomin- Minimumn Recom- Hole al Permissible

-_do

p - d, m e n d e d ;;a: Liga- LigamentTube ment Width

KY?:Fit Width Tubesheet Thickness

1 1-l/2 2 z-1/2 3 4 5 ) 6

I .25 ‘j4 4” 1.012 0.238 0.205 0.203 0.202 0.200 0.198 0.195 0.192 0.1691.31 5116 0.301 0.26, 0.266 0.264 0.263 0.261 0.258 0.255 0.251 EZ1.38 318 9 0.363 0.330 0.328 0.32, 0.325 0.323 0.320 0.317 0.314 0.185

1.25 5/16 9 1,264 0.299 0.266 0.265 0.263 0.262 0.261 0.268 0.256 0.253 0.150

1.25 318 a 1.518 0.367 0.325 0.324 0.323 0.322 0.321 0.316 0.316 0.314 0.180

1.25 712 6 2.022 0.478 .- 0.446 0.445 0.444 0.443 0.442 0.440 0.438 0.250

Notes: The above table of minimum standard ligaments is based on a ligament?olerance not exceeding the sum of twice the drill drifttolerance plus 0.02V for tubes less than S/8” OD and 0.030’ for tube holes S/w OD and larger.Drill drift tolerance = 0.0016 (thickness of tubesheet in tube diameters), inches

*RCB-7.5 TUBE-TO-TUBESHEET JOINTS

RCB-7.51 EXPANDED TUBE-TO-TUBESHEET JOINTS

Expanded tube-to-tubesheet joints are standard.

~~-7.511 LENGTH OF EXPANSION

Tubes shall be expanded into the tubesheet for a length no less than 2” (50.8 mm) orthe tubesheet thickness minus 1 /e” (3.2 mm), whichever is smaller. In no case shallthe expanded portion extend beyond the shell side face of the tubesheet. Whenspecified by the purchaser, tubes may be expanded for the full thickness of thetubesheet.

C-7.51 1 LENGTH OF EXPANSION

Tubes shall be expanded into the tubesheet for a length no less than two tubediameters, 2” (50.8 mm),, or the tubesheet thickness minus l/8” (3.2 mm), whichever issmaller. In no case shall the expanded portion extend beyond the shell side face ofthe tubesheet. When specified by the purchaser, tubes may be expanded for the fullthickness of the tubesheet.



TABLE RCB-7.42 M

TABLE OF TUBESHEET LIGAMENTS AND RECOMMENDED HEAVIEST TUBE GAGES

(All Dimensions in mm)

Edo P-d

1.25 1.591.50 3.18

1.33 3.171.42 3.96

1.25 3.181.31 3 . 9 71.37 4.76

1.25 3.981.30 4 . 7 81.40 6.36

1.25 4.761.33 6.351.42 7.941.60 9 . 5 3

:::z Ec1.36 7.951.43 9.52

1.25 6 .351.31 7.941.38 9.53

1.25 7.94

I.25 9x

1.25 12.71

Iieaviest TubeRecom- Holemended Dia.

Tube Std.

2;Fit

ve table of minimum standarc.nce plus 0.5lmm for tubes 18:~Merance = 0.041 (thickness d

Tubesheet Thickness

laments is based on a ligament tolerance not exceeding the sum of twice the drillthan 15.9mm 00 and 0.76mm for tube holes 15.9mm OD and larger.lbesheet in tube diameters), mm.

RCB-7.512 CONTOUR OF THE EXPANDED TUBE

The expanding procedure shall be such as to provide substantially uniform expansionthroughout the expanded portion of the tube, without a sharp transition to the

unexpanded portion.

,, ,, RB-7.513 TUBE PROJECTION

Tubes shall be flush with or extend by no more than one half of a tube diameterbeyond the face of each tubesheet, except that tubes shall be flush with the toptubesheet in vertical exchangers to facilitate drainage unless otherwise specified bythe purchaser.

RCB-7.52 WELDED TUBE-TO-TUBESHEET JOINTS

When both tubes and tubesheets, or tubesheet facing, are of suitable materials, the tubejoints may be welded.

RCB-7.521 SEAL WELDED JOINTSWhen welded tube joints are used for additional leak tightness only, and tube loadsare carried by the expanded joint, the tube joints shall be subject to the rules ofParagraphs RCB-7.4 through RCB-7.51.

Standards Of The Tubular Exchanger Manufacturers AsSOCiatiOI’I 73


74

RCB-7.522 STRENGTH WELDED JOINTS

When welded tube joints are used to carry the longitudinal tube loads, considerationmay be given to modification of the requirements of Paragraphs RCB-7.4 throughRCB-7.51. Minimum tubesheet thicknesses shown in Paragraphs R-7.131, C7.131and B-7.131 do not apply.

RCB-7.523 FABRICATION AND TESTING PROCEDURES

Welding procedures and testing techniques for either seal welded or strength weldedtube ioints shall be by agreement between the manufacturer and the purchaser.

RCB-7.53 EXPLOSIVE BONDED TUBE-TO-TUBESHEET JOINTS

Explosive bonding and/or explosive expanding may be used to attach tubes to thetubesheets where appropriate. Consideration should be given to modifying the relevantparameters (e.g., tube-to-tubesheet hole clearances and ligament widths) to obtain aneffective joint.

R-7.6 TUBESHEET PASS PARTITION GROOVES

Tubesheets shall be provided with approximately 3/16” (4.8 mm) deep grooves for pass partitiongaskets.

CB-7.6 TUBESHEET PASS PARTITION GROOVES

For design pressures over 300 psi (2068 kPa), tubesheets shall be provided with pass partitiongrooves approximately 3/16” (4.8 mm) deep, or other suitable means for retaining the gaskets inplace.

RCB-7.7 TUBESHEET PULLING EYES~

In exchangers with removable tube bundles having a nominal diameter exceeding 12” (305 mm)and/or a tube length exceeding 96’ (2438 mm), the stationary tubesheet shall be provided with twotapped holes in its face for pulling eyes. These holes shall be protected in service by plugs ofcompatible material. Provision for means of pulling may have to be modified or waived for specialconstruction, such as clad tubesheets or manufacturer‘s standard, by agreement between themanufacturer and the purchaser.

RB-7.6 CLAD AND FACED TUBESHEETSThe nominal cladding thickness at the tube side face of a tubesheet shall not be less than 5/16’(7.8 mm) when tubes are expanded only, and l/8” (3.2 mm).when tubes are welded to thetubesheet. The nominal cladding thickness on the shell side face shall not be less than 3/8” (9.5mm). Clad surfaces, other than in the area into which tubes are expanded, shall have at least l/8’(3.2 mm) nominal thickness of cladding.

C-7.8 CLAD AND FACED TUBESHEETS

The nominal cladding thickness at the tube side face of a tubesheet shall not be less than 3/16’(4.8 mm) when tubes are expanded only, and i/8” (3.2 mm) when tubes are welded to thetubesheet. The nominal cladding thickness on the shell side face shall not be less than 3

/8” (9.5

mm). Clad surfaces, other than in the area into which tubes are expanded, shall have at east i/8”(3.2 mm) nominal thickness of cladding

.-


r-l

”

L.

”

r.

j ,,”

/-.

,P

-7

RCB-8 FLEXIBLE SHELL ELEMENTS


This paragraph shall apply to fixed tubesheet exchangers which require flexible elements to reduce shelland tube Ion

Ritudinal stresses and/or tube-to-tubesheet joint loads. Light gau

joints within t e scope of the Standards of the Expansion Joint Manufacturerse bellows ty e ax

il ” E p”nsion

ssoctatron ( JMA are notincluded within the purview of this paragraph. The analysis contained within these paragraphs is basedupon the equivalent geometry used in “Expansion Joints for Heat Exchangers” by S. Kopp and M. F. Sayer:however, the formulae have been derived based upon the use of plate and shell theory modified to accountfor the stiffness of the knuckle radii, when used. Flanged-only and Ranged-and-flued types of expansionjoints are examples of flexible shell element combinations. The designer shall consider the most adverseoperating condrtions specified by the purchaser. (See Paragraph E-3.2.)

ACE-E.1 APPLICATION INSTRUCTIONS AND LIMITATIONSThe formulae contained in the following paragraphs are applicable based upon the followingassumptions:

Applied loadings are axial.Torsional loads are negligible.The flexible elements are sufficiently thick to avoid instability.The flexible elements are axisymmetric.All dimensions are in inches (mm) and all forces are in pounds (kN).Poisson’s ratio is 0.3.

RCB-8.11 CALCULATION SEQUENCEThe sequence of calculation shall be as follows:

(1)(2)

(3)(4)(6)(6)(7)

(8)(9

(10)

Select a geometry for the flexible element per Paragraph RCB-8.21.Determine the effective geometry constants per Paragraph RCB-8.22.Calculate the element flexibility factors per Paragraph RCB-8.3.Calculate the element geometry factors per Paragraph RCB-84.Calculate the stiffness multiplier per Paragraph RCB-8.5Calculate the equivalent flexible element stiffness per Paragraph RCB-8.6.Calculate the induced axial force per Paragraph RCB-8.7 for each condiiion asshown in Table RCB-8.7.Calculate the flexible element moments and stresses per Paragraph RCB-8.8.Compare the ffexible element stresses to the appropriate allowable stresses perthe Code, for the load conditions as noted in step 7.Repeat steps 1 through 9 as necessary.

RCB-8.12 CORROSION ALLOWANCEThe shell flexible elements shall be analyzed in both the corroded and uncorroded conditions.

RCB-8.13 HYDROSTATIC TEST CONDITIONSThe shell flexible elements shall be evaluated for the hydrostatic test conditions.

RCB-8.2 GEOMETRY DEFINITIONThe geometry may be made up of any combination of cylinders and annular plates with or withoutknuckle radii at their junctions.

RCB-8.21 PHYSICAL GEOMETRY CONSTANTSFigure RCB-8.21 defines the nomenclature used in the following paragraphs based uponnominal dimensions of the flexible elements.



FIGURE RCB-8.21

(b)

whereID and I iare the lengths of the cylinders welded to single Rexible shell elements.When two flexible shell elements are joined with a cylinder, the applicable cylinder length. 2 0or 1 i used for calculation with the FSE shall be half the actual cylinder length. The applicablecylinder length, 1 0 and 1 i shall be 0 when a cylinder is not attached.

NOTE: All dimensions shown in Figure RCE-8.21 are in inches (mm).

RCB-8.22 EFFECTIVE GEOMETRY CONSTANTSFigure RCB-8.22 defines the nomenclature used in the following paragraphs based upon theequivalent flexible element model.

FIGURE RCB-8.22

+X1,

to?5L ’t, :1,

7 c

4

t.

Yb Y, u

7x+

t.


where


.

t, =t E if the flexible element has a knuckle radius at the inside junction, inches (mm)

t, if the flexible element does not have a knuckle radius at the inside junction,inches (mm)

t, =t p if the flexible element has a knuckle radius at the outside junction, inches (mm)

t, if the flexible element does not have a knuckle radius at the outside junction,inches (mm)

G+t,a=-2

, inches (mm)

OD-t,b=-

2, inches (mm)

I1=b-U , inches (mm)

L=f,16+ I ‘ , + -2 ’

inches (mm)

fEl,=f,+r,+- ,inches(mm)2

r,=r.+0.5tE inches (mm)ra=ra+0.5fE :inches(mm)K = Stiffener multiplier (See Paragraph RCB 8.5)

, inches (mm) Note: Cylindrical sections beyond the limit,

Y* = 2 a, need only meet the Coderequirements for cylinders.

, inches (mm) Note: Cylindrical sections beyond the limit,

Y b = 2 a, need only meet the Coderequirements for cylinders.

G,OD,tE,ro,rb,fo,fD,ti and l.areindicatedinFigureRCB-8.21.

Lc, RCB-8.3 ELEMENT FLEXlBlLlPl FACTORS

The effective flexibility factors are given by:

1.285 radians/inch (radians/mm)

“a==

1 ,285 radians/inch (radians/mm)

D, =O.O916E,t, 3, inch-pounds

Metric, D,=0.0916E.t, 3~10-6,mm-kN

D, = 0.0916Eatb ‘, inch-pounds

Metric, D,=0.0916E,t,3x10 -d , mm-kN



DE = O.O916E,t, 3, inch-pounds

Metric, DE=0.0916EEtE 3~10-6,mm-kN

0, = Pa YCI for the inner cylinder, radians

Q, = PO Yo for the outer cylinder, radians

j, = sinnsinhn

j,=cosflcoshI2

2 22’1, +12

k,=sinhfl+sinn

k, =coshCI+ cos.CI

k,

k,=sinh Cl - sin Cl

ko

k,=coshn- cosn

k,where

Thesevalues must becalculated for .Q, at theinner cylinder as well asnbat the outer cylinder.

E, = Modulus of elasticity of the inner cylinder, psi (kPa)

En = Modulus of elasticity of the outer cylinder, psi (kPa)

E E = Modulus of elasticity of the flexible shell element, psi (kPa)

Ea =E E if the flexible element has a knuckle radius at the inside junction, psi (kPa)E if the flexible element does not have a knuckle radius at the inside junction,p; (kPa)

Eb =E E if the flexible element has a knuckle radius at the outside junction, psi (kPa)E, if the flexible element does not have a knuckle radius at the outside junction,psi (kPa)

a, b , t cI , t D, t E1 y .and y bare defined in Paragraph RCB-8.22.

RCB-8.31 CYLINDER-TO-CYLINDER FLEXIBILITY FACTORS

The cylinder-to-cylinder flexibility factors, e .and e b are given by the fOlIOwing:

Note:

at the inside junction at the outside junction If there is no outer cylindere, = e e, = e s*= 1

Calculate C 4, C s, C 6, C , and C 8 with the appropriate values of C , , C 2 and C 3 for the inside andoutside junction.



when Cz is less than 1.0

SECTION 5

c, = -0.364661+ 0.338172 0 .0366351

CZ zC,

c,=_, 0687,+1.~l164_0.122627C* C2 z

C6 =0.0696709+ 1,7641X,-5.46103C, 3

C,=-0.142734+0.9186S6C,-2.00749C,3

when C z is greater than or equal to 1 .O

c,=3.37310- 1.707962C2+0.226216C2z

1000

C, = -0.403287 + 0.320037C,- O.O307508C, *

C6=-0.684978+0.582549C2-0.0547812C2 2

CT=-0.201334+0.168201Cz-0.0157280Czz

a n d

c5 cb c7- - -_3+---i-cqc,=clz cb e,;’

c3

e = 2.718”

Notes:

(1) When C, is less than 0.4, C z shall be set equal to 0.4.

(2) When Cz and C 3 are both equal to 1.0, e shall be set equal to 1.0.

RCB-8.4 ELEMENT GEOMETRY FACTORS

Calculations for the stiffness and stresses are dependent upon the ffexible element geometry factorsgiven by:

Note: kvalues are evaluated using 0, for the inner cylinder.

Note: kvalues are evaluated using C,for the outer cylinder.

x = -ac(0.769+ 1.428d’)I

DC

2.2~~ d2.X2=

DE



X3=-a2[1.538+ln(d){2+.c(2+3.714d2)}]

40,

x =-2.2bc4 DE

x5=bc(0.769d2+ 1.428)

DE

x =-ab(l.538+5.714cln(d))6

40,

X=(x,-y,)(x,+y,)-x,x,

XZX6-X3X5-X3Y2X, =

X

q, =0.385a2+ 1.429cb21n(d)

q,=(-0.385-1.429cln(ci))bZ

q, = 0.25ab2!~+3.714c(in(d))2

g49*=1_g2-------n(s)

m, = 0.51- 0.635g2 +g*

m,=0.635(1-g’)+g*

m,=2.357g~+3.714g*

aandbaredefinedinPamgraphRCB-8.22and13.,(3,.D.,~D,,D,,e.,e,,k,,k,andk,are defined in Paragraph RCB-8.3.


c MECHANICAL STANDARDS TEMA CLASS R C Bc

SECTION 5

c RCB-8.5 STIFFNESS MULTIPLIER

RCR-8.51 If y,/G 2 0.073, y0 = 1 Ify,/G < 0.075, calculatey,pertheformula given below

Ifyb/G>0.075,y,= 1. Ify,~G<O.O75,calculatey,pertheformulagivenbelow.

y,=O.961- 1 1.293(y./G)+450.903(y./G)2-5647(~~/G)3+23140(y~/C)~

RCB-8.52 If both r,and rD are present, Fig. RCB-8.21 (a) and rm = rb, determine value of mfromFigure RCB-8.51 and calculate the term, = , according to the following equations:

Fort< 160,~~4.30(G/1E)~0~*87

For:> 160,~=2.92(G/tE)~0~21’

The final stiffness multiplier is represented by the product, K = =m y0 v b

RCB-8.53 If both r ,and rb are present, Fig. RCB-8.21 (a), but not equal, determine m 0, from Fig. ~‘-RCB-8.52 using r Ib, m from Fig. RCB-8.51 using r ‘= , and m 02 from Figure RCB-8.52 usingr’_ Calculate m as shown in Paragraph RCB-8.52 above.

The final stiffness multiplier is represented by the product,

K ;c(mmnIzy,v,

RCB-8.54 If onlyrb is present, Fig. RCB-8.21 (b) , determine m from Figure RCB-8.52 and calculatethe term, h , according to the following equations:

m,For: < 160,h=2.13(G/tE)~0”49

I; ~j,,, ,, .L

4,

3 ‘,,,,

hFort t 160,h= 1.86(G/tE)~“‘22

3 The final stiffness multiplier is represented by the product, K = hm y, y,49

4RCR-8.55 If only r cL is present, Fig. RCB-8.21 (c) determine m from Figure RCB-8.51 using r ‘o and

calculate = , from Paragraph RCB-8.52. Determine m “from Figure RCB-8.52 using r ‘o = r ‘”

r3 and calcutate, A , from Paragraph RCB-8.54.

” The final stiffness multiplier is represented by the product,

K==mhm,YaYo

km,-=m+=mhm,

RCB-8.56 If both r ,and rb equal 0 , Fig. RCB-8.21 (d), K = y 0 v “.


w

3.000 -

2.800 -.Ratios not within the range of the r/t and r/h values shown areconsidered outside the scope of this analysis.

r/t = 8

2.600 --

2.400 -/'

E3 2.200

tig 2.000

1

i l'*O"Q-J 1.600

r/h

FIGURE RCB-8.51Stiffness Multiplier as a Function of Flexible Shell Element Dimensionless Parameks

(Inner and Outer Knuckle Radii Equal)

Fl?Htn

2.OGO

1.900

1.800

1.700

1.600

1.500

1. .400

1.300

1.200

1.100

1 .ooo

r/h

FIGURE RCB-8.52Stiffness f&Mptief 89 a Function of Flexible Shell Element DimSIISiOnlSSS l%WimStSrS

(No Inner thuckte)


RCB-8.6 EQUIVALENT FLEXIBLE ELEMENT STIFFNESS

When there is only one flexible shell element (See Paragraph RCB8.2) in a shell, the spring rate,Ibs/inch (kN/mm), is given by:

sj,=2naD, K

x7qi+x8qz+q3where the terms are defined in Paragraphs RCB-8.22, RCB-8.3, RCB-8.4, and RC6-8.5.

When two or more flexible elements are used in a shell, the overall effective spring rate of the systemof flexible elements is given by:

1si=

‘+’ ,....+-1_SjEl a ,EZ S/E”

where

s j = Overall effective spring rate, Ibs/inch (kN/mm), as used in Paragraph RCB-7.161

s jE, , s iE2,. . s jEn = Respective spring rates of each flexible shell element, calculatedmdrvrdually from the above formula, Ibs/inch (kN/mm)

Note: A single convolute consists of two flexible shell elements.

RCB-8.7 INDUCED AXIAL FORCE

84

The calculation of the flexible shell element stresses is contingent upon calculating an induced axialforce acting on each element. This axial force on the inner shell circumference shall be calculated foreach condition as described in Paragraphs RCB-8.11 through RCB-8.13 and is given by:

CZP,’F,,=y I Ibs./inch

(Metric) F,, = Fx tom6 , kN/mm

where P,*=P,+P,‘-Pdand P,=P,-P,*

TABLE RCB-8.7F cI* PARAMETER VARIATIONS

Notes:(1) This condition is not applicable for differential pressure design per Paragraph RCB-7.165.

(2) a is defined in Paragraph RCB-8.22.


5fi

9nFs9 MECHANICAL STANDARDS TEMA CLASS R C B SECTION 5

(3) Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, usingactual shell and tubesheet thicknesses for each condition under consideration parParagraphs RCB8.11 through RCB-8.13. ALGEBRAIC SIGNS MUST BE RETAINED.

RCB-8.8 FLEXIBLE ELEMENT MOMENTS AND STRESSES

,. The following paragraphs provide the formulae to calculate the predicted stress levels in each flexibleelement. Each flexible element configuration will have a unique set of stresses for each conditionanalyzed.

RCB-8.81 MOMENTS AT THE JUNCTIONS

~,The stresses in the annular flat plate and the cylindrical portions of a flexible element aredependent upon the moments, inch-lbs per inch (mm-kN per mm) of circumference, at theinside and outside junctions. The moments are given by:

P,b3-0, = 80,

i-2gm,-y$g%(g)

P,b3e* = -

8D, (-*m,-m,+0.5-g’)

PI = Shell side design pressure, psi (kPa), for the condition under consideration(including 0 or negative value if vacuum, as applicable)

F yx = The term as calculated in Paragraph RCB-8.7 dependent upon the conditionunder consideration

k , and ki = The terms as calculated in Paragraph RCB-8.3, using 0. *at the outer cylinder

The remaining terms are as defined in Paragraphs RCB-8.22, RCB-8.3 and RCB-8.4

ACB-8.82 ANNULAR PLATE ELEMENT STRESSES

The~annular plate meridional bending stress, psi (kPa), shall be calculated for each conditionspecified in Paragraphs RCB-8.11, RCBB. 12 and RCB8.13 from the following formula:

where

A,=-cM.+cdZM,+0.65acF,,In(g)-P,(0.325m,b2+0.4l25a2)

A,=b’(cM.-CM,-0.65acFa~ln(g)+0.0875m,P,b2)


3


A,=0.65a(F..-0.5aP,)

F Cl.". = The term as calculated in Paragraph RCB-8.7 dependent upon the conditionunder consideration.

PI = Shell side design pressure, psi (kPa), for the condition under consideration(including 0 or negative value if vacuum, as applicable).

r = Radial distance, from the shell centerline to the point under consideration,inches (mm).

The remaining terms are as defined in Paragraphs RCB-8.22. RCB-8.4 and RCB-8.81

Note:

(1) SW = S b calculated for the shell side pressure only condition

(2) S rnbd = S b calculated for the differential expansion only or tube side pressure onlycondition.

(3) S R = S bcalculated for all conditions as specified in Table RCB-8.7.

(4) s,,, , s,,, and S mmd as defined by the Code, are negligible for the annularplate element within the scope of Paragraph RCB8.

(5) The maximum annular plate stress will be located where:

or r=a

err-b

~c~3-8.133 CYLINDRICAL ELEMENT STRESSES

The circumferential membrane stresses, psi (kPa), in the cylinders shall be calculated for eachcondition specified in Paragraphs RCB-8.11, RCB-8.12 and RCB-8.13 from the followingformula:

S =E(6+u,)m r

where

u, =13(y-x)

v,=B,sin(v,)sinh(v,)+B,cos(v,)cosh(v,)

6=$P,r-O.W,]

x = The distance under consideration, as shown in Figure RCB-8.22, inches (mm)

$eBr;Aning terms are as defined in Paragraphs RCBS.21, RCB-8.22, RCB-8.3 and



E=E,

M=M.

F,=F..

e=&? 0

D=D,

whereFor the inner cylinder

r=CI

f=t,for(y,-x)< 1,

t=t.for(y.-x)>lj

t=smalleroft.or t, for(y,-x)= Ii

For the outer cylinder

r=b

t=t,for(yb-x)<lo

t=l,for(ya-x)>I,

t = smaller oft, or t (1 for

(Yh-X)= I,

E-E,

M=M,

e= eb

D=D,

B=P.3

Y=Ya

(1) SC,“, = S m calculated for the shell side pressure only condition.

(2) s cm.? = S m calculated for the differential expansion only or tube side pressure onlycondition.

(3) s Cmpd = S, calculated for the combined pressure and differential expansion,, condition.

(4) The maximum value of S m will be located where x = y y or x = 1 a for the innercylinder and where x = yb or x = 1, for the outer cylinder.

RCB-8.84 MAXIMUM CYLINDER STRESS FOR CYCLE LIFE CALCULATIONSThe maximum stress, psi (kPa), for a particular set of conditions, for use in the evaluation ofcycle life is given by:

where

F 2 is defined in Paragraph RCB-8.83

andFor the inner junction

M=M,

t = the smaller of t E or t c1

For the outer junction

M=M,

t = the smaller oft E or t b



Note:

(1) A positive value of M establishes a compressive stress in the outer fiber of thecylinder under consideration,

(2) S,, is a possible outer limit for establishing a stress range.

(3) S,for the cylindrical element is equal to S,,.

RCB-8.9 ALLOWABLE STRESSES

The allowable flexible element stresses shall be as defined by the Code, using an appropriate stressconcentration factor for the geometry under consideration.

RCB-8.10 MINIMUM THICKNESS

The minimum thickness of flexible shell elements shall be as determined by the rules of ParagraphsRCB-8.1 throuless than i/8” 3.2 mm) for nominal diameters 18” (457 mm) and smaller, 3/16’ (4.8 mm) for nominal

9

h RCB-8.9. However, in no case shall the thickness in the uncorroded condition be

diameters 19” 483 mm) through 30” (762 mm), or l/4” (6.4 mm) for nominal diameters greater than30” (762 mm).

RCB-9 CHANNELS, COVERS, AND BONNETS

RCB-9.1 CHANNELS AND BONNETS

R-9.11 MINIMUM THICKNESS OF CHANNELS AND BONNETS

Channel and bonnet thickness is determined by the Code design formulae, plus corrosion allowance,but in no case shall the nominal thickness of channels and bonnets be less than the minimum shellthicknesses shown in Table R-3.13. The nominal total thickness for clad channels and bonnets shallbe the same as for carbon steel channels.

CB-9.11 MINIMUM THICKNESS OF CHANNELS AND BONNETS

Channel and bonnet thickness is determined by the Code design formulae, plus corrosion allowance,but in no case shall the nominal thickness of channels and bonnets be less than the minimum shellthicknesses shown in Table CB3.13. The nominal total thickness for clad channels and bonnetsshall be the same as for carbon steel channels.

RCB-9.12 MINIMUM INSIDE DEPTH

For multipass channds and bonnets the inside depth shall be such that the minimum cross-over areafor flow between successive tube passes is at least equal to 1.3 times the flow area through the tubesof one pass. When an axial nozzle is used, the depth at the nozzle centerline shall be a minimum ofone-third the inside diameter of the nozzle.


RCB-9.131 MINIMUM THICKNESS

The thickness of pass partitions shall not be less than the greater of that shown inTable RCB-9.131 or calculated in Paragraph RCB-9.132. Pass partition plates may betapered to gasket width at the contact surface.

TABLE RCB-9.131

NOMINAL PASS PARTITION PLATE THICKNESSDimensions are in Inches (mm)

1 Nominal Size I Carbon Steel Alloy Material


Less than 24(616)

24to66(610-1524)

61 to 100(1549-2540)


RCB-9.132 PASS PARTITION PLATE FORMULA- -

where

t 2 Minimum pass partition $ate rhickne&, in&h& (mm)

B = Table value (linear interpolation may be used)

g = Pressure drop across plate, psi (kPa)

.S = Code allowable stress in tension, at design metal temperature, psi (kPa)

b = Plate dim&&n. &&Table RCB-&132, inches (&)

TABLE RCB-9.132PASS PARTITION DIMENSION FACTORS

Three sides fixedOne side simply supported

a / b B0.25 0.0200.50 0.081

,0.75 0.1731.0 0.3071.5 0.5392.0 0.6573.0 0.718

Long sides fixedShort sides simply

supported

a / b B1.0 0.41821.2 0.46261.4 0.48601.6 0.49681.8 0.49712.0 0.4973a7 0.5000

Short sides fixedLong sides simply supported

a/b1.0

I .21.41.61.82.0

B0.4182

::KZ0.65400.69120.71460.7500

RCB-9.133 PASS PARTITION WELD SIZE

The pass partition plate shall be attached with fillet welds on each side with a minimumleg of 3/4 t from Paragraph RCB-9.132. Other types of attachments are allowed butshall be of equivalent strength.


Special con&ier&tior&&t be given to reinforcement or thickness requirements forinternal partitions subjected to pulsating fluids, extreme differential pressures and/ortemperatures, undue restraints or detrimental deflections under specified operatingconditions or unusual start-up or maintenance conditions specified by the purchaser.

Consideration may also be given to special design configurations and/or methods ofanalysis which may justify reduction of pass partition plate thickness requirements.

Also, consideration should be given to potential bypass of tubeside fluid where thepass partition might pull away from the gasket due to deflection.

RCB-9.14 POSTWELD HEAT TREATMENT

Fabricated channels and bonnets shall be postweld heat treated when required by the Codeor specified by the purchaser.

Standards Or The Tubular Exchanger Manufacturers Association 89

SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C B ~’

RCB-9.2 FLAT-CHANNEL COVER

*RCB-9.21 FLAT CHANNEL COVER DEFLECTION - MULTIPASS UNITS

The effective thickness of a flat channel cover shall be the thickness at the bottom of the passpartition groove (or the face if there is no groove) minus corrosion allowance in excess ofgroove depth. The thickness is to be at least that required by the appropriate Code formulaand thicker if required to meet proper deflection criteria.

The recommended limit for channel cover deflection is:

0.03” (0.8 mm) for nominal diameters thru 24” (610 mm)

0.125% of nominal diameter (nominal diameter/800) for larger sizes

A method for calculation of channel cover deflection is:

Y = -+(O.O435G’P+ 0.5.SBA,h,)

where

Y =

G =

E =

T =

P =

s*=

Ag=

h,=

Channel cover deflection at the center, inches (mm)

Gasket load reaction diameter as defined by the Code, inches (mm)

Modulus of elasticity at design temperature, psi (kPa)

Thickness under consideration, inches (mm)

Design pressure, psi &Pa)

Allowable bolting stress at design temperature, psi (kPa)

Actual total cross-sectional root area of bolts, square inches (mm2)

Radial distance from diameter Gto bolt circle, inches (mm)

If the calculated deflection is greater than the recommended limit, the deflection may bereduced by acceptable methods such as:

Increase channel cover thickness by the cube root of the ratio of calculated deflectionto the recommended limit.

Use of strong backs.

Change type of construction.

Note: For single pass channels, or others in which there is no pass partition gasket sealagainst the channel cover, no deflection criteria need be considered.

R-9.22 CHANNEL COVER PASS PARTITION GROOVES

Channel covers shall be provided with approximately 3/16” (4.8 mm) deep grooves for passpartitions. In clad or applied facings, all surfaces exposed to the fluid, including gasketseating surfaces, shall have at least i/8” (3.2 mm) nominal thickness of cladding.

CB-9.22 CHANNEL COVER PASS PARTITION GROOVES

For design pressures over 300 psi (2068 kPa), channel covers shall be provided withapproximately 3/16” (4.8 mm) deep grooves for pass partitions, or other suitable means forholding the gasket in place. In clad or applied facings, all surfaces ex

,Rosed to fluid, including

gasket seating surfaces, shall have at least l/8” (3.2mm) nominal thrc ness of cladding.



RCB-10.1 NOZZLE CONSTRUCTION

RCB-10 NOZZLES

Nozzle construction shall be in accordance with Code requirements. Shell nozzles shall not protrudebeyond the inside contour of the shell if they interfere with bundle insertion or removal. Shell orchannel nozzles which protrude beyond the inside contour of the main cylinder wall must be selfventing or draining by notching at their intersection with the high or low point of the cylinder. Ifseparate vent and drain connections are used, they shall be flush with the inside contour of the shellor channel wall. Flange dimensions and facing shall comply with ASME B16.5. Bolt holes shall

” straddle natural center lines. Flanges outside the scope of ASME 816.5 shall be in accordance withCode.

WE-lo.2 NOZZLE INSTALLATION

Radial nozzles shall be considered as standard. Other types of nozzles may be used, by agreementbetween manufacturer and purchaser.

R-10.3 PIPE TAP CONNECTIONS

All pipe tap connections shall be a minimum of 6000 psi standard couplings or equivalent. Eachconnection shall be fitted with a round head bar stock plug conforming to ASME 816.11 of the samematerial as the connection. Alternate plug materials may be used when galling is anticipated, exceptcast iron plugs shall not be used.

C-10.3 PIPE TAP CONNECTIONS

All pipe tap connections shall be a minimum of 3000 psi standard couplings or equivalent

B-10.3 PIPE TAP CONNECTIONS

All pipe tap connections shall be a minimum of 3000 psi standard couplings or equivalent. Eachconnection shall be fined with a bar stock plug of the same material as the connection. Alternate

plug materials may be used when galling is anticipated, except cast iron plugs shall not be used.

RCB-10.31 VENT AND DRAIN CONNECTIONS,, All high and low points on shell and tube sides of an exchanger not otherwise vented or

drained by nozzles shall be provided with 3/4” minimum NPS connections for vent and drain.

R-10.32 PRESSURE GAGE CONNECTIONS

All flanged nozzles 2” NPS or larger shall be provided with one connection of 3/4” minimumNPS for a pressure gage unless special considerations allow it to be omitted. See ParagraphRB-10.4.

C-10.32 PRESSURE GAGE CONNECTIONS

Pressure gage connections shall be as specified by the purchaser. See Paragraph C-10.4

B-10.32 PRESSURE GAGE CONNECTIONS

All flanged nozzles 2” NPS or larger shall be provided with one connection of 1 2” minimumNPS for a pressure gage unless special considerations allow it to be omitted. See ParagraphRB-10.4.

RB-10.33 THERMOMETER CONNECTIONS

All flanged nozzles 4” NPS or larger shall be provided with one connection of 1” minimumNPS for a thermometer unless special considerations allow it to be omitted. See ParagraphRB-10.4.

C-10.33 THERMOMETER CONNECTIONS

Thermometer connections shall be as specified by the purchaser. See Paragraph C-10.4.

RB-10.4 STACKED UNITS

Intermediate nozzles bemeen units shall have flat or raised face flanges. Pressure gage andthermometer connections may be omitted in one of the two mating connections of units connectedin series. Bolting in flanges of mating connections between stacked exchangers shall be removablewithout moving the exchangers.



C-10.4 STACKED UNITSintermediate nozzles between units shall have flat or raised face flanges. Pressure gage andthermometer connections may be omitted in one of the two mating connections of units connectedin series.

RCG-10.5 SPLIT FLANGE DESIGNCircumstances of fabrication, installation, or maintenance may preclude the use of the normalintegral or loose full ring nozzle flanges.used in accordance with the Code.

Under these conditions, double split ring flanges may be

*RCB-10.6 NOZZLES LOADINGS

92 Standards Of The Tubular Exchange Manufacturers Association

T-7

Heat exchangers are not intended to serve as anchor points for piping; therefore, for purposes ofdesign, nozzle loads are assumed to be negligible, unless the purchaser specifically detarls suchloads rn his inquiry as indicated in Figure RGP-RCB-10.6. The analysis and any modifications in thedesign or construction of the exchanger to cope with these loads shall be to the purchasersaccount.

a-%

.--

The “Recommended Good Practice” section of these standards provides the designer with additionalinformation regarding imposed piping loads.


RCB-I 1 END FLANGES AND BOLTINGFlanges and bolting for external joints shall be in accordance with Code design rules, subject to thelimitations set forth in the following paragraphs.

R-11.1 MINIMUM BOLTSIZEThe minimum permissible bolt diameter is 3/4” M20). Sizes l”and smaller shall be CoarseThreadSeries, and larger sizes shall be S-Pitch Thread keries. Dimensional standards are included inSection 9, Table D-5. Metric thread pitch is shown in Section 9, Table D-5M.

C-11.1 MINIMUM BOLT SIZEThe minimum recommended bolt diameter is l/2” (M14). If bolting smaller than l/2” (M14) is used,precautions shall be taken to avoid overstressing the bolting. Dimensional standards are included inSection 9, Table D-5. Metric bolting is shown in Section 9, Table D-5M.

B-11.1 MINIMUM BOLT SIZEThe minimum permissible bolt diameter shall be 5/8” (M16). Dimensional standards are included inSection 9, Table D-5. Metric bolting is shown in Section 9, Table D-5M.

RCE-11.2 BOLT CIRCLE LAYOUT

RCB-I 1.21 MINIMUM RECOMMENDED BOLT SPACING;hzMminimum recommended spacing between bolt centers is given in Section 9, Table D-5 or

RCE-11.22 MAXIMUM RECOMMENDED BOLT SPACINGThe maximum recommended spacing between bolt centers is:

whereB = Bolt spacing, centerline to centerline, inches (mm)

dB = Nominal bolt diameter, inches (mm)

t = Flange thickness, inches (mm)

m = Gasket factor usad in Code flange calculations

RCB-11.23 LOAD CONCENTRATION FACTORWhen the distance between bolt centerlines exceeds recommended B,.,, the total flangemoment determined by Code design methods shall be multiplied by a correction factor equalto:

B

J-E---mex

where B is the actual bolt spacing as defined by Paragraph RCB-11.22.

RCE-11.24 BOLT ORIENTATIONBolts shall be evenly spaced and normally shall straddle both natural centerlines Of theexchanger. For horizontal units, the natural centerlines shall be considered to be thehorizontal and vertical centerlines of the exchanger. In special cases, the bolt count may bechanged from a multiple of four.

RCB-11.3 MINIMUM RECOMMENDED WRENCH AND NUT CLEARANCES

Minimum recommended wrench and nut clearances are given in Section 9, Table D-5 andTable D6M.


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C B””

RCB-11.4 BOLT TYPE

Except for special design considerations, flanges shall be through-bolted with stud bolts,threaded full lenath with a removable nut on each end. One full stud thread shall extendbeyond each nuTto indicate full engagement.

*ACB-11.5 LARGE DIAMETER LOW PRESSURE FLANGES

See “Recommended Good Practice” section.

*RCB-11.6 BOLTING-ASSEMBLY AND MAINTENANCE

A

*-*

94

See “Recommended Good Practice” section,


FLOW INDUCED VIBRATION SECTION 6

(Note: This section is not metricated.)

V-l SCOPE AND GENERAL

V-l.1 SCOPEFluid flow, inter-related with heat exchanger geometry, can cause heat exchanger tubes to vibrate.This phenomenon is highly complex and the present state-of-the-art is such that the solution to thisproblem is difficult to define. This section defines the basic data which should be considered whenevaluatin potential flow induced vibration problems associated with heat exchangers. When.potentiai low Induced vibration problems are requested to be evaluated, the relationships presented7in this section and/or other methods may be used. Due to the complexity of the problem, the TEMAguarantee does not cover vibration damage,

V-l.2 GENERAL

Damaging tube vibration can occur under certain conditions of shell side flow relative to baffleconfiguration and unsupported tube span. The maximum unsupported tube spans in TableRCB-4.52 do not consider potential flow induced vibration problems. In those cases, where theanalysis indicates the probability of destructive vibration, the user should refer to Paragraph V-13.

,~v-2 VIBRAT ION AMAGE PASTERNS

Mechanical failure of tubes resulting from flow induced vibration may occur in various forms. Damage canresult from any of the following independent conditions, or combinations thereof.

V-2.1 COLLISION DAMAGEImpact of the tubes against each other or against the vessel wall. due to large amplitudes of thevibrating tube, can result in failure. The impacted area of the tube develo s the characteristic,flattened, boat shape spot, generally at the mid-span of the unsupported ength. The tube wallPeventually wears thin, causing failure.

V-2.2 BAFFLE DAMAGE

Baffle tube holes require a manufacturing clearance (see Paragraph RCB-4.2) over the tube outerdiameter to facilitate fabrication. When large fluid forces are present, the tube can impact the bafflehole causing thinning of the tube wall in a circumferential, uneven manner, usually the width of thebaffle thickness. Continuous thinning over a period of time results in tube failure.

V-2.3 TtiBESHEtiT CLAMPING EFFECT

Tubes may be expanded into the tubesheet to minimize the crevice between the outer.$be wail andthe tubesheet hole. The natural frequency of the tube span adjacent to the tubesheet IS Increased bythe clamping effect. However, the stresses due to any lateral deflection of the tube are alsomaximum at the location where the tube emerges from the tubesheet, contributing to possible tubebreakage.

V-2.4 MATERIAL DEFECT PROPAGATION

Designs which were determined to be free of harmful vibrations will contain tubes that vibrate withvery small amplitude due to the baffle tube hole clearances and the flexibility of the tube,span. Suchlow level stress fluctuations are harmless in homogeneous material. Flaws contained wlthin thematerial and strategically oriented with respect to the stress field, can readily propagate and actuatetube failure. Corrosion and erosion can add to such failure mechanisms.

V-2.5 ACOUSTIC VIBRATION

Acoustic resonance is due to gas column oscillation and is excted by phased vortex shedding., Theoscillation creates an acoustic vibration of a standing wave type. The generated sound wave will notaffect the tube bundle unless the acoustic resonant frequency approaches the tube naturalfrequency, althou h the heat exchanger shell and the attached piping may vibrate, accompaniedwith loud noise. 8hen the acoustic resonant frequency approaches the tube natural frequency, anytendency toward tube vibration will be accentuated with possible tube failure.

V-3 FAILURE REGIONSTube failures have been reported in nearly all locations within a heat exchanger. Locations of relativelyflexible tube spans and/or high flow velocities are regions of primaty concern.


SECTION 6 FLOW INDUCED VIBRATION

V-3.1 U-BENDS

Outer rows of U-bends have a lower natural frequency of vibration and, therefore, are moresusceptible to flow induced vibration failures than the inner rows.

V-3.2 NOZZLE ENTRANCE AND EXIT AREA

Impingement plates, large outer tube limits and small nozzle d&net&s can contribute to restrictedentrance and exit areas. These restricted areas usually create high local velocities which can resultin producing damaging flow induced vibration.

,V-3.3 TUBESHEET REGION

Unsupported tube spans adjacent to the tubesheet are frequently longer than those in the baffledregion of the heat exchanger, and result in lower natural frequencies. Entrance and exit areas arecommon to this region. The possible high local velocities, in conjunction with the lower naturalfrequency, make this a region of primary concern in preventing damaging vibrations.

V-3.4 BAFFLE REGION

Tubes located in baffle windows have unsupported spans equal to multiples of the baffle spacing.Long unsupported tube spans result in reduced natural frequency of vibration and have a greatertendency to vibrate.

V-3.5 OBSTRUCTIONS

Any obstruction to flow such as tie rods, sealing strips and impingement plates may cause highlocalized velocities which can initiate vibration in the immediate vicinity of the obstruction.

V-4 DIMENSIONLESS NUMBERS

V-4.1 STROUHAL NUMBER

Shedding of vortices from isolated tubes in a fluid medium is correlated by the Strouhal Number,which is given by:

where

fs=v =

do=

,_f.do1 2 v

Vortex shedding frequency, cycies/sec

Crossflow velocity of the fluid relative to the tube, ft/sec

Outside diameter of tube, inches ~.’ “’ ~’ ” “. “~’ ” ‘~“.

For integrally finned tubes:

d 0 = Fin root diameter, inches

Note: In closely spaced tube arrays, the rhythmic shedding of vortices degenerates into a broadturbulence and a correlation based on Strouhal Number alone is inadequate.

V-4.2 FLUID ELASTIC PARAMETER

A dimensionless parameter used in the correlations to predict flow induced vibration is given by:

144w,6,X=

Pod0 2I.. ,,,,~ ,,, I, i,, ,.~. .,;,. ,~ .,:F: ,,->, ,., .,~‘,.:_i*,_~.,.‘;, i .,,, ,i~,,, ,,,,11 ,,,, .* ._ ,.,,.,.” ,,,,... , ,,..,,, ~,__” _,... “.~,, ,,.,,,___, . .._

,,

96 Standards Of The Tubular Exchanger Mantifacttirers Association


where

w0 = Effective weight of the tube per unit length, defined in Paragraph V-7.1, Ib/ft

5, = Logarithmic decrement in the tube unsupported span (see Paragraph V-8)

p 0 = Density of the shell side fluid at its local bulk temperature, Ib/ft3

d, = Outside diameter of tube, inches


d 0 = Fin root diameter, inches

V-5 NATURAL FREQUENCY

V-5.1 GENERAL

Most heat exchangers have multiple baffle supports and varied individual unsupported spans.Calculation of the natural frequency of the heat exchanger tube is an essential step in estimating itspotential for flow induced vibration failure. The current state-of-the-art flow induced vibrationcorrelations are not sophisticated enough to warrant treating the multi-span tube vibration problem(or mode shapes other than the fundamental) in one comprehensive analysis. Therefore, thepotential for vibration is evaluated for each individual unsupported span, with the velocity and naturalfrequency considered being that of the unsupported span under examination. For more complexmode shapes and multi-spans of unequal lengths, see Paragraph V-14 Reference (10).

V-5.2 FACTORS AFFECTING NATURAL FREQUENCY

The individual unsupported span natural frequency is affected by:

(1) Tube elastic and inertial properties and tube geometry.

(2) Span shape.

(3) Type of support at each end of the unsupported span.

(4) Axial loading on the tube unsupported span. (see Paragraph V-6)

V-5.21 SPAN SHAPESThe basic span shapes are the straight span and the U-bend span.

V-5.22 SPAN SUPPORTSThe common support conditions are:

( I) Fixed at the tubesheet and simply supported at the baffle.

(2) Simply supported at each baffle.

The baffle supports have clearances which render them non-linear when analyzed as asupport. The tubesheet is not rigid and, therefore, the “built-in” assumption IS onlyapproximate. These approximations are known to have minor effects on the calculatednatural frequency.

V-5.3 FUNDAMENTAL NATURAL FREQUENCY CALCULATION

The value of the fundamental natural frequency of a tube unsupported span can be calculated for thecombinations of span shape and end support conditions using Table V-5.3

where

,f a = Fundamental natural frequency of the tube unsupported span, CyCleS/Sec

I = Tube unsupported span as shown in Table V-5.3, inches

Elastic modulus of tube material at the tube metal temperature, psi (see ParagraphRCB-1.43)

Effective weight of the tube per unit length, defined in Paragraph V-7.1, Ib/ft



I - Moment of inertia of the tube cross section, Inches 4 is given by

I = &(d, 4-d,4)

d i = Tube inside diameter, inches

do = Outside diameter of tube, inches


d D = Fin root diameter, inches


I


Span Geometry

(1)Baffles

Edge condition: both endssimply supported

(2)Tubesheet

Edge condition: one end fixed. otherend simply supported

(31Tubesheets

Edge condition: both ends fixed

(4)

D

I-

Edge condition: both ends simplysupported

(5)

ED

I-


Edge condition: both ends simplysuPported

(7)

6 II

d ,I


TABLE V-5.3FUNDAMEkTAL NATURAL FREQUENCY

I

Eouation

SECTION 6

Nomenclature

= Tube axial stress multiplier. SeeParagraph V-6

= Constant depending on edgecondition geometry.

Span GeometryI c

1 9.9

2 15.42

3 22.37

___i__r = Mean bend radius, inches

c, = Mode constant of U-bend

Span Geometry C, Figure

v-5.3

v-5.3.1

v-5.3.2

v-5.3.3


SECTION.6 FLOW INDUCED VIBRATION

FIGURE V-S.3U-BEND MODE CONSTANT, c L1

8d

2 !2d d

2d


.

/

L-


FIGURE V-5.3.1U-SEND MODE CONSTANT, C

I(

SECTION 6

i

0

d



FIGURE V-5.3.2U-SEND MODE CONSTANT, C u

$d

sd

c5

:: zd d

102 Stancfards Of The Tubular Exchanger Manufacturers Association


FIGURE V-5.3.3U-BEND MODE CONSTANT, C u

SECTION 6

-

-

-

-

-

-

-

-

-

-

-

-

6%,..,

r, Standards Of The Tubular Exchanger Manufacturers Association 103


V-6 AXIAL TUBE STRESS

V-6.1 AXIAL TUBE STRESS MULTIPLIER

By the very function of a heat exchanger, the tubes are subjected to axial loads. Compressive axialloads decrease the tube natural frequency, and tensile loads tend to increase it. The resulting tubeaxial stress multiplier for a given tube unsupported span is determined by the tube end supportconditions.

1/Z?

where

F=S,A,

S,=

A, =

FK’EI

CR= -12

K =

K=

K =

E =

l=

I =

V-6.2 U-TUBES

Tube longitudinal stress, psi (for fixed tubesheet exchanger, s, may becalculated from Paragraph RCB-7.23)

Tube metal cross sectional area, inches ’ (see Table D-7)

Jtfor both ends simply supported

4.49 for one end fixed, other end simply supported

2 Ft for both ends fixed

Elastic modulus of tube material at the tube metal temperature, psi (seeParagraph RCB-1.43)

Tube unsupported span, inches

Moment of inertia of the tube cross-section, inches 4 (see Paragraph V-5.3 andTable D-7)

For some applications U-tubes may develop high levels of axial stress. A method to compute thetube axial stresses in the legs of U-tube exchangers is given in Paragraph V-14, Reference (1).

V-7 EFFECTIVE TUBE MASS

To siminstea dp

lify the application of the formulae, the constants have been modified to enable the use of weightof mass.

V-7.1 EFFECTIVE TUBE WEIGHTEffective tube weight is defined as:

w,=w,+w,~+H,

w t = Total metal weight per unit length of tube, Ib/ft (see Table D-7)

Wfl = 0.00545p idi s = Weight of fluid inside the tube per unit length of tube, Ib/ft

H m = Hydrodynamic mass from Paragraph V-7.1 1


SECTION 6FLOW INDUCED VIBRATION

where

p i = Density of fluid inside the tube at the local tube side fluid bulk temperature, Ib/ft 3

d i = Inside diameter of tube, inches

V-7.11 HYDRODYNAMIC MASS

Hydrodynamic r&S is an S&t d&h increases the apparent weight of the vibrating body due tothe displacement of the shell side fluid resulting from:

(1) Motion of the vibrating tube

(2) The proximity of other tubes within the bundle

(3) The relative location of the shell wall

Hydrodynamic mass is defined as:

H, = C,w,,

where

cm = Added mass coefficient from Figure V-7.1 I

wfo= o.oomp,d, ‘= Weight of fluid displaced by the tube per unit length of tube, Ib/ft

where

p e = Density of fluid outside the tube at the local shell side fluid bulk temperature,

ib/ft3 (For two phase fluids, use two phase density.)



d, = Fin root diameter, inches

Standards Of The Tubular Exchanger Manufacturers Association I 105


FIGURE V-7.1 1

,.LC.“, i, i ”,.:. ,,~, .,m, :,,: :.,, ,.,.,i-

k*+Y’_il: ~,ADDED MASS COEFFICIENT - C, 1

TUBE PITCH

TUBE ODE’;

106 Standards Of ihe Tubular Exchanger Manufacturers Association


0 V-8 DAMPING

8The mechanisms involved in damping are numerous, and the various effects are nor readily measured or

0quantified. The following expressions for logarithmic decrement, 6 p are based strictly on experimentalobservations and idealized models.

0 For shell side liquids, 6 Tis equal to the greater of 6 1 or 6,

3.41 do6,=-

wof,

O.O12d,or 6,=

w0

whereIL = Shell side liquid viscosity, at the local shell side liquid bulk temperature, centipoise

d 6 = Outside diameter of tube, inches. For integrally finned tubes,

do = Fin root diameter, inches

p 6 = Density of shell side fluid at the local bulk temperature, Ib/ft 3

f n = Fundamental natural frequency of the tube span, cycles/set

zUO = Effective weight of the tube as defined in Paragraph V-7.1, lb/r?

f3 For shell side vapors 6 T = 6 v as follows:

6, = 0.3,4&

where!? N = Number of spans/e3 t b = Baffle or support plate thickness, inches

0 1 = Tube unsupported span, inches

8 ,, For two phase shell side media

0 ,,Q

6,-p= O.‘=Wf(s,)f(si)

wheref ( e o ) = Void fraction function

Eg=6x

for Eg < 0.4

= 1 for 0.4 5 tp 5 0.7

= I-(s) f o r t,>0.7

V,E =-0 v,+v,~

I/ 9 = Volume flowrate of gas, ft3/sec

I/ I = Volume flowrate of liquid, ft3/sec

f (s 7 j = Surface tension function

ST=-ST70



s I = Surface tension of shell side liquid at the local bulk temperature.Paragraph V-14, Reference (20))

(See

srm- Surface tension of shell side liquid at ambient temperature.V-14, Reference (20))

(See Paragraph

P I = Density of shell side liquid at the local bulk temperature, Ib/ft3

P ~ = Density of shell side gas at the local bulk temperature, lb/ft3

di, = Outside diameter of tube, inches. For integrally finned tubes, d 0 = Fin rootdiameter, inches

w, = Effective tube weight as defined in Paragraph V-7.i,Ib/ft

Note: Use two phase density in the calculation for hydrodynamic mass

P rp = Two phase density at local bulk temperature Ib/ft3

=PJ-e.)+P,c.

c,, = Confinement function, seeTable V-8

Total two phase damping

6,=6,,+6,+b,

Note: Use two phase properties for density and hydrodynamic mass.

TABLE V-8

CONFINEMENT FUNCTIONC,”

Triangular Pitch Square PitchC,” CW

1.20 2.25 1.871.25 2.03 1.721.33 1.78 1.561.50 1.47 1.35

,, ,:, ,~,~.


”,i

.,,

FLOW INDUCED VIBRATION sECTION 6

V-9 SHELL SIDE VELOCITV DISTRIBUTION

V-9.1 GENERAL,,

One of the most important and least predictable parameters of flow induced vibration is fluid velocity.To calculate the local fluid velocity at a particular point in the heat exchanger is a difficult task. Verycomplex flow patterns aretube bundle or leak througt:

resent in a heat exchanger shell. Various amounts of fluid bypass theclearances between baffles and shell, or tube and baffle tube holes.

Until methods are developed to accurately calculate local fluid velocities, the designer may useaverage crossflow velocities based on available empirical methods.

V-9.2 REFERENCE CROSSFLOW VELOCITY

The crossflow velocity in the bundle varies from span to span, from row to row within a span, andfrom tube to tube within a row. The reference crossflow velocity is calculated for each region ofinterest (see Paragraph V-3) and is based on the average velocity across a representative tube row inthat region.

The presence of pass partition lanes aligned in the crossflow direction, clearance between the bundleand the shell, tube-to-baffle hole annular clearances, etc. reduce the net flow rate of the shell sidefluid in crossflow. This should be considered in computing the reference crossflow velocity.

V-9.21 REFERENCE CROSSFLOW VELOCITY CALCULATIONS

The following method of calculating a reference crossflow velocity takes into account f$idbypass and leakage which are related to heat exchanger geometry. The method is valrd forsingle phase shell side fluid with single segmental baffles in TEMA E shells. Other methodsmay be used to evaluate reference crossflow velocities.

Reference crossflow velocity is given by:

v -‘(Fh)W)

(M)(o,)(~0)(3600) ‘ft’sec

V-9.21 1 CALCULATION OF CONSTANTS

The constants used in the calculation of the reference crossflow velocity are given by:

d,-d,c, = -

d,

C3=DI-D,

D,



TABLE V-9.2ilA

TUBE PAlTERN (See Figure RCB-2.4)

30” 60” 90” I 45”

110

C4 1.26 1.09 1.26 0.90

C, 0.82 0.61 0.66 0.56

I1 I I I

CC5 1.40 1.28 “~ 1.38 1.17I I I

m 0.85 0.87 0.93 0.80

TABLE V-9.21 1B

hC 8 vs cut-to-diameter ratio z

h 0.10 0.15 0.20 0.25 0.30 0.35 0.40 0.45 0.50

z

C* 0.94 0.90 0.86 0.80 0.74 0.68~ 0.62 0.54 0.49

Linear interpolation is permitted

1 1.67

M =

ax = (b)(Dd(Col)where

D j = Shell inside diameter, inches

D z = Baffle diameter, inches

D 3 = Outer tube limit (OTL), inches

d I = Tube hole diameter in bafk inches





cl 0 = Fin outside diameter, inches

P = Tube pitch, inches

1 3 = Baffle spacing, inches

P o = Density of shell side fluid at the local bulk temperature, lb/t”

W = Shell fluid flow rate, Ib/hr

h = Height from baffle cut to shell inside diameter, inches

v-e.3 SEAL STr3fP.SSeal strips are often usad to help block the circumferential bypass space between a tube bundle andshell, or other bypass lanes. Seal strips force fluid from the bypass stream back into the bundle.This increases the reference crossflow velocity and should be considered in a vibration analysis.

Local fluid velocity in the vicinity of seal strips may be significantly higher than the average crossflowvelocity. (See Paragraph V-14, Reference 6.)

V-9.31 REFERENCE CROSSFLOW VELOCITY WITH SEAL STRIPS

The reference crossflow velocfty is calculated by using a modified value for c 1 in theequations in Paragraph V-9.21 1.

C,=l+ (31i 1 +(l.s)(c,)

4

v-e.4 PASS LANES PARALLEL TO FLOW

When pass lanes are oriented parallel to flow (at 9O”to the baffle cut) they create a relatively lowresistance path for fluid to follow. The net effect is for less fluid to cross the tube bundle, resulting ina lower average crossflow velocity. However, tubes adjacent to these lanes may be subjected tohigh local velocities. The number and width of these lanes should be considered when the referencecrossflow velocity is calculated.

v-9.4-f REFERENCE CROSSFLOW VELOCITY WITH PASS LANES PARALLEL TO FLOW

To account for pass lanes5

rallel to flow, if they are not blocked by some type of specialbaffle, a modified value of a can be used

where

D3 = Outer tube limit minus (number of parallel pass lanes x width of pass lanes),inches

V-9.6 BUNDLE ENTRANCE REGION AND IMPINGEMENT PLATES

Tubes directly beneath inlet nozzles and impingement plates can be subjected to local fluid velocitiesgreater than those in other parts of the bundle. A number of documented vibration problems havebeen caused by high inlet fluid velocities. These standards provide guidelines for maximum velocityin this region and set criteria for the use of impingement plates. The p 1/s limits in ParagraphRCB-4.6 are furnished for protection against tube erosion, but do not necessarily prevent vibrationdamage.

V-9.6 INTEGRALLY FINNED TUBES

In computing the reference crossflow velocity, the presence of fins shall be taken into account. Forthe purposes of using the equations In Paragraph V-9.2 to calculate a reference crossflow velocity,the fin diameter should be used in place of the nominal tube OD for integrally finned tubes.



V-10 ESTIMATE OF CRITICAL FLOW VELOCITY

The critical flow velocity, V c , for a tube span is the minimum cross-flow velocity at which that span mayvibrate with unacceptably large amplitudes. The critical flow velocity for tube spans in the window, overlap,inlet and outlet regions, U-bends, and all atypical locations should be calculated. The critical velocity, I/c ,is defined by:

[/ =Df.do_Ift/sec

c 12

whereD = Value obtained from Table V-10.1

f n = Fundamental natural frequency, cycles/set (see Paragraph V-5.3)



cl 0 = Fin root diameter, inches

The user should ensure that the reference crossflow velocity V, at every location, is less than I/c for thatlocation.


,_


TABLE V-10.1

FORMULAE FOR CRITICAL FLOW VELOCITY FACTOR, D

Tube Pattern Parameter(See Figure RCB-2.4) Range for Dimensionless Critical Flow Velocity Factor, D

X

0.1 to 130 ” 8.86(-&0.+‘~

over 1 to 3008.86(++’

0.01 to 1 2.80~‘.‘~60”

over 1 to 300 2.80x0.”

0.03 to 0.7 2.10x0.‘5

over 0.7 to 300 2.35x0.”

0.1 to 300450 4.13(-+5]x~~~

P = Tube pitch, inches

d, = lube OD or fin root diameterfor integrally finned tubes, inches

144w,6,

x= pod,’= Fluid elastic parameter

where

p o = Shell side fluid density at the corresponding local shell side bulk temperature, Ib/ft

6 T = Logarithmic decrement (See Paragraph V-8)

W 0 = Effective weight of the tube per unit length, Ib/ft (See Paragraph V-7.1)



V-l 1 VIBRATION AMPLITUDE

V-11.1 GENERAL

There are four basic flow induced vibration mechanisms that can occur in a tube bundle. These arethe fluidelastic instability, vortex shedding, turbulent buffeting,, and acoustic resonance. The firstthree mechanisms are accompanied by a tube vibration ampktude while acoustic resonance causesa loud acoustic noise with virtually no increase in tube amplitude.

Fluidelastic instability is the most damaging in that it results in extremely large amplitudes of vibrationwith ultimate damage patterns as described in Paragraph V-2. The destgn approach in this case is toavoid the fluidelastic instability situation thereby avoiding the accompanying large amplitude ofvibration (see Paragraph V-10). Vortex shedding may be a problem when there is a frequency matchwith the natural frequency of the tube. Vibration due to vortex shedding is expected whenJ.<Zf.,,wheref,,= 12Sk/d.(see Paragraph V-12.2). Only then should the amplitude becalculated. This frequency match may result in a vibration amplitude which can be damaging totubas in the vicinity of the shell inlet and outlet connections. Vortex shedding degenerates into broadband turbulence and both mechanisms are intertwined deep inside the bundle. Vortex shedding andturbulent buffeting vibration amplitudes are tolerable within specified limits.and respective limits are shown below.

Estimation of amplitude

V-l 1.2 VORTEX SHEDDING AMPLITUDE

Y", = pc;\;mplftude of vibration at midspan for the first mode, for single phase fluids,

c, = Lift coefficient for vortex shedding, (see Table V-l 1.2)

PO= Density of fluid outside the tube at the local shell side fluid bulk temperature, lb/t3

do= Outside diameter of tube, inches

v =

6,. =

.f, =

LOO=

For integrally finned tubes, d 0 = fin root diameter, inches

Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

Logarithmic decrement (see Paragraph V-8)

Fundamental natural frequency of the tube span, cycles/set (see Paragraph V-5.3)

Effective tube weight per unit length of tube, Ib/ft (see Paragraph V-7.1)

114

CLp,doV’yus = 2rc26T,f~uJ,

V-11.21 RECOMMENDED MAXIMUM AMPLITUDE

YrS 5 O.O2d, , inches

V-11.3 TURBULENT BUFFETING AMPLITUDE

where

Yta = Maximum amplitude of vibration for single phase fluids, inches

c F = Force coefficient (see Table V-l 1.3)

V-11.31 RECOMMENDED MAXIMUM AMPLITUDE

Yrs 5 O.O2d, , inches



TABLE V-l 1.2

LIFT COEFFICIENTSC,

P

d,

30”

TUBE PATTERN (See Figure RCB-2.4)

60” 90” 45”

1.20 0.090 0.090 0.0701.25 0.091 0.091

::k%0.070

1.33 0.065 0.017 0.070 0.0101.50 0.025 0.047 0.068 0.049

‘TABLE V-11.3FORCE COEFFICENTS

C,

Location

Bundle Entrance Tubes

Interior Tubes

fn C,

<40 0.022

>40<88 -0.00045.f, + 0.04288 0

240 0.012

>40<88 -O.O0025f, + 0.022288 0



V-12 ACOUSTIC VIBRATION

Acoustic resonance is due to a gas column oscillation. Gas column oscillation can be excited byphased vortex shedding or turbulent buffeting. Oscillation normally occurs perpendicular to both thetube axis and flow direction. When the natural acoustic frequency of the shell approaches theexciting frequency of the tubes, a coupling may occur and kinetic energy in the flow stream isconverted into acoustic pressure waves. Acoustic resonance may occur independently ofmechanical tube vibration.

V-12.1 ACOUSTIC FREQUENCY OF SHELL

Acoustic frequency is given by:

.,a=?( pn(PI&j)“” ,cycles/sec

where

w = Distance between reflecting walls measured parallel to segmental baffle cut, inches

p, = Operating shell side pressure, psia

Y = Specific heat ratio of shell side gas, dimensionless

P o = Shell side fluid density at local fluid bulk temperature, Ib/ft 3

pi = Longitudinal pitch, inches (see Figures V-12.2A and V-12.26)

p, = Transverse pitch, inches (see Figures V-12.2A and V-12.28)

d, = Outside diameter of tube, inches. For integrally finned tubes, d, = Fin outerdiameter, inches

i = mode (1, 2, 3, 4)

V-12.2 VORTEX SHEDDING FREQUENCY

The vortex shedding frequency is given by:

12sv.fus = d, cycles/set

where

1/ = Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

S = Strouhal number (see Figures V-12.2A and V-t2.2B)

do = Outside diameter of tube, inches


do = Fin outer diameter, inches



V-f23 TURBULENT BUFFETING FREQUENCY

The turbulent buffeting frequency is given by:

SECTION 6

f,,=~[;1.0,(1-~)‘+0.28] ,cycles/sec

where

d 0 = Outside diameter of tube, inches


d, = Fin outer diameter, inches

a0

x =E!’ do

p 1 = Longtudinal pitch, inches (see Figures V-12.2A and V-12.2B)

pr = Transverse pitch, inches (see Figures V-12.2A and V-12.26)

V = Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

V-12.4 ACOUSTIC RESONANCE

Incidence of acoustic resonance is possible if any one of the following conditions is satisfiedat any operating condition.

V-12.41 CONDITION A PARAMETER

o.Rf”,<f,< 1.2.f”,or

0.8.ft,<I.<1.?f,,

V-12.42 CONDITION B PARAMETER

v>.f”&(~~-0.5)6

V-12.43 CONDITION C PARAMETER

“>j,d,1z.b

and

where

x0=xr for go-tube patterns

x0 = 2x j for 30°, 45”, and 60” tube patterns

.f, = Acoustic frequency, cycles/set (see Paragraph V-12.1)

S = Strouhal number (see Figures V-12.2A and V-12.2B)



R. = Reynolds number, evaluated at the reference cross flow velocity

R,=124.13d,~p,

UP

p = Shellside fluid viscosity, centipoise

V-12.5 CORRECTIVE ACTION

There are several means available to correct a resonant condition, but most could have some effecton exchanger performance. The simplest method is to install deresonating baffle(s) in the exchangerbundle to break the wave(s) at or near the antinode( This can be done without significantlyaffecting the shell side flow pattern. In shell and tube exchangers, the standing wave forms arelimited to the first or the second mode. Failure to check both modes can result in acousticresonance, even with deresonating baffles.

116 Standards Of The Tubular Exchanger Manufacturers Association,q,-,-


FIGURE V-1231STROUHAL NUMBER FOR 90 “TUBE PATTERNS

FLOW

pr/do = 3.0



FIGURE V-12.2BSTROUHAL NUMBER FOR 30 O, 46” AND 60’ TUBE PATTERNS

S


0 . 9

0 . 8

0. 7

0. 6

13

FLOW

f * 2.625PI/do = 3.95

FLOW IN’DUCED VIBRATION

V-13 DESIGN CONSIDERATIONS

SECTlOti 6

Many parameters acting independently or in conjunction with each other can affect the flow inducedvibration analysis. One must be cognizant of these parameters and their effects should beaccounted for in the overall heat exchanger design.

V-13.1 TUBE DIAMETERUse of the largest reasonable tube diameter consistent with practical thermal and hydraulicdesign economics is desirable. Larger diameters increase the moment of inertia, therebyeffectively increasing the sttffness of the tube for a given length.

V-13.2 UNSUPPORTED TUBE SPANThe unsupported tube span is the most significant factor affecting induced vibrations. Theshorter the tube span, the greater its resistance to vibration.The thermal and hydraulic design of an exchanger is significant in determining the type ofshell, baffle design and the unsupported tube length. For example, compared to single passshells, a divided flow shell will result in approximately one-half the span length for an equalcrossflow velocity. TEMA type X shells provide the opportunity to use multiple support platesto reduce the unsupported tube span, without appreciably affecting the crossfiow velocity.Corn ared to the conventional segmental baffle flow arrangement, multi-segmental baffles~sign il?scantly reduce the tube unsupported span for the same shell side Row rate and pressuredrop.“No tubes in window” flow arrangement baffles provide support to all tubes at all bafflelocations and also permit the use of multiple intermediate supports without affecting thecrossflow velocity while reducing the unsupported tube span.

V-13.3 TUBE PITCHLarger pitch-to-tube diameter ratios provide increased ligament areas which result in areduced crossffow velocity for a given unsupported tube span, or a reduced unsupportedtube span for a given crossflow velocity.The increased tube to tube spacing reduces the likelihood of mid-span collision damage andalso decreases the hydrodynamic mass coefficient given in Figure V-7.1 1.

V-13.4 ENTRANCE/EXIT AREASEntrance and exit areas are generally recognized to be particularly susceptible to damage in

vibration prone exchangers.Entrance and exit velocities should be calculated and compared to critical velocities to avoidvibration of the spans in question. It should be noted that compliance with ParagraphRCB-4.62 alone is not enough to insure protection from flow induced vibration at theentrance/exit regions of the bundle.Consideration may be given to the use of partial supports to reduce unsupported tube spansin the entrance/exft regions. Sufficient untubed space may have to be provided at the shellinlet/outlet connections to reduce entrance/exit velocities. Impingement plates should besized and positioned so as not to overly restrict the area available for flow. The use ofdistribution belts can be an affective means of lowering entrance/exit velocities by allowingthe shell side fluid to enter/exit the bundle at several locations.

V-13.5 U-BEND REGIONSSusceptibility of U-bends to damaging vibration may be reduced by optimum location ofadjacent baffles in the straight tube legs and/or use of a s ecial bend support device.Consideration may also be given to protecting the bends f:om Row induced vibration byappropriately locating the shell connection and/or adjacent baffles.

V-13.6TUBlNG MATERIAL AND THICKNESSThe natural frequency of an unsupported tube span is affected by the dastic modulus of thetube. High values of elastic moduli inherent in ferritic steels and austenitic stainless alloysprovide greater resistance to vibratory flexing than materials such as aluminum and brasswith relatively low elastic moduli. Tube metallurgy and wall thickness also affect the dampingcharacteristic of the tube.



V-13.7 BAFFLE THICKNESS AND TUBE HOLE SIZEIncreasing the baffle thickness and reducing the tube-to-baffle hole clearance increases thesystem damping (see Paragraph V-8) and reduces the magnitude of the forces acting on thetube-to-baffle hole interface.

The formulae in this section do not quantitatively account for the effects of increasing thebaffle thickness, or tightening of the baffle hole clearance.

V-13.8 OMISSION OF TUBES

Omission of tubes at predetermined critical locations within the bundle may be employed toreduce vibration potential. For instance, tubes located on baffle cut lines sometimesexperience excessive damage in vibration prone units; therefore, selective removal of tubesalong baffle cut lines may be advantageous.

V-13.9 TUBE AXIAL LOADINGThe heat exchanger designer must recognize the potential adverse impact on vibration bycompressive axial loading of tubes due to pressure and/or temperature conditions. This isparticularly significant for tubes in single pass, fixed tubesheet exchangers where the hot fluidis in the tube side, and in all multiple tube pass fixed tubesheet exchangers. The use of anexpansion joint in such cases may result in reduction of the tube compressive stress. (SeeParagraph V-6.)

V-14 SELECTED REFERENCES

(I) Singh, K. P., and Soler, A. I., “Mechanical Design Of Heat Exchangers And Pressure VesselComponents”, Arcturus Publishers, Cherry Hill, N.J., (1984)

(2) Paidoussis, M. P., “Flow Induced Vibration Of Cylindrical Structures: A Review Of TheState-Of-The-Art”, McGill University, Merl Report No. 82-1 (1982)

(3) Barrington, E. A., “Experience With Acoustic Vibrations In Tubular Exchangers”, ChemicalEngineering Progress, Vol. 69, No. 7 (1973)

(4) Barrington, E. A., “Cure Exchanger Acoustic Vibration”, Hydrocarbon Processing, (July, 1978)

(5) Chen, S. S., and Chung, Ho, “Design Guide For Calculating Hydrodynamic Mass, Part I: CircularCylindrical Structures”, Argonne National Laboratory, Report No. ANL-CT-76-45

Chung, H., and Chen, S. S., “Design Guide For Calculating

Hydrodynamic Mass, Part II:Noncircular Cylindrical Structures’, Ibid, Report No. ANL- T-78-49

(6) ;gdj J. H., “Flow Induced Vibration In A Heat Exchanger With Seal Strips”, ASME HTD, Vol. 9

(7) Chen, S. S., “Flow Induced Vibration Of Circular Cylindrical Structures”, Argonne NationalLaboratory, Report No. ANL-CT-85-51

(8) ~~~~~,‘~ion Of Heat Transfer”; Institution Of Mechanical Engineers, pp

(9) German, Daniel J., “Free Vibration Analysis Of Beams 8 Shafts”, John Wiley&Sons, (1975)

(10) Pettigrew, M.J., Goyder, H.G.D., Qiao, 2. L., Axisa, F., “Damping of Multispan Heat ExchangerTubes”, Part 1: In Gases, Flow-Induced Vibration (1986) ASME PVP Vol. 104, (1986), pp 8187

(11) Pettigrew, M.J., Taylor, C. E., Kim, B.S., “Vibration of Tube Bundles In Two-Phase Cross Flow:Part I -Hydrodynamic Mass and Damping”, 1988 International Symposium on Flow-InducedVibration and Noise -Volume 2, The Pressure Vessel and Piping Division - ASME, pp 79-103

(12) Connors, H.J., “Fluidelastic Vibration Of Tube Arrays Excited By Crossflow”, Flow inducedVibration In Heat Exchangers, ASME, New York (1970)

(13) Chen, S.S., “Design Guide For Calculating The Instability Flow Velocity Of Tube Arrays InCrossRow”, Argonne National Laboratory, ANL-CT-81.40 (1981)

(14) Kissel, Joseph H., “Flow Induced Vibrations In Heat Exchangers-A Practical Look”, Presentedat the 13th National Heat Transfer Conference, Denver (1972)

(15) Moretti, P.M., And Lowery, R.L., “Hydrodynamic Inertia Coefficients For A Tube Surrounded ByRigid Tubes”, ASME paper No. 75-PVR 47, Second National Congress On Pressure Vessel AndPiping, San Francisco

(16) WRC Bulletin 389, dated February 1994



(17) Owen, P.R., “Buffeting Excitation Of Boiler Tube Vibration”, Journal Of Mechanical EngineeringScience, Vol. 7, 1965

(18) Byrce, W.B., Wharmsby, J.S. and Fitzpatrick, J., “Duct Acoustic Resonances Induced By FlowOver Coiled And Rectangular Heat Exchanger Test Banks Of Plain And Finned Tubas”, Proc.BNES International Conference On Vibration In Nuclear Plants, Keswick, U.K. (1978)

(19) Chen, Y.N., “Flow Induced Vibration And Noise In Tube Bank Heat Exchangers Due To VonKarman Streets,” Journal Of Engineering For Industry

(20) API, ‘Technical Data Book _ Petroleum Refining”, 1996


SECTION 7 THERMAL RELATIONS

(Note: This section is not metricated.)

T-l SCOPE AND BASIC RELATIONS

T-l.1 SCOPEThis section outlines the basic thermal relationshiequipment. Included are calculation procedures or determining mean temperature difference andP

s common to most tubular heat transfer

overall heat transfer coefficient, and discussions of the cause and effect of fouling, and proceduresfor determining mean metal temperatures of shell and tubes. Recommendations for the calculationof shell side and tube side heat transfer film coefficients and pressure losses are considered to beoutside rhe scope of these Standards. It should be noted, however, that many of the standard detailsand clearances can significantly affect thermal-hydraulic performance, especially on the shell side.Particularly relevant in this respect is the research conducted bythe University of DelawareEngineering Experiment Station under the joint sponsorship of ASME, API, TEMA, and otherinterested organizations. The results are summarized in their “Bulletin No. 5 (1963) Final Report ofthe Cooperative Research Program on Shell and Tube Exchangers.”

T-l.2 BASIC HEAT TRANSFER RELATION

where

~~ = Required effective outside heat transfer surface, ft2

Q = Total heat to be transferred, BTU/hr

U = Overall heat transfer coefficient, referred to tube outside surface BTU/hr ft2 O F

Al m = Corrected mean temperature difference, 0 F

T-l.3 DETERMINATION OF OVERALL HEAT TRANSFER COEFFICIENT

The overall heat transfer coefficient V, including fouling, shall be calculated as follows:

where

U=

h,=

hi =

To =

ri =

I-,=

Overall heat transfer coefficient (fouled)

Film cbefficient of shell side fluid

Film coefficient of tube side fluid

Fouling resistance on outside surface of tubes

Fouling resistance on inside surface of tubes

Resistance of tube wall referred to outside surface of tube wall, including extended surface ifpresent

124 Standards Of The Tubular Exchanger Manufacturers +sociation

THERMAL RELATIONS SECTION 7

2 = Ratio of outside to inside surface of tubing

E, = Fin efficiency (where applicable)

The units of (/, h D and hi are BTU/hr ft2oFandtheunitsofr.,rjandr,arehrft*oF/BTU

T-l.4 TUBE WALL RESISTANCE

T-1.41 BARE TUBES

T-1.42 INTEGRALLY FINNED TUBES

t [d+ZNw(d+to)]r, = -

where

12k (d-t)

d =

Lo=

t =

N=

k =

OD of bare tube or root diameter if integrally finned, inches

Fin height, inches

Tube wall thickness, inches

Number of fins per inch

Thermal conductivity, BTU/hr ft o F

T-l.5 SELECTED REFERENCE BOOKS

(1) A. P. Fmas and M. N. Ozisik, “Heat Exchanger Design”, John Wiley & Sons, 1965.

(2) M. Jacob, “Heat Transfer”, Vol. 1, John Wiley & Sons, 1949.

(3) D. Q. Kern, “Process Heat Transfer”, McGraw-Hill Book Co., 1950.

(4) J. G. Knudsen and D. L. Katz, “Fluid Dynamics and Heat Transfer”, McGraw-Hill Book Co., 1958.

(5) W. H. McAdams, “Heat Transmission”, McGraw-Hill Book Co., Third Ed., 1954.

(6) Chemical Engineers’ Handbook, McGraw-Hill Book Co., Fifth Ed., 1973.

T-2 FOULING

T-2.1 TYPES OF FOUUNG

Several unique types of fouling mechanisms are currently recognized. They are individuallycomplex, can occur independently or simultaneously, and their rates of development are governed

: by physical and chemical relationships dependent on operating conditions. The major foulingmechanisms are:

Precipitation foulingParticulate fouling

Chemical reaction foulingCorrosion foulingBiological fouling



T-2.2 EFFECTS OF FOULING

The calculation of the overall heat transfer coefficient (see Paragraph T-l .3) contains the terms toaccount for the thermal resistances of the fouling layers on the inside and outside heat transfersurfaces. These fouling layers are known to increase in thickness with time as the heat exchanger isoperated. Fouling layers normally have a lower thermal conductivity than the fluids or the tubematerial, thereby increasing the overall thermal resistance,

In order that heat exchangers shall have sufficient surface to maintain satisfactory performance innormal operation, with reasonable service time between cleanings, it is important in design toprovide a fouling allowance appropriate to the expected operating and maintenance condition,

T-2.3 CONSIDERATIONS IN EVALUATING FOULING RESISTANCE

The determination of appropriate fouling resistance values involves both physical and economicfactors, many of which vary from user to user, even for identical services. When these factors areknown, they can be used to adjust typical base values tabulated in the RGP section of thesestandards.

T-2.31 PHYSICAL CONSIDERATIONS

Typical physical factors influencing the determination of fouling resistances are:

Fluid properties and the propensity for foulingHeat exchanger geometry and orientationSurface and fluid bulk temperaturesLocal fluid velocitiesHeat transfer processFluid treatmentCathodic protection

T-2.32 ECONOMIC CONSIDERATIONS

Typical economic factors influencing the determination of appropriate fouling resistances are:

Frequency and amount of cleaning costsMaintenance costsOperating and production costsLonger periods of time on streamFluid pumping costsDepreciation ratesTax ratesInitial cost and variation with sizeShut down costsOut-of-service costs

T-2.4 DESIGN FOULING RESISTANCESThe best design fouling resistances, chosen with all physical and economic factors properlyevaluated, will result in a minimum cost based on fixed charges of the initial investment (whichincrease with added fouling resistance) and on cleaning and down-time expenses (which decreasewith added fouling resistance). By the very nature of the factors involved, the manufacturer isseldom in a position to determine optimum foulinpast experience and current or projected costs, ?I

resistances. The user, therefore, on the basis ofs

particular services and operating conditions.ould specify the design fouling resistances for his

In the absence of specific data for setting properresistances as described in the previous paragraphs, the user may be guided by the values tabulatedin the RGP section of these standards. In the case of inside surface fouling, these values must bemultiplied by the outside/inside surface ratio, as indicated in Equation T-l .3.

T-3 FLUID TEMPERATURE RELATIONS

,T-3.1 LOGARITHMIC MEAN TEMPERATURE DIFFERENCEFor cases of true countercurrent or cocurrent flow, the logarithmic mean temperature differenceshould be used if the following conditions substantially apply:


THERMAL RELATIONS

Constant overall heat transfer coefficientComplete mixino wlthin any shell cross pass or tube sassThe number of cross baffles is large ’Constant flow rate and specific heatEnthalpy is a linear function of temperatureEqual surface in each shell pass or tube passNegligible heat loss to surroundings or internally between passes

SECTION 7

The followina references contain relevant information on the above items:

(1) K. Gardner and J. Taborek, “Mean Temperature Difference -A Reappraisal”, AlChE Journal,December, 1977

(2) A. N. Caglayan and P. Buthod, “Factors Correct Air-Cooler and S&T Exchanger LMTD”, The Oil& Gas Journal, September 6, 1976

For cases where the above conditions do not apply, a stepwise calculation of temperature differenceand heat transfer surface may be necessary.

Excessive fluid leakage through the clearance between the cross baffles and the shell or between alongitudinal baffle and the shell can significantly alter the axial temperature profile. This conditionmay result in significant degradation of the effective mean temperature difference. The followingreferences may be used for further information on this subject:

(l)~o.F;~N~~ “jup; p;;er, “New Ideas on Heat Exchanger Design”, Hydrocarbon Processing,

(2) J. W. Palen and J. Tabbrek, “Solution of Shellside Flow Pressure Drop and Heat Transfer byStream Analysis”, CEP Symposium No. 92, Vol. 65, 1969

T-3.2 CORRECTION FOR MULTIPASS FLOW

In multipass heat exchangers, where there is a combination of cocurrent and countercurrent flow inalternate passes, the mean temperature difference is less than the logarithmic mean calculated forcountercurrent flow and greater than that based on cocurrent flow. The correct mean temperaturedifference may be evaluated as the product of the logarithmic mean for countercurrent flow and anLMTD correction factor, F. Figures T-3.2A to T3.2M inclusive give values for F as a function of theheat capacity rate ratio R and the required temperature effectiveness P. These charts are based onthe assumption that the conditions listed in Paragraph T-3.1 are applicable. Caution should beobserved when applying F factors from these charts which lie on the steeply sloped portions of thecurves. Such a situation indicates that thermal performance will be extremely sensitive to smallchanges in operating conditions and that performance prediction may be unreliable.

Pass configurations for Figures T-3.2A through T-3.2H are stream symmetric; therefore, t and T maybe taken as the cold and hot fluid temperatures, respectively, regardless of passage through the tubeside or shell side. For non-stream symmetric configurations represented by Figures T-3.21 throughT-3.2M, t and T must be taken as the tube side and the shell side fluid temperatures, respectively.

The following references may be useful in determining values of F for various configurations andconditions.

Confiauration Reference

(1) General W. M. Rohsenow and J. P. Hartnett, “Handbook of HeatTransfer”, McGraw-Hill Book Co., 1972

(2) Three tube passes per shell pass F. K. Fischer, “lnd. Engr. Chem.“, Vol. 30,377 (1936)

(3) Unequal size tube passes K. A. Gardner, “lnd. Engr. Chem.“, Vol. 33, 1215 (1941)

(4) Weighted MTD D. L. Gulley, “Hydrocarbon Proc.“, Vol. 45, 116 (1966)

T-3.3 TEMPERATURE EFFECTIVENESS

The temperature effectiveness of a heat exchanger is customarily defined as the ratio of thetemperature change of the tube side stream to the difference between the two fluid inlettemperatures, thus:



p_ (fZ-tl)CT,-I,)

where Pis the effectiveness. Figures T-3.3A, T-3.3B, and T-3.3C show the temperature effectivenessof counterflow, single-pass shell and two-pass tube, and two-pass shell and four-pass tubeexchangers respectively, in terms of overall heat transfer coefficient, surface, fluid flow rates, andspecific heats.

In all cases, the lower case symbols (t I , t 2, w and c) refer to the tube side fluid, and upper case(7, , T z. W and C )to the shell side fluid. (This distinction is not necessary in the case ofcounterflow exchangers, but confusion will be avoided if it is observed.) These charts are based onthe same conditions listed in Paragraph T-3.1.

T-4 MEAN METALTEMPERATURES OF SHELL AND TUBES

T-4.1 SCOPE

This paragraph outlines the basic method for determination of mean shell and tube metaltemperatures. These temperatures have a pronounced influence in the design of fixed tubesheetexchangers. Knowledge of mean metal temperatures is necessary for determining tubesheetthickness, shell and tube axial stress levels, and flexible shell element requirements. This paragraphprovides the basis for determining the differential thermal expansion term, D L, required for thecalculation of equivalent differential expansion pressure, P.(see Paragraph RCB-7.161).

T-4.2 DEFINITIONS

T-4.21 MEAN METAL TEMPERATURE

The mean metal temperature of either the shell or tubes is the temperature taken at the metalthickness midpoint averaged with respect to the exchanger tube length. For the case ofintegrally finned tubes, the temperature at the prime tube metal thickness midpoint applies.The fin metal temperature should not be weighted with the prime tube metal temperature

T-4.22 FLUID AVERAGE TEMPERATURE

The shell or tube fluid average temperature is the bulk shell or tube fluid temperatureaveraged with respect to the exchanger tube length.

T-4.3 RELATIONSHIP BETWEEN MEAN METAL TEMPERATURES AND FLUID AVERAGETEMPERATURES

T-4.31 SHELL MEAN METAL TEMPERATURE

The shell mean metal temperature, generally assumed to be equal to the shell fluid averagetemperature, is given by:

T,=Y

where

TM = Shell mean metal temperature, O F

5 = Shell fluid average temperature, ’ F

This assumption is valid for cases without abnormal rates of heat transfer between the shelland its surroundings. If significant heat transfer to or from the shell could occur,determination of the effect on the shell metal temperature should be made. In general, mosthigh or low temperature externally insulated exchangers and moderate temperaturenon-insulated exchangers meet the above assumption.



T-4.32 TUBE MEAN METAL TEMPERATURE

The tube mean metal temperature is dependent not only on the tube fluid averagetemperature, but also the shell fluid average temperature, the shell and tube heat transfercoefficients, shell and tube fouling resistances, and tube metal resistance to heat transfer,according to the following relationship:

where

I M = Tube mean metal temperature, Q F

i = Tube side fluid average temperature, O F (see Paragraph T-4.4)

All other terms are as defined by Paragraphs T-l .3 and T-4.31.

T-4.33 TUBESHEET MEAN METAL TEMPERATURE

Untubed portion of tubesheet

7Tr+Ts

T.9 = 2

Tubed portion of tubesheet:

where:

T 1 = Tubeside fluid temperature, O F

T, = Shellside fluid temperature, ’ F

h r = Tubeside heat transfer coefficient, BTU/Hr-ft* - o F

h, = Shellside heat transfer coefficient, BTU/Hr-ft* -’ F

K =

where k = tubesheet metal thermal conductivity, BTU/Hr-ft a F

L = tubesheet thickness, inches

F =1

cosh(K)+ysinh(K)



for triangular pftch

A=ndL/Z

a=0.433PZ-ndZ/8

for square pitch

A=ndl.

d=P'-ndZ/4

where

d = tube ID, inches

P = tube pitch, inches

-.

T-4.4 ESTfMATlON OF SHELL AND TUBE FLUID AVERAGE TEMPERATURESr-z

The methods presented in this paragraph are based on equipment operating under steady-stateconditions.

T-4.41 GENERAL CONSIDERATIONS

Fluid average temperatures in shell and tube heat exchangers are affected by the following:

(1) Shell and tube fluid terminal temperatures

(2) Shell and tube fluid temperature profiles with respect to enthalpy (the followingmethods assume linear profiles)

(3) Variable heat transfer rates with respect to exchanger length (the following methodsassume a constant heat transfer rate through the length of the unit)

(4) He-le~sexchanger geometry, specifically pass configuration, of the shell as well as the

T-4.42 ISOTHERMAL SHELL FLUID/ISOTHERMAL TUBE FLUID, ALL PASS ARRANGEMENTS

T=T,=T,

i=t,=t,

where

T I = Shell side fluid inlet temperature, O F

T z = Shell side fluid outlet temperature, O F

f , =Tube side fluid inlet temperature, ’ F

t 2 =Tube side fluid outlet temperature, o F

T-4.43 ISOTHERMAL SHELL FLUID/LINEAR NONISOTHERMAL TUBE FLUID, ALL PASSARRANGEMENTS

T=T,=Ts

~=TILMTD

,-



T-4.44 LINEAR NONISOTHERMAL SHELL FLUID/ISOTHERMAL TUBE FLUID, ALL PASSARRANGEMENTS

i=t, =t,

?=itLhi’TD

T-4.45 LINEAR NONISOTHERMAL SHELL AND TUBE FLUIDS, TYPE “E” SHELL

The average shell fluid temperature may be determined from the following equation:

The value of ndepends on tube pass geometry and flow direction as given below:

Single pass tubes - cocurrent flow

a=-LM7D,,1t2-t1 I[Td+,]

Single pass tubes - countercurrent flow

For cases where 0.99 < CT,-7.2)

(rz-r,)< 1.01 useT=C.S(T,+T,)

Even number of tube passes

where

L M T D , , = Cocurrent flow L M TD

LMTD,,, = Uncorrected countercurrent flow L M 7 D

t , , t2, T , , 7,. are defined in Paragraph T-4.42

The average tube fluid temperature may then be determined from the following equation:

i=TiLMTD(F’)

where

F = L M T D Correction Factor

T-4.46 OTHER CASES

For cases involving nonlinear temperature-enthalpy profiles and/or pass geometries otherthan those given above, other methods must be used to establish mean metal temperatures.However, with the assumption of constant overall heat transfer rate, the following relatronshtpalways applies:

T-i= *LMTD(F‘)

If one fluid average temperature can be established accurately, knowing the effective meantemperature difference allows the other to be determined.



T-4.5 SELECTION OF THE DESIGN CASE

All foreseeable modes of operation should be considered when specifying the metal temperatures tobe used for calculation of the equivalent differential expansion pressure. Consideration should begiven to the following:

(1) Normal operation, as specified by purchaser, under fouled conditions at the design flow ratesand terminal temperatures

(2) Operation at less than the design fouling allowance (under such conditions, the purchasershould supply details in regard to anticipated operating parameters)

Other operating conditions to which the equipment may be subjected, as specified by the purchaser,may include, but are not necessarily limited to:

(1) Alternate flow rates and/or terminal temperatures as may be the case during start-up, shutdown,variable plant loads., etc.

(2) Flow of a process fluid or clean fluid through one side, but not the other

The largest positive and negative values of equivalent differential expansion pressure generallycorrespond with the cases under which the largest positive and negative differential thermal growthsoccur: an exception being if varying values of material modulii of elasticity alter the comparison.

The differential thermal growth between the shell and tubes is determined as follows:

aL=L,(a,[T,-70]-cx,[t.-70])

where

n L = Differential thermal growth between the shell and tubes, inches

L, =Tube length, face-to-face of tubesheets, inches

a, =Coefficient of thermal expansion of the shell, inches/inch/ o F (see Table D-l 1)

CL r = Coefficient of thermal expansion of the tubes, inches/inch/ D F (see Table D-i 1)

T-4.6 ADDITIONAL CONSIDERATIONS

T-4.61 SERIES ARRANGEMENTS

Individual exchangers in series arrangements are generally subjected to different temperatureconditions. Each individual exchanger should be evaluated separately. Alternately, all couldbe designed for the most severe conditions in the series.

T-4.62 OTHER MODES OF OPERATIONIf fiied tubesheet heat exchangers are to be operated under conditions differing from thosefor which the initial design was checked, it is the purchaser’s responsibility to determine thatsuch operation will not lead to a condition of overstress. This requires a full re-evaluation ofrequired tubesheet thickness, shell and tube longitudinal stresses, tube-to-tubesheet jointloads, and flexible shell elements based on the new operating conditions.


THERMAL RELATIONS

FIGURE T-3.1

CHART FOR SOLVING LMTD FORMULA

LM-,-,, = W-TD - LTD)

where GTTD = Greater Terminal Temperature Difference.LlTD = Lesser Terminal Temperature Difference.

SECTION 7

Greater Terminal Temperature Difference


I/SECTION 7 THERMAL RELATIONS

FIGURE T-32%

-!


SECTION 7


ISECTiON 7 THERMAL RELATIONS

FIGURE T-3.2C


i

0.6

P = TEMPERATURE EFFICIENCYLMTD CORRECTION FACTOR

4 SHELL PASSES 8 OR MULTIPLE OF 8 TUBE PASSES


FIGURE T-3.2E


P s TEMPERATURE EFFICIENCY

L M T O C O R R E C T I O N F A C T O R

t, 6 SHELL PASSES 12 OR MORE EVEN NUMBER OF TUBE PASSES

p.+Z$ ~Jzz8I- I trt1


FIGURE T-3.2G


THERMAL RELATIONS

FIGURE T-3.2H

0 0 0 0


SECTION 7

141


FIGURE T-3.21 0

142

. d d d d


THERMAL RELATIONS

FIGURE T-3.2J

T dMOlWj NOIL33MM03 OlRl :j


SECTION 7

143

1SECTION 7 THERMAL RELATIONS

FIGURE T-3.2K

hlo13wj NOILXlUMO3 am = 3


SECTION 7

.cl

Standards Of The Tubul: Exchanger Manufa&rers Association 145


FIGURE T-3.2M

2 -

c-I-t,8-I-l-r

.0 d d d d


--.

THERMAL RELATIONS

“-7RATUAE EFFICIENCY:w4 nw FYCMANGERS

IEMI-kCOUNTL.. __._ ___.__

P- f,-t,

T,-t,R - WC/WC

See Par.r-3.3

FIGURE T-3.3A

SECTION 7

u - Overall heat transfer coefficienf

A = Total Surface

w = Flow rate of tube fluid

w = Flow rate of shell fluid

c - Specific heat of tube fluid

= Smcific heat of shell fluid

I ,

I I /IllI I

I I III I II

0.1 0.2 0.3 0.4 0.6 0.8 1 2 3 4 5 6 8 10



F

FIGURE T-3.3B

TEMPERATURE EFFICIENCY1 SHELL PASS

EVEN NUMBER OF TUBE PASSES

P= f,-t,~T, -f, See Par. T-3.3

R - wcrwc& Fig. T-3.2A

u - Overall heat transfer coefficient

A - Total surface

u = Flow rate of tube fluid

c - Specific heat of tube fluid

C _ Specific heat of shell fluid

0.7

0.6

0.5

I

0.4

0.3

0.2

0.1

00.1 0.2 0.3 0.4 0.6 0.8 1 2 3 4 5 6 8 ICI

un/wc



FIGURE T-3.3C

TEMPERATURE E!=F,C,EMC” “ “ [ n - T - l - -2 SHELL PASSES

4 OR MULTIPLE OF 4 TUBE

P- f*-i, III I I__ see ParT, -f, & Fia. T.

._

.._

PASSES

T-3.3-3.28

R-WC/WC -

I/ - Overall heat transfer coefficient

A = Total Surfam

w - flow rate of tube fluid

IJ - ROW rate of shell fluid

e - Specific heat of tube fluid

0.7

I I I I

0.4 I-


!SECTION 8 PHYSICAL PROPERTIES OF FLUIDS

(Note: This section is not metric&d)

P-l FLUID DENSITY

p-1.1 SPECIFIC GRAVITY OF LIED P FRACTIONS and saturated light hydrocarbons are shown in

Figure P-l .1.

P-l.2 DENSITY OF ORGANIC LIQUIDSThe general density nomograph Fig. P-l .2 permits the approximation of the density of organic liquidsat temperatures between -150” F and +5OO” F, if densities at two temperatures are known. TableP-l.2 lists the coordinates on the center grid for locating the reference points for 65 compounds.The reference point for a substance may be determined if the density is known for two differenttemperatures. The intersection point of the two straight lines joining the corresponding values of theknown temperatures and densities is the desired reference point of the substance.

P-l.3 COMPRESSIBILITY FACTORS FOR GASES AND VAPORS

The P - u - T relationships for gases and vapors may conveniently be expressed by the equationPv = ZRT, where P is the absolute pressure, ziis the specffic volume, Tis the absolute temperature,R is a constant which may be found by dividing the universal gas constant R by the molecular weightof the gas, and 2 is the compressibility factor. 2 has the value of unity for an ideal gas under allconditions and, therefore, is a measure of the extent of the deviation of a real as or vapor from theideal state. Figures P-l .3A, P-l .3B, P-l .3C are generalized plots of compress, lltiy factor as a?&.

function of reduced pressure, f’ 1 P 0 and reduced temperature, T / 7 C. The dotted curves representconstant values of the pseudo-reduced volume u r ’ = u/( RT,/P,) where the subscript crefers tothe critical value. These may be used to calculate pressure (or temperature) when the temperature(or pressure) and specific volume are known. If Pis expressed in pounds per square inch, zlin cubicfeet per pound, and Tin degrees Rankine, the numerical value of R is 10.73. For critical properlydata. see Paragraph P-6.

P-2 SPECIFIC HEAT

P-2.1 LIQUID PETROLEUM FRACTIONSThe specific heats of Ii uid petroleum fractions of various API gravities are shown as functions oftemperature in Figure 9.2 1. The specific heat versus temperature lines shown apply to virginmid-continent stock and must be corrected for other stocks. An inset curve of this correction factorversus characterization factor is provided.

P-2.2 PETROLEUM VAPORSThe specific heats of petroleum vapors of various characterization factors are shown as functions oftemperature in Figure P-2.2.

P-2.3 PURE HYDROCARBON GASESThe low pressure specific heats of a number of pure hydrocarbons are shown as functions oftemperature in Figures P-2.3A, P-2.36 and P-2.3C.

P-2.4 MISCELLANEOUS LIQUIDS AND GASESThe specific heats of miscellaneous Iialignment charts, Figures P2.4A and8-2.48.

uids and gases at various temperatures may be read from the

P-2.5 GASES AND VAPORS AT ELEVATED PRESSURESSpecific heat data in Figures P-2.2, P-2.3A, P-2.3C and P-2.4B apply only at pressures low enough sothat the specffic heats are not significantly affedad by pressure changes. At higher pr,essures, thespecific heats may be substantially higher than the low pressure values. Figure P-2.5 IS a gr+%alizedchart which may be used to calculate the approximate correcdon to the low pressure speclflc heat


#Y,

,-,

,c---

PHYSICAL PROPERTIES OF FLUIDS SECTION 8

for any gas at high pressure. The isothermal change in molal specific heat, AC, = C, - Cpf isplotted against reduced pressure, P, , with reduced temperature, T, , as a parameter. Outsrde therange of the chart, the following empirical equations are accurate enough for most practicalpurposes. ForT,> 1.2andAC.<2,AC,=5.03Pr/T. 3,forT,< 1.2andAC p < 2.5, AC p = 9 P, IT, ‘. For critical property data, see Paragraph P-6.1 and P-6.2.

P-3 HEAT CONTENT

Heat content of petroleum fractions, including the effect of pressure, are shown as functions of temperatureand API gravity for various UOP K values in Figure P-3.1._The latent heats of vaporization of various liquids may be estimated by the use of Figure P-3.2. Therecommended range of use is indicated for the compounds listed.

See Table P-3.3 for heat capacity ratios for various gases.

P-4 THERMAL CONDUCTIVITY

P-4.1 CONVERSION OF UNITS

Table P-4.1 gives factors for converting thermal conductivity values from one set of units to another.

P-4.2 HYDROCARBON UQUIDS

The thermal conductivities of liquid normal paraffinic hydrocarbons are shown in Figure P-4.2.

P-4.3 MISCELLANEOUS LIQUIDS AND GASES

Tables P-4.3A and P-4.3B give tabulated values of thermal conductivity for a number of liquids andgases at atmospheric pressure.

P-4.4 GASES AND LIQUIDS AT ELEVATED PRESSURES

Thermal conductivity for gases at elevated pressure can be corrected by the use of Figure P-4.4A.Thermal conductivity for liquids at elevated pressure can be corrected by the use of Figure P-4.46.This chart is intended for use above 500 psia and when 71 T, is less than 0.95.

P-5 vlsc0sll-Y

P-5.1 VISCOSITY CONVERSION

A viscosity conversion plot, Figure P-5.1, provides a means of converting viscosity from Saybolt:Redwood or Engler time to kinematic viscosity in centistokes. The absolute viscosity in centiporsesmay be determined by multiplying the kinematic viscosity in centistokes by the specific gravity.Table P-5.1 gives factors for converting Viscosity values to various systems of units.

P-5.2 PETROLEUM OILS

The viscosities of petroleum oils having Watson and Nelson (UOP) characterization factors of 10.0,11.8, 11.8 and 12.5 are shown plotted against temperatures in Figures Pd.2A, P-5.2B, P-5.2C andP-5.2D.

P-5.3 LIQUID PETROLEUM FRACTIONS

Figures P-5.3A and P-5.3B give viscosity data for a number of typical petroleum fractions plotted asstraight lines on ASTM viscosity charts. These charts are so constructed that for any givenpetroleum oil the viscosity-temperature points lie on a straight line. They are, therefore, a convenientmeans for determining the viscosity of a petroleum oil at any temperature, provided vrscosities at twotemperatures are known. Streams of similar API gravity may have widely different viscosltles;therefore, values of viscosity shown here should be considered as typical only.

P-5.4 MISCELLANEOUS LIQUIDS AND GASES

The viscosities of certain liquids are shown as functions of temperature in Figure P-5.4& Theviscosities of certain gases and vapors at one atmosphere pressure are given by Figure P-5.4B,


._

SECTION 8 PHYSICAL PROPERTIES OF FLUIDS

P-S.5 EFFECT OF PRESSURE ON GAS VISCOSITYFigure P-5.5 is a generalized chart which may be used to estimate the viscosities of gases andvapors at elevated pressure if the critical temperature and pressure and the viscosity at low pressureare known. The vrscostty raho, uLp/ pLorm, IS plotted against reduced pressure, I’,,, wrth reducedtemperature, 7, , as a parameter, where, CL .,,and up are respectively the viscosrhes at atmosphericpressure and at pressure P. For critical property data, see Paragraph P-6.

P-6 CRITICAL PROPERTIES

P-6.1 PURE SUBSTANCESTable P-8.1 gives values of the molecular weights, critical temperatures, and critical pressures for avariety of pure compounds. For the calculation of compressibility factor, it is recommended that thecritical pressures and temperatures of hydrogen, helium, and neon be increased by 118 psi and14.4” R respectively.

P-6.2 GAS AND VAPOR MIXTURESFigures P-l .3, P-2.5, and P-5.5 may be used to estimate the properties of gas mixtures as well aspure substances if pseudo-critical properties are used in place of the critical values. Thepseudo-critical temperature and pressure are defined as follows:T p,,,=Y,T,,+Y,T<g+.........+Y"T."

P ..,,=Y,P,,+Y2P.2+.........+YnP~n

;her;Y , , Y 2, etc. are the mole fractions of the individual components and Tr, , T rZ , etc., andrl, <2% etc. are therr cnhcal temperatures and pressures.

P-7 PROPERTIES OF GAS AND VAPOR MIXTURESTo estimate properties of a gas or vapor mixture for which the individual component fractions and propertiesare known, the following formulas may be used:

P-7.1 SPECIFIC HEAT

c,,~(,=x,c,,+x,c,,+ . . . . . . . . . . +x,c,,

P-7.2 THERMAL CONDUCTIVITY

KK,Y,(M,)"3+K*Y2(M2)"3+..,..+KNYN(MN)"3

mix =Y,(M,)"3+Y2(M2)"3+.....+YN(n/lN)"J

CL,Y,(MI)"'+C~~Y*(M~)"~+.....+C~~Y~(MN)"'cl,nix =

YI(1VI,)1'2+Y2(iC12)I'Z+.....+YN(MN)I'2

where, for component “N “:

XN=

YN=M,,=

C&d=KM=

Ir,=

Weight FractionMole FractionMolecular WeightSpecific HeatThermal ConductivityViscosity

152 Stanciards Of The Tubular Exchanger Manufacturers Association


P-8 SELECTED REFERENCES

(1) Reid, R. C. and Sherwood, T. K., “Properties of Gases and Liquids”, 2nd Ed., McGraw-Hilt BookCompany, Inc., New York, 1966.

(2) Comings, E. W., “High Pressure Technology”, McGraw-Hill Book Company, Inc., New York, 1966.(3) Hougen, 0. A., Watson, K. M., Ragatz, R. A., “Chemical Process Principles”, Part 1, 2nd Ed., John

Wiley & Sons, Inc., New York, 1956.(4) Tsederberg, N. V., “Thermal Conductivities of Gases and Liquids”, The M.I.T. Press, Massachusetts

Institute of Technology, Cambridge, Massachusetts, 1965.(5)tY’aT~ C. L., “Physical Properties, Chemical Engineering”, McGraw-Hill Book Company, inc., New York,

(6) Gallant, R. W., “Physical Properties of Hydrocarbons”, Vol. 1 & 2, Gulf Publishing Co., Houston, Texas,1968.


SECTION 8 PHYSICAL PROPERTIESOF FLUIDS

FIGURE P-l.1

154 Standards ~Of The Tubular Exchanger Manufacturers Association


FIGURE P-l.2

GENERAL DENSITY NOMOGAAPH

X AND V VALUES’ FOR DENSITY NOMOGRAPH



FIGURE P-1.3A

I-

d

90

La3

g’ -

%= Z %OKW Allll8lSS3MdYY03

156 Standards Of The Tubular Exchanger Manufacturers Aseociation

PHYSICAL PROPERTIES OF FLUIDS

FIGURE P-1.3B

Z ‘MO13W Alill’diSS3MdP,03


SECTION 8

157


FIGURE P-1.X

1Mx-2 ‘t1013w Allllelss3wwo3



FIGURE P-2.1

SECTION 8

0 ,w 2c.l 300 ml NH) 6W m 800 PW IOGJ 1100 1100

TEMPERATURE 1 DEGREES F.



FIGURE P-2.2

SPECIFIC HEATS OF PETROLEUM FRACTIONS

“~a”Ll I I I I I I I I I I I I I I I I I I I I I I I ! I I I f! !_V! ! !/! I

160 Standarcls Of The Tubular Exchanger Manufacturers Association

I?$

A

13

:-,

”

-.

Sitandards Of The Tubular Exchanger Manufacturers Association


FIGURE P-2.3A

SECTION 8

161

SECTIoN 8 PHYSICAL PROPERTIES OF FLUIDS

FIGURE P-2.38


-




DEG F400

300!200

FIGURE P-2.4A

SPECIFIC HEATS OF LlQUltjS



Deg Fo-

200 -

4 0 0 7

600 -

800 -

1,000 -

I,200 -

1,400 1

1,600 y

1,600 -*

zpoo

FIGURE P-2.46

SPECIFIC HEATS-GASES 1 ATM. C4.0

C= Specifc heot=Etu/(Lb)(DeqF)=Pcu/(Lb)(DeqC)

1.0a9asa7

0.6

320

330

3 4 0

‘,5

;

0.10.09

‘0” 0080.07

a06

005



FIGURE P-2.5

, , , , ( , /

! I II/IIIII illIll

Standards Of,The Tubular Exchanger Manufacturers Association


FIGURE P-3.1

HEAT CONTENT OF PRROLEUM FRACTIONS INCLUDING THE EFFRCT OF PRESSURE



FIGURE P-3.2

LATENT HEATS OF VAPORIZATION OF VARIOUS LIQUIDS

Example:-For water at 212’F. t.-t = 707.212 = 495 and thelatent’heat per lb is 970 Stu

(Latent heat accurate within + 10 per cent)



TABLE P-3.3HEAT CAPACITY RATIOS (C “1 C v)

Acetylene 1.26Air 1.403Ammonia 1.310Argon 1.688Benzene 1.10 (200°F)

Carbon Dioxide 1.304Chlorine 1.355Dichlorodifiouromethane 1.139 (7+F)

Ethane 1.22

Ethyl Alcohol 1.13 (2OOOF)

Ethyl Ether 1.08 (95 o F)

Ethylene 1.255

Helium 1.660 (-292 O F)

Hexane (n-) l.08(176°F)

Hydrogen 1.410Methane 1.31

Methyl Alcohol 1.203 (171 “F)

Nitrogen 1.404

Oxygen 1.401Pentane (n-) 1.086 (189 ’ F)

Sulfur Dioxide 1.29

(All values at 66 0 F and one atmosphere unless otherwise noted)

TABLE P-4.1

THERMAL CONDUCTWY .CONVERSfON FACTORS



FIGURE P-4.2

.12

.I1



FIGURE P-4.3A

THERMAL CONDUCTIVITY OF LIQUIDSk 7 B.t.u./(hr.l(sq. tt.~l”f./fl.l

Liquid

Acetylene .~, ..~ ..,.,.,~.~. ..,.,.,.

A c r y l i c A c i d

Ally1 A l c o h o l

Amy1 A l c o h o l

Aniline ~, ~. ~, ~.

Benzene ., ~, ~.

Bromobenzene

Butyl A l c o h o l (N)

C a r b o n Disulfide ,.,

C a r b o n Tetrachloride

Chlarobenzene _.

Chloroform ..~~.............~.,,,

Cumene ..~......,.

Cyclohexane

Dichlorodifluoramethcme ~.

Ethyl Acetate ..~...,,...,.,......,..,,,.,.

Ethyl A l c o h o l

Ethyl Benzene ~.~..~..~~..~..,.,.....,.,,.,

T. “F k tI Liquid r. “F.

170-220

3232

10032068

21268

21268

30068

32032

39032

320-40

50160300

300-112

88-112212

32390

-100212

32390

40100250-80

5014032

230--4o300

32390

,078 11.093,076 Glycerine ~.,137,069 Heptone (NI .,,057

.066 He&l A l c o h o l,095, 0 9 2 Hexyi A l c o h o l,089,085 Methylethyl-Ketone (MEK),133,089 M e t h y l A l c o h o l (Methenol),085

, 0 8 4 Propy, A l c o h o l USO),072,071.;;;I/ Toluene

,075 V i n y l Acetote,050.069 W a t e r,081,060

,066,063 I!,058,068 (Ortho),065,110,080 Xylem (Meta)080,045


k-

-ii0 .I850 .I32

68 ,11668 ,161

390 ,18150 ,074

300 ,05050 ,072

300 ,04668 ,077

280 ,07168 ,077

250 ,0740 ,069

250 ,067- 2 2 ,132300 ,096

50 ,077300 ,056

50 .076300 ,054

68 ,076176 ,065390 ,047

50 ,0692.50 ,048-40 ,106300 ,072

- 4 0 ,092140 ,075300 ,072

32 ,063390 ,050-40 ,084

86 ,065300 ,046

32 ,088230 ,065

32 343100 ,363200 383300 ,395420 ,376620 ,275

32 ,087176 ,068390 ,048

32 ,080176 ,062390 ,044

171


FIGURE P-4.3B

THERMAL CONDUCTIVITIES OF GASES AND VAPORS[k = BTU/(hrXsq ft)(deg. F per ft)]

Subsiance -328 - 148

Acetone

ZefyleneAmmoniaArgonBeXL.eneButane (n-1Buiane W-1Carbon dioxideCarbon disulfideCarbon monoxideCarbon feirachlorideChlorineChloroformCyclohexaneDichlorodifluoromefhonEthaneEthyl acefafeEfhyl alcoholEfhyl chlorideEthyl etherEthyleneHeliumHeptane (n-1Hexane (n-1HexeneHydrogenHydrogen sulfideMercuryMethaneMethyl acefateMethyl alcoholMethyl chlorideMethylene chlorideNf?OlINitric oxideNitrogenNitrous oxideoxygenPentane (l-l-)Pentane (iso-)PrODaneSulfur dioxideWater vapor.

zero pressure* Value at - 58’ F.+ “al”.3 a* 68” F.

T-

e

.0040

.0037

.0338

.0293

.0040

.0038

T-

.0056

.0091

.0097’

.0063

.0064’

.0088

.0055

.0051

.0612

.0652

.0109

.0089

.0091

.0047

.0091

TEMPER) 9T

.0126

.0095

-t-.0052 .0075.0078

.0040

.0134JO42

.0043

.0038 .0047

.0176

.0059 .oow

fq

URE “F.

212

“0099.0172.0184.0192.0123.0103.0135.0139.0128

.0176

.0052

.0058

.0094

.0080

.0175

.0096

.0124

.0095

.0131

.0161

.0988

.0103

.0109

.1240

.0255

,012s.0094.0063

.0181

.0138

.0188

.0127

.OlSl

.0069

392

.0157

.0224

.0280

.0148.0166

.0177

.0068

.0081

~~.0115

.0150

.0145

.0200

.0112

.1484

.0197

.0358

.0140

.0091

.0220

-LI

.1705

I

.0230 1 .0279


PHYSICAL PROPERTIES OF FLUIDS SECiiON 8

FIGURE P-4.4A

,-I N


m

N


FIGURE P-4.4B

b=k, (2)

h

Where; krhh

0 1 2 3 4 5 6 7 8 9 10 11 12


,?

,->

,-.

*

.-\

,-.,

,-,

,-.

,C?

--i

-.

.7

SECTION 8PHYSICAL PROPERTIES OF FLUIDS

TABLE P-5.1V I S C O S I T Y C O N V E R S I O N F A C T O R S

CsntipDiSeS 1 .oi JO0672 .0000209 2.42 .000102

PI>o,res =- 100 1 .0672 .00209 242 .0102cm-set

lb 1486 14.88 1 .Q311 3600 .I517il.set

ib.rec-F 47900 479 32.2 1 116000 4.88

lb ,413 .00413 .000276 .00000664 i .0000421,,.hr

VISCOSITY CONVERS’lON PLOTENGLER DEGREES

TIME IN SECONDS-SAYBOLT IUNIVERSAL d FUROL), REDWOOD No,. , & P, ENGLER TIME



FIGURE P-5.2A

FIGURE P-5.28

176 6fandards Of The Tubular Exchanger Manufacturers Association


FIGURE P-5.2C

FIGURE P-5.2D

V I S C O S I T Y - T E M P E R A T U R E R E L A T I O N S H I P F O R P E T R O L E U M O I L SLlNrl or CONIIANI DIGllfW /L.P.I. CH*m.CrIIIzITtON WXO”. I = 11.5

Ref: wotson. wien 6 Murphy. Indurtrial 6 Enpineelinq ChemiPfry 28.6054 (L936,

Standaids Of The Tubular Exchanger Manufacturers Association


FIGURE P-5.3B

Standards df The Tubular Exchanger Manufacturers Association

SECTION 8

10 5040

0 -I 3020

-I0 IO

-20 1 -20

O-10

-30

VitCoStfyCenticmiser

ViscosityCentipcixs

0.1

0.09

0.08

0.07

0.06

0.05

0.04

a03

:

-MO

0

0

100

100 200

3 0 0

100

4 0 0

3 0 0

3 0 0 600

700

4 0 0

800

5 0 0 9 0 0

1000500

~~

11001200,

7 0 0 ,5001400

BOO 1500900 1600

1700IO00 le.00

a009 Y)

Q008 >

a007 -I

0 . 0 0 6 -

6005 $


FIGURE P-5.5

HIGH PRESSURE GAS VISCOSITY10

8

6

1.5

10.1 0.2 0.3 0.4 0.5 0.8 1 2 3 4 5 6 8 10

REDUCED PRESSURE - P. =g

~e~rin,ed by permission from Chemical Engineerinq Progress Sympotium Series. St. No. 16. 1955. N. I. Cam. J. D. Parent, and R. E. Peck.

TABLE P-5.1

-T-CRITDCAL PROPERTY DATb

z&zjQy-L

1c


GENERAL INFORMATION SECTION 9

CONTENTS

TITLE

Dimensions of Welded and Seamless Pipe.. ...................................... .....................

Dimensions of Welded Fittings.. ..............................................................................

Dimensions of ASME Standard Flanges.. ................. ..............................................

Bolting Data - Recommended Minimum .................................................................

Metric Bolting Data - Recommended Minimum.. ....................................................

Pressure -Temperature Ratings for Valves, Fittings and Flanges.. ........................

Characteristics of Tubing .........................................................................................

Characteristics of Tubing (Metric) ............................................................................

Hardness Conversion Table.. ...................................................................................

Internal Working Pressures of Tubes At Various Values of Allowable Stress ........

Modulus of Elasticity..............................................................................I...... ~...........

Modulus of Elasticity (Metric). ..................................................................................

Mean Coefficients of Thermal Expansion ................................................................

Mean Coefficients of Thermal Expansion (Metric) ..................................................

Thermal Conductivity of Metals. ...............................................................................

Thermal Conductivity of Metals (Metric) ..................................................................

Weights of Circular Rings and Discs.. ......................................................................

Chord Lengths and Areas of Circular Segments.....................................................

Conversion Factors ..................................................................................................

Conversion Tables for Wire and Sheet Metal Gages.. ............................................

PAGE

184

185

186-187

188

189

1 go-229

230

231

232

233-235

236

237

238

239

240241

242-247

248

249-250

251


SECTION 9 GENERAL INFORMATION

DIMENSIONS OF WELDED AND SEAMLESS PIPE



TAB,6 0.*

DIMENSIONS OF WELDING FITTINGS

r,-L

22

;2

‘2i<

‘?:,’-L

:

i

3%3%3%3%

3%3%3%3%-

:

:

,-

I

t


SECTION’9 GENERAL INFORMATION

DIMENSIONS OF ASME STANDARD FLANGES(All Dimensions in Inches)

THREllOFD FLANGE

LB. FLANGES 300 LB. FLANGES0-r

i

4.F

::$4.24 %

4.24%4.X8.X8%

L

400 LB. FIANGES .N(T

600 LB. FLA

UTA


GENERAL INFC?RMATION SECTION 9

DIMENSIONS OF ASME STANDARD FLANGES

900 LB. FLANGES 1500 LB. FLA ;ES

(1) Bore to match schedule of attachedpipe.

(2) Includes l/16” raised face in 150pound and 300 pound standard.Does not include raised face ‘in 400.600. 900, 1500 and 2500 poundstandard.

(3) Inside pipe diameters are also pro.vided by ihis table.



TABLE D-5

BOLTING DATA - RECOMMENDED MINIMUM

(All Dimensions in inches Unless Noted)

Nut dimensioris are based on American National Standard 818.22Threads C/re National Coarse Se%8 beiow I inch orid eight-pitch fhwa.3 series 1 inch and above



TABLE D-5M

METRIC BOLTING DATA - RECOMMENDED MINIMUM

(All Dimensions in Millimeters Unless Noted)



D-6TABLES FOR

PRESSURE-TEMPERATURE RATINGSFOR VALVES, FITIINGS, AND FLANGES

INTRODUCTORY m,,,.

1. Products used within the jurisdiction of the ASME Boiler and PressureVessel Code and the ASME Standard for pressure piping are subject to themaximum temperature and stress limitations upon the material and piping statedtherein.

2. The ratings at -20 o F to 100 OF, given for the materials covered on pages194 to 229 inclusive, shall also apply at lower temperatures. The ratings for lowtemperature service of the cast and forged materials listed in ASTM A352 andA350 shall be taken the same as the -20 o F to 100 o F ratings for carbon steel onpages 194 to 229 inclusive.

Some of the materials listed in the rating tables undergo a decrease in impactresistance at temperatures lower than -20 ’ F to such an extent as to be unable tosafely resist shock loadings, sudden changes of stress or high stressconcentrations. Therefore, products that are to operate at temperatures below-20 o F shall conform to the rules of the applicable Codes under which they are tobe used.

3. The pressure-temperature ratings in the tables apply to all productscovered by this ASME Standard. Valves conforming to the requirements of thisASME Standard must, in other respects, merit these ratings.

All ratings are the maximum allowable nonshock pressures (psig) at thetabulated temperature degrees F) and may be interpolated between thetemperatures shown. iJhe pnmary service pressure ratings (150,, 300, 400,600,900, 1500,250O) are those at the head of the tables and shown rn bold face type inthe body of the tables.

Temperatures (degrees F) shown in the tables, used in determining theserating tables, were temperatures on the inside of the pressure retaining structure.

The use of these ratings require gaskets conforming to the requirements ofParagraph 5.4 of ASME B16.5(1996). The user is responsible for selecting gasketsof dimensions and materials to withstand the required bolt loading withoutinjurious crushing, and suitable for the service conditions in all other respects.Reference: American Socieby’of Mechanical En ineers Standard Steel Pipe Flanges and FlangedFittings (ASME Standard 816.5-(1996 and 1998 ) reprnted with the permission of The American3Society of Mechanical Engineers, United Engineering Center, 345 E. 47th Street, New York, NY10017. All rights resewed.



TABLE IA LIST OF MATERIAL SPECIFICATIONS

Applicable ASTM Specffics

Forgings castings

A 105 A 216 Or. WCBA 350 Gr. LF2

A 515 Or. 70A 516 Gr. 70A 637 Cl. 1

A 350 Gr. LF6 Cl. 1

A 216 Gr. WCCA 362 Gr. LCC

A 350 Gr. LF6 Cl. 2A 352 Gr. LC2

A 350 Gr. LF3 A 352 Gr. LC3

A 362 Gr. LCB

A 203 Gr. ~6A 203 Gr. E

A 515 Gr. 65A 516 Gr. 65A 203 Gr. AA 203 Gr. D

A 350 Gr. LF, Cl. t

A 182 Gr. Fl A 217 Gr. WC1A 352 Gr. LCl

A 182 Gr. F2A 217 Gr. WC4A 217 Gr. WC5

A 182 Gr. F12 Cl. 2A 217 Gr. WC6

A 182 Gr. F, 1 Cl. 2

A 182 Gr. F22 Cl. 3 A 217 Gr. WCS

A 182 Gr. F5A 182 Gr. F5a A 217 Gr. C5

A 182 Gr. F9 A 217 Gr. Cl2

A 182 Gr. F91 A 217 Gr. C12A

A 182 Gr. F304 A 351 Gr. CF3A 182 Gr. F304H A 351 Gr. CFB

A 182 Gr. F316 A 351 Gr. CF3MA 182 Gr. F316H A 351 Gr. CFBM

A 351 Gr. CGBM

A 515 Gr. 60A 516 Gr. 60

A 204 Gr. AA 204 Gr. 6

A 204 Gr. C

A387Gr.11CI.2

A 387 Or. 22 Cl. 2

A 387 Gr. 91 Cl. 2

A 240 Gr. 304A 240 Gr. 304H

A 240 Gr. 316A 240 Gr. 316HA 240 Gr. 317

A 182 Gr. F304L A 240 Gr. 304LA 182 Gr. F316L A 240 Gr. 316L

A 182 Gr. F321 A 240 Or. 321A 182 Gr. F321H A 240 Gr. 321H

NominalDesignation

C-SiC-Mn-Si

PrOSSUre-TemperatureRating Table

2-1.1

C-Mn-Si -V

C-Mn-Si 2-1.2

C-Mn-Si -V2’/1Ni3’%Ni

C-Si 2-1.3C-Mn-Si2%Ni3’hNi I

MaterialGroup

1.1

1.2

1.3

1.4

1.5

1.7 C-‘&MO 2-1.7‘Kr-%MoNi-%Cr-%Mo%Ni-%Cr-1Mo

lCr-‘&MO Z-l.9i%Cr-%Mol’%Cr-%Mo-Si

2%Cr-IMo 2-1.10

5Cr-‘/~Mo 2-1.13

SCr-1Mc 2-1.14

SCr-lMo-V 2-1.15

18Cr-8Ni 2-2.1

1.9

1.10

1 . 1 3

1.14

1.15

2.1

2.2 16Cr-12Ni-2Mo 2-2.2

18Cr-13Ni-3Mo19Cr-lONi-3Mo

2.3

2.4

Reprinted from ASME 816.5.;996 and 1996, by permission of The American Society of MechanicalEngineers. All rights reserved



TABLE 1A LIST OF MA1 UAL SPECIFICATIONS ICONT’DI

APP!lici-able

F347HOr. F348

A 182 Gr. F348H

2-2.6 A 351 Gr. CH8A 351 Gr. CH20

25Cr-12Ni

I I

2.7 25Cr-20Ni 2-2.7

A 240 Gr. 309sA 240 Gr. 309H

A 240 Gr. 3105A 240 Gr. 310H

A 351 Gr. CK20A 182 Gr. F310

2.8 20Cr-18Ni-6Mo22Cr-5Ni-3Mo-N25Cr-7Ni-OMo-N24Cr-lONi-4Mo-V25Cr-SNi-2Mo-3Cu

25Cr-7Ni-3.5Mo-W-Cb

25Cr-7Ni-3.5Mo-N-Q-W

2-2.8 A 182 Gr. F44A 182 Gr. F51A 182 Gr. F53

A 35, Gr. CK3MCuN A 240 Gr. 531254A 240 Gr. S31803A 240 Gr. 532750

A 351 Or. CEBMNA 38, Gr. CD4MCuA 351 Gr.

CD3MWCuNA 182 Gr. F55 A 240 Gr. 532760

B 463 Gr. NO8020

8 162 Gr. NO2200

6 162 Gr. NO2201

8 127 Gr. NO4400

6 168 Gr. NO6600

8 409 Gr. NO8800

8 333 Gr. Nl0665

8 575 Gr. N102768 443 Gr. NO56258 333 Or. NlOOOl8 434 Gr. N10003B 575 Gr. NO64558 424 Gr. NO8825

B 435 Gr. NO6002

B 482 Gr. NO8020

B 160 Gr. NO2200

B 180 Gr. NO2201

B 564 Gr. NO4400B 164 Gr. NO4405

I

I3.5 72Ni-15Cr-8Fe 2-3.5

3.6 33Ni-42Fe2.1Cr 2-3.6

3.7 65Ni-28Mo-2Fe 2-3.7

3.8 54Ni-16Mo-15Cr 2-3.860Ni-22Cr-SMo-3.5Cb82Ni-28Mo-5Fe70Ni-16Mo-7Cr-5FeGlNi-16Mo-160

42Ni-21.5Cr-3Mo-2.3Cu

B 584 Gr. NO6600

B 584 Gr. NO8800

B 335 Gr. N10665-

B 56-f Gr. N102788 564 Gr. NO6625B 335 Gr. NlOOOlI3 573 Gr. N100036 574 Gr. NO5455B 554 Gr. NO8825

3.9 47Ni-22Cr-9Mo-18Fe 2-3.9

3.10 1 25Ni-46Fe-2lCr-5Mo 1 2-3.10

3.11 44Fe-25Ni-21Cr-MO 2-3.11

3.12 26Ni-43Fe-22Cr-5Mo 2-3.1247Ni-22Cr-ZOFe-7Mo

B 572 Gr. NO6002

B 612 Gr. NO8700

8 649 Gr. NO8904

B 62, Gr. NO83208 581 Gr. NO8985

8 620 Gr. NO8320B 682 Gr. NO8985

Reprinted from ASME 816.5-1596 and 1998, by permission of The American Society of MechanicalEngineers. All rights reserved

Standards Of The Tubular Exchanger Manufacturers Association192


TABLE IA LIST OF MATERIAL SPECIFICATIONS (CONT’D)

Meterisl NominalGroun Desianstion

Pr9SKt”re- Applicable ASTM Specifications’TemperatureI Retina Table Forainar Caninaa Plates

3.13 49Ni-25Cr-IEFe-6Mo Z-3.13 8 581 Gr. NO6975 B 582 Gr. NO6975Ni-Fe-Cr-Mo-Low Cu B 564 Gr. NO8031 8 625 Gr. NO8031

3.14 47Ni-22Cr-19Fe-6Mo 2-3.14 B 581 Gr. NO6007 8 582 Gr. NO6007

3.15 33Ni-@Fe-21Cr 2-3.15 B 564 Gr. NO8810 B 409 Gr. NO8810

3 . 1 6 1 SSNi-19Cr-l%Si 1 2-3.16 1 B 511 Gr. NO8330 1 1 B 536 Gr. NO8330

3.17 29Ni-20.5Cr-3.5Cu-2.5Mo 2-3.17 A 351 Gr. CN7M

GENERAL NOTES:(a) For temperature limitations, see Notes in Table 2.(b) Plate materials are listed only for use as blind flanges (see para. 5.1). Additional plate materials listed in ASME 816.34

may also be used with corresponding 816.34 Standard Class ratings.lc) Material Groups not listed in Table 1A are intended for use in valves. See ASME 816.34.

NOTE:(1) ASME Boiler and Pressure Vessel Code. Section II materials, which also meet the requirements of the listed ASTM speci-

fications, may also be used.

Reprinted from ASME 816.5-1996 and 1998, by permission of The American Society of MechanicalEngineers. All rights resewed



TABLES 2PRESSURE-TEMPERATURE RATINGS FORGROUPS 1.1 THROUGH 3.17 MATERIALS

TABLE 2-1.1 RATINGS FOR GROUP 1.1 MATERIALS

NominalDssignation Forgings Castings Plates

C-Si A 105 (II A 216 Gr. WC6 II) A 516 Gr. 70 11,

C-Mn-Si A 350 Gr. LF2 (11

IA 516 Gr. 70 111121A 537 Cl. 1 (31

C-Mn-Si-V A 350 Gr. LF6 Cl. 1 (41

NOTES:(I) Upon prolonged exposure to temperatures above BOO’F, the carbide phase of steel may be

converted to graohite. Permissible, but not recommended for prolonged use above BOO’F.(21 Not to be used over 86O’F.(3) Not to be used over 700°F.(4)(kn to be used over 5OO*F.

CIOSSTemp., “F

-20 to 100200300400500

600650700750800

850900950

1000


WORKING PRESSURES BY CLASSESL miig

I-I--

150 306

285 740260 675230 655200 635170 600

1401261109580

65503520

650535535505410

270170105

50 I400 500

990900876845800

1480135013151270,200

730715710670550

1095107510651010826

365 535230 345140 20570 105

900 1500

2220 37052025 33751970 3280,900 31701795 2995

1540 2735,610 26851600 2665,510 25201235 2060

805 1340515 860310 515155 2 6 0 I


2500

617056255 4 7 052804990

45604475444042003430

22301430860430


TABLE 2-1.2 RATINGS FOR GROUP 1.2 MATERIALSNominal

Designation Forgings Castings Plates

C-Mn-Si A 215 Gr. WCC (1)A 352 Gr. LCC (2)

C-Mn-Si-V A 350 Gr. LF5 Cl. 2 13)

2’hNi A 352 Gr. LC2 A203Gr. S Ill

3%Ni A 350 Gr. LF3 A 352 Gr. LC3 A 203 Gr. E 111

NOTES:I11 Upon prolonged exposure to temperatures above BOO’F, the carbide phase of steel may be

convened to graphite. Permissible, but not recommended for prolonged use above 900°F.(2) Not to ba used over 650’F.131 Not to be used over MO’F.

ClaSSTemp., 'F

-20 to 100200300400500

600650700750600

650900950

1000

150

290250230200170

14012511095SO

55503620

360

750750730705555

505590570505410

27017010550

i PRESSURE

400

10001000970940885

805765755570550

35523014070

V CLASSES,P ,ig

600 900

1500 22501500 22501465 21651410 21151330 1995

1210 13151175 17551135 17051010 1510625 1235

535345205105

805515310155 T

15w

37503750364035303325

30252940264025202050

,340860515250 T

25M)

62605250607058605540

5040.4905473042003430

22301430

650430

Reprinted from ASME 816.6.1996 and 1996, by permission of The American Society of MechanicalEngineers. All rights reserved


SECTION 9

NominalDssignation Forgings Castings Plats

c-si A 352 Gr. LCB (3) A 515 Gr. 65 (1)

C-Mn-Si A 516 Gr. 65 (1)121

2’/ZNi A 203 Gr. A Ill

3%Ni A 203 Gr. D (1)

NOTES:(I) Upon prolonged exposure to temperatures above 800°F. the carbide phase of steel “-,a” be

convened to graphite. Permissible, but not recommended for prolonged use abc ,ve 800°F.(21 Not to be used over 850°F.(3) Not to be used we, 650°F.

CISSTemp., ‘F

-20 to 100200300400600

265250230200170

600 140660 125700750600

850900950

1000

1109560

535 710 ,065 1600 2666 4440525 695 1045 1570 2615 4365520 690 1035 1555 2590 4320475 630 945 1420 2365 3945390 520 760 1175 1955 3260

66 27050 17035 105

2 0 50

WORKI NO PRESSURES BY CIASSE! ;. OS ;ig

695655640620585


400 600

13901315127512351165

850825775

900 1500 2500

2085 3470 57851970 3260 54701915 3190 53151650 3085 51451745 2910 4850

35523014070

535 805 1340 2230345 515 860 1430205 310 515 860105 155 260 430

Reprinted from ASME 816.51996 and 1996. by permission 01 The American Society of MechanicalEngineers. All rights reserved



NominalDesignation Forgings Castings Plates

C-Si A 515 G,. 60 (I)

C-Mn-Si A 350 Gr. LFI, Cl. 1 (1) A 516 Gr. 60 [l)(2)

NOTES:11) Upon prolonged exposure to temperatures above BOO”F, the carbide phase of steel may be

convened to graphite. Permissible, but not recommended for prolonged use above 800°F.(2) Not to ba used over 65O’F.

ChSSTarno.. ‘F

WORKING

150 l-=300

-20 tcl 100200300400500

235215210200170

600 140650 125700 110760 95800 60

850900

65503520

950'1000 I

620 825 1236560 750. 1125550 730 1095530 705 1060500 665 995

455 610450 600450 600445 590370 495

916695895885740

535345206105

2701701 0 550

PRESSURt

400

366230140

70

-is 6:V CLt,SSES

600

-;. PS

I

i9

900 1500

1850 30851665 28101640 27351585 26451495 2490

1370134513451325ItlO

805615310155

22852245224522101850

1340860515260

Reprinted from ASME 816.51996 and 1998, by permission of The American Society of MechanicalEngineers. All rights resewed

IStandards Of The Tubular Exchanger Manufacturers Association

2500

51454680456044054150

38053740374036853085

22301430

860430

197



NominalDesignation Forgings castings PlIlteS

C-‘/&IO A 182 Gr. Fl (1) A 217 Gr. WC1 il)l2l A 204 Gr. A 11)A 352 Gr. LCl (3) A 204 Gr. B (1)

NOTES:(1) Upon prolonged exp~~uretotemperatures above 875-F. the carbide phase ofcarbon-molyb-

denum steel may be converted to graphite. Permissible, but not recommended for prolongeduse above 875’F.

(2) Use normalized and tempered material only.(3) Not to be used over 65O’F.

CIOSSTamp., ‘F

-r

150 300 400 600 900

-20 to loo200300400500

265 695 925 1390 2085260 680 905 1360 2035230 655 670 1305 ,956200 640 855 1280 1920170 620 830 1245 1865

600 140 605 805 ,210 1815650 125 590 785 1175 1765700 110 570 755 1135 1705750 95 530 710 1065 1595800 80 510 675 1015 ,826

850 66 485 650 975 1460900 50 450 600 900 1350950 35 280 375 560 845

1000 20 165 220 330 495

198

ES iIY CLASSES. m

I1500 2500

3470 57853395 56503260 54353200 53303105 5180

3025 50402940 4905

‘~‘2840 47302660 44302540 4230

2435 40602245 3745,406 2345825 1370

Reprinted from ASME 816.6-1996 and 1998, by permission of The American Society of MechanicalEngineers. All rights resenred




NominslDerignation Forgings Castings Plates

C-%Mo A 204 Gr. C (1)

‘Xr-%Mo A 182 Or. FZ (31

Ni-%Cr-%Mo A 217 Gr. WC4 L?)(3)

3/nNi-3/&r-1Mo A 217 Gr. WC5 12)

NOTES:(11 Upon prolonged exposure to temperatures above 875°F. the carbide phase of carbon-molyb-

denum steel may be convertedto graphite. Permissible, but not recommended for prolonged“se above 875°F.

12) Use normalized and tempered material only.(3) Not to be used over 1000°F.

-20 to 100200300400500

600660700750800

850900950

10001050

150

260230200170

1401251109580

65503520

WORKI

300

750750720695665

605590570530510

485450315200160

ING

1PRESSURE V CLASSES .pcdg

400 600 900 1500 2500

10001000965925885

805785756710675

650600420270210

1500144513851330

,2101175113510651015

9 7 590063040531;

2250 3760 62502250 3750 62502165 3610 60152080 3465 57751995 3325 5640

1815 3025 50401765 2940 49051705 2840 47301595 2660 44301525 2640 4230

14601350945605475

2436224516751010790

40603745263016851315

Reprinted from ASME 816.51996 and 1998, by permission of The American Society of MechanicalEngineers. All rights resewed





lCr-‘/zMo A 182 Gr. F12 Cl. 2 (l)(Z)

l’/&r-‘&MO A 217 Gr. WC6 l1)(31

l’/&r-%Mo A 162 Gr. Fll Cl. 2 (l)(Z) A 367 Gr. 11 Cl. 2 (21

NOTES:(I) Use normalized and tempered material only.(2) Permissible, but not recommended for prolonged use above 1 lOO*F.(3, Not to be used over 1 IOWF.

CkSSTemp., “F

-20 to 100200300400500

600650700750800

850900950

,0001050

110011501200


150 300 400 600 so0 1500 2500

290 750 1000 1500 2250 3750 6250260 750 1000 1500 2250 3760 6250230 720 965 1445 2165 3610 6015200 695 925 1385 2080 3465 5775170 665 886 1330 1995 3325 5640

1401251109580

65503520

.

605 805 ,210 1815 3025 5040690 765 ,176 ,766 2940 4905670 755 1135 1705 2640 4730530 710 1065 1595 2660 4430510 675 1015 1525 2540 4230

485450320215146

650 975600 900425 640290 430190 290

2435 40602245 37451595 26551060 1600720 1200

9560

130 19080 12550 75

14601350955660430

290186115

460310190

600515315

PRESSURE I CLASSES, is

Reprinted from ASME 816.51996 and 1998, by permission of The American Society of MechanicalEngineers. All righk reserved

GENERAL INFdiiMATlON SECTION 9


Designation Forgings Castings Plate*

Z’/,Cr-1Mo A 182 Gr. F22 Cl. 3 (2, A 217 Gr. WC9 (l)(3) A 387 Gr. 22 Cl. 2 (2)

NOTES:il t Use normalized and tempered material only.(21 Permissible, but not recommended for brolonged use above 11OO’F.(3) Not to be used over 11OO’F.

ClOSSTemp., ‘F

-20 *o 100200300400500

600650700750800

850900950

10001050

1100 110 145 220 330 550 915,150 70 90 135 205 345 5701200 40 55 80 125 205 345

150 300 400

290260230200170

750750730705665

10001000970940885

140 605 805125 590 785110 570 75595 530 71080 510 675

65 485 65050 450 60035 375 50520 260 345

175 235

PRESSURE SE:Y CLASSES,

600

15001500145514101330

1210117511351065,015

975900

520350

i9

900

2250 3750 62502250 3750 62502185 3640 60702115 3530 58801995 3325 5540

,815 3025 50401765 2940 49051705 2840 47301595 2660 44301525 2540 4230

1460 2435 40601350 2245 37451130 1885 ,3145780 1305 2170525 875 1455

1500

Reprinted from ASME 816.5-1998 and 1998, by permission of The American Society of MechanicalEngineers. All rights resarwd





lGCr-VNi-ZMo A 182 Gr.F316 (1) A351 Gr.CF3M (21 A240 Gr.316lllAl82 Gr.F316H A351 Gr.CFBM 11) A 240Gr.316H

18Cr-13Ni-3Mo A 240 Gr.317 (1)

19Cr-lONi-3Mo A351Gr.CGBM 131

NOTES:(II Attfxnperaturos over lOOO"F.use onlywhenthe carbon contentis0.04% or higher.I21 Not to be used over850PF.(31 Nat to be used over 1000°F.

ClC3rJTemp.,'F 150 300 400 600 900 1500 2500

-2oto 100 275 720 960 1440 2160 3600 6000200 235 620 825 1240 1860 3095 5160300 216 560 745 1120 1680 2795 4660400 195 515 685 1025 1540 2570 4280600 170 480 635 955 1436 2390 3980

600 140 450 600 900 1365 2255 3760650 125 445 590 890 ,330 2220 3700700 110 430 680 870 1305 2170 3620750 95 425 570 855 1280 2135 3660800 80 420 565 845 1265 2110 3520

850 65 420 555 835 1255 2090 3480900 50 415 555 830 1245 2075 3460950 35 385 515 775 1160 1930 32201000 20 350 465 700 1050 1750 29151050 345 460 685 1030 1720 2866

11001150120012501300

. . .

. . .

.

. . .

305 405 610 915 1525 2546235 315 475 7 1 0 1185 1970185 245 370 555 925 1545145 195 295 440 735 1230115 155 235 350 585 970

1350140014501500

95 130 190 290 480, 80075 100 150 225 380 63060 80 115 175 290 48540 56 85 125 205 345

WORKI NG PRESSURESSYIXASSES . D!iig

Reprintedfrom ASME E16.~1996and199B,bypermissionofTheAmerican Societyof MechanicalEngineers. Allrightsre&xved



TABLE Z-2.3 RATINGS FGR GROUP 2.3 MATERIALSNominal

Designation Forgings I CI16titlllS I Plates

16Cr-12Ni-2Mo A 182 Gr. F316L I A 240 Gr. 3161

18Cr-8Ni A 182 Gr. F304L 11) A 240 Gr. 304L (1)

NOTE:111 Not to be used over 600°F.

W O R K I N G PRESSURf BY CLASSES rig

I150 3 0 0 4 0 0 600 900 1500

-20 to 1002 0 03 0 04 0 0600

230 600 8 0 0195 505 675176 4 5 6 605160 4 1 5 550145 3 8 0 510

120010159108257 6 6

18001520136012401145

30002530227020651910

140 3 6 0 4 8 0125 3 6 0 470110 3 4 6 4 6 09 5 3 3 5 4 5 08 0 3 3 0 440

720700685670660

1080106010301010985

18001750171516801645

6 5 320 430 6 4 5

‘, P!

I 965 I 1610

Temp., “F 2 5 0 0

5 0 0 04 2 2 03 7 8 03 4 4 03 1 8 0

6 0 06 5 07 0 07 5 08 0 0

3 0 0 02 9 2 028602 8 0 02740

8 5 0 2 6 6 0






18Cr-IONi-Ti A 192 Gr.F321(2) A240Gr.321lZlA 182Gr. F321H (1) A240Gr.321H (1)

NOTES:(11 At temperatures overlOOO'F,useonlyifthe materialisheattreated byheatingtoa minimum

temperature of2000'F.12) Notto be usedoverlOOO"F.

CISSSTemp., 'F 150 300 400 600 cm0 1500 2500

-2oto 100 275 720 960 1440 2160 3600 6000200 245 645 860 1290 1935 3230 6380300 230 595 795 1190 1785 2975 4960400 200 550 733 1105 1655 2760 46005 w 170 515 685 1030 1545 2 5 7 0 4285

600 140 485 650 975 1480 2435 4060650 125 480 635 955 1435 2390 3980700 110 465 620 930 1395 2330 3880750 95 460 610 915 1375 2290 3820800 80 450 600 900 1355 2255 3760

850 65 445 695 895 1340 2230 3720900 50 440 590 885 1325 2210 3680950 35 385 515 775 1160 1930 32201000 20 355 475 715 1070 1785 29701060 315 415 625 940 1565 2605

11001150120012501300

. .

. .

. . .

. . .

..,

.

270 360 545 815 1360 2266235 315 475 710 1185 1970185 245 370 555 925 1545140 185 280 4 2 0 705 ,170110 145 220 330 550 916

1350140014501500

85 115 170 255 430 71565 86 130 195 325 54550 70 105 155 255 43040 50 75 115 190 315

WORKI NG PRESSURESSYCLASSES , P! ;ig

Reprintedfrom ASME1996and 1998, bypermissionofTheAmerican Societyof MechanicalEngineers. AlI rights resewad

208 Standards of The Tubular Exchanger Manufacturers Association



NominalDesignation Forgings castings PI*te*

18Cr-lONi-Cb A 162 Gr. F347 (2) A 351 Gr. CFBC 131 A 240 Gr. 347 (2)A 182 Gr. F347H (1) A 240 Gr. 347H (1)A 182 Gr. F346 (2) A 240 Gr. 348 (2)A 162 Gr. F348H (11 A 240 Gr. 348H (1)

NOTES:(1) For temperatures over 1000°F. use only if the material is heat treated by heating to a minimum

temperature of 2000°F.(2) Not to be used over 1000°F.(3) At temperatures over 1000°F. use the material only when the carbon content is 0.04% or higher.

CIESSTam,,., ‘F

-20 to 1002 0 03 0 04 0 05 0 0

6 0 06 5 07 0 07 5 08 0 0

8 5 09 0 09 5 0

1 0 0 01050

1100,150, 2 0 012501300

135014001450,600

150 300 600

275 720 960 1440 2160265 660 860 1320 1960230 615 8 2 0 1230 1645200 575 765 1145 1720170 540 720 1060 1620

1401251109 580

6 5503 52 0

515 865 , 0 2 5 1640505 670 1010 1610495 660 990 1465490 655 965 1475485 650 976 1460

485 645 970 1455 2426 4 0 4 0450 600 900 1350 2246 3 7 4 5385 515 776 1160 ,930 3 2 2 0365 4 6 5 7 2 5 1090 1820 3 0 3 0360 4 6 0 720 1080 1800 kOo0

325 4 3 0 645 965 ,610 2 6 8 5275 365 550 625 1370 2 2 8 5170 230 345 515 655 1430125 165 245 370 615 103095 125 165 2 8 0 465 7 7 0

70 9 0 135 20565 7 5 110 1654 0 55 80. 12535 4 6 7 0 105

WORKI

-NG’PRESSURES BY CLASSES;. Ds i9

1500

3 3 0 03 0 7 028702700

2 5 7 02520247024602435

345275205170

4 7 8 04 5 0 0

4 2 8 04 2 0 04 1 2 04 1 0 04 0 6 0

5704 5 53 4 5

Reprinted from ASME 816.51996 and 1996, by permission of The American Society of MechanicalEngineers. All rights reserved





23Cr-12Ni A 240 Gr. 309s (l)l2)(3)A 240 Gr. 309H

ZSCr-12Ni A 351 Gr. CH8 (11A 351 Gr. CH20 (1)

NOTES:(1) At temperatures war 1OOVF. use only when the carbon content is 0.04% or higher.1.2) For temperatures above 1OOO’F. use only if the material solution is heat treated to the minimum

temperature specified in the specification but not lower than 1900°F. and quenching in wateror rapidly cooling by other msans.

(3) This material should be used for service temperatures 1050°F and above only when assuranceis provided that grain size is not finer than ASTM 6.

CbSSTemp.. ‘F 150 3 0 0

PRESSURE

4 0 0 6 0 0

is

900 1500

-20 to 100 260 6 7 0 896 1345 2015 33602 0 0 230 6 0 5 805 1210 1615 30253 0 0 220 570 760 1140 1705 26454 0 0 200 535 710 1065 1600 26655 0 0 170 505 670 1010 1510 2 6 2 0

6 0 0 140 480 635 955 14356 5 0 125 4 6 5 620 930 13957 0 0 110 4 6 5 610 9 1 0 13707 5 0 9 5 4 4 5 695 895 13408 0 0 80 435 580 8 7 0 1306

23902330228022302170

8 5 0 6 5 4 2 5 585 8 5 0 12759 0 0 50 415 555 6 3 0 12459 5 0 3 6 365 616 77s 1160

1000 2 0 335 4 5 0 670 10101050 290 390 585 875

. . .

. . .

225 3 0 0 4 4 5 670170 230 3 4 5 515130 175 260 3 9 0100 135 2 0 0 300

8 0 105 160 235

6 0 8 0 115 1764 5 6 0 9 0 1353 0 4 0 6 0 952 5 3 0 5 0 70..I

L

WORK6 Y CLASSES

21262075193016801460

,116860650495395

290225155120

2500

50404 7 4 04 4 4 04 2 0 0

3 9 8 03 8 8 03 8 0 03 7 2 03 6 2 0

35403 4 6 03 2 2 028002 4 3 0

186014301065

8 3 06 6 0

4 8 53 7 02 6 0

Reprinted from ASME 816.5-IS96 and 1998. by permission of The American Society of MechanicalEngineers. All rights reserved

210 Standards’Of The Tubular Exchanger Manufacturers Association



NominalDssianation Foraines Castinas Plates

25Cr-20Ni A 162 Gr. F310 (l)(3) A351 Gr.CK20ill A 240 Gr.3105 11)(2)13)A xnn, 31oi.l

I I _ _ _ _ -.

NOTES:11) At temperatures over 1OOO'F. we only when the carbon content is 0.04% or higher.(2) For temperatures above 1OOO'F. use only if the material is hear treated by heating it to a

temperature of at least 19OO'F and quenching in water or rapidly cooling by other means.(31 Service temperatures of1050°F and above should be used onlywhen assurance is provided

that grain size is not finer than ASTM 6.

CbSTemp.,'F

NO7-

150 300 400 600 900 1500

-2ota 100 260 670 895 1345200 235 605 610 1215300 220 570 760 1140400 200 535 715 1070500 170 505 675 1015

20151920170516051520

3360 56003035 50602645 47402675 44602530 4220

600 140 460 6dO 960 1440 2400 4000650 125 470 625 935 1405 2340 3900700 110 455 610 910 1370 2280 3800750 95 450 600 900 1345 2245 3740600 90 435 580 875 1310 2185 3640

650 65 425 570 655 1280 2135 3560900 50 420 555 835 1255 2090 3480950 35 365 515 775 1160 1930 32201000 20 345 460 685 1030 1720 26651050 I 335 450 670 1010 1660 2800

1100115012001250

. . .,

,,

..,

. . .

260 345 520 780 1305 2170190 250 375 565 945 157013s 185 275 410 665 1145105 135 205 310 515 85575 100 150 225 375 630

135014001460

WORKli

60 60 115 175 290 40545 60 90 135 225 37035 45 65 100 165 27525 35 50 75 130 215

PRESSURE 53 8YClASSES.p! iig

RsprimedfromASME816.5-1996and 1998,bypermissionofTheAmerican Societyof MechanicalEngineers. All rights resewed

Standards Of The Tubulai Exchanger Manufacturers Association 211


TABLE Z-2.8 RATINGS FOR GROUP 2.8 MATERIALSNominal


ZOCr-18Ni-6Mo A 182 Gr. F44 A 361 Gr. CKJMCuN A 240 Gr. 531254

2X2-5Ni-3Mo-N A 182 Gr. F51 (11 A 240 Gr. 531803 Ill

25Cr-7Ni-4Mo-N A 192 Gr. F53 IIt A 240 Gr. 532750 ill

24Cr-lONi-OMo-V A 351 Gr. CEEMN (1)

25Cr-5Ni-2Mo-3Cu A 351 Gr. CD4MCu (1)

25Cr-7Ni-3.5Mo-W-Cb A 351 Gr. CDSMWCuN Ill

25Cr-7Ni-3.5Mo-N-Cu-W A 182 Gr. F55 0) A 240 Gr. 532760 11)

NOTE:(1) This steel may become brittle after service at moderately elevated temperatures. Not to be

used over 6OO’F.


WDRKI

300

750720665615575

555550540530

i PRESSURE

460

1000 ,150O9 6 0 1440885 1330820 1230770 1150

740735725710

,116 1670 27851100 1650 27501085 1625 27101065 1595 2660

Y CLASSES, prig

I I600, I 900 I 1500

2160199518451730

37503600332530702980

Reprinted from ASME 616.51996 and 1999, by permission of The American Society Of MechanicalEngineers. Alkiphts reserved

2500

62506000554051204600

4640458045204430




35Ni-35Fe-ZOCr-Cb B 462 Cr. NO8020 (1) B 463 Gr. NO8020 (1)

NOTE:Ill Use annealed material only.

6iD 125700 110160 95800 80

WORKING PRESSURES BY CLASSES

I

290260230200170

140

=--F-750720715675655

1000960950900875

606590570530510

8057857557106 7 5 L

600

15001440142513451310

12101175113510651015

900 1500

2250 37502160 36002140 35652020 33651965 3275

1815 30251765 29401705 28401595 26601525 2540 I

2500

62506000594056105460

60404905473044304230

RBplinted from ASME 816.5-1996 and 1998, by permission of The American Society of MechanicalEngineers. All rights reserved


SECTION 9



99.ONi 8 160 Gr. NO2200 ll)t21 B 162 Gr. NO2200 111

NOTES:(11 Use annealed material only.(21 The chemical composition. mechanical properties, heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturingprocedures. tolerances, tests, certification, and markings shall be in accordance withASTM 8 564.

WORKING PRESSURES BY CLASSES, prig

Cl.%%temp., “F 150 a00 400 600 900 1500

-20 to 100 140 360 480 720 1080 1800200 140 360 480 720 1080 1800300 140 360 480 720 1080 1800‘loo 140 360 480 720 1080 1800500 140 360 480 720 1080 1800

600 140 360 480 720 1080 1800

2500

30003000300030003000

3000


Reprinted from ASME B16.51695 and 1998. by permission of The American Society of MechanicalEngineers. All rights resewed

GENERAL INFORMATION


NominalDesignation Forgings Castings Plate5

SS.ONi-Low C B 160 Gr. NO2201 l1112l 6 162 Gr.NO2201lll

NOTES:ill Use annealed material only.121 The chemical composition, mechanical properties, heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturingprocedures, tolerances, tests, certification, and markings shall be in accordance withASTMB564.

SECTION 9

ClassTsmD.. 'F

-20 to 100200300400500

600650700750800

850900950

10001050

110011601200

150

SO 240 320 480 720 1200 200086 230 305 a55 685 ,140 190085 225 300 445 670 1115 186085 215 290 430 650 1080 180085 215 290 430 650 1080 1800

8585858080

215 230 430 650 1090 1800216 290 430 650 1080 1800215 290 430 650 1080 1800210 280 420 635 1055 1760205 270 410 610 1020 1700

503520

6045

WORKI

300

2051401153575

35

NO PRESSURI3 EIYCIASSEZ iig

499

270 410 610185 280 415150 230 345125 185 280100 150 220

1020695570465370

17001155,950770615

80 125 185 310 51660 95 140 230 38550 75 110 185 310

600 900 1500 2500

ReprintedfromASME816.5-1996and 1998,bypermissionofTheAm.ricanSocietyofMeohani~lEngineers. Wrights resewed




NominalDesignation Forgings Castings PIatE%

67Ni-30Cu B 564 Gr. NO4400 (1, B 127 Gr. NOMOO Ill

67Ni-30Cu-S B 164 Gr. NO4405 (l)(Z)

NOTES:(1) Use annealed material only.I21 The chemical composition, mechanical properties. heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturingprocedures, tolerances, tests, certification. and markings shall be in accordance with ASTMB 564.

NG

ISt

i

, PC

i

WORKII

300

PRESSURE

400

IY CLASSES

600

iig

900

I I IClass

Temn.. ‘F 150

-20 to 100200

50004400412039803960

39603960396039003820

28302055

230200190185170

1401251109680

6650

600530496480475

476476475470460

340248

800705660635635

635635635625610

455330

18001585148514351435

14351435143514051375

1020740

12001055990955950

950950950935915

680495

26402470300

400500

600650700750800

850900

23902375

23752375237523402290

16951 2 3 5

Reprinted from ASME 816.5.1996 and 1996, by permission of The American Society Of MechanicalEngineers. All rights resewed


GENERAL INFORMATlbN SECTION 9



72Ni-15Cr-8Fe B 564 Gr. NO6600 I,) B 166 Gr. NO6600 Ill

NOTE:

ClfiSSTemp., ‘F 150 300 400 600 1500

-20 to 100 290 750 1000 1500 2250 3750 62502 0 0 260 750 1000 1500 2250 3750 6 2 5 0300 230 730 970 1465 2185 3640 6 0 7 04 0 0 200 705 940 1410 2115 3530 5680500 170 665 885 1330 1995 3325 5 5 4 0

6 0 0 140 605 805 1210 1815 3025 5 0 4 0650 125 590 785 1175 1765 2 9 4 0 4 9 0 57 0 0 110 570 755 1135 1705 2840 4 7 3 07 5 0 9 5 530 7 1 0 1065 1595 2660 4 4 3 0800 80 510 675 1015 1520 2540 4 2 3 0

8 5 0 6 59 0 0 50

9 5 0 35, 0 0 0 201050

465450325215140

9 57 060

6 5 0 975 1460600 900 1350435 656 980290 430 650185 260 415

2435 4 0 6 02245 3 7 4 516351080695

2 7 2 61800

11001150

WORKI i PRESSURE ,Y CLASSES ig

1259 080

185 280 465 7 7 0135 205 340 565125 185 310 615

RBprintad from ASME B16.51996 and 1998. by permission of The American Society of MechanicalEngineers. All riehts reserved





33Ni-42Fe-210 S 554 Gr. NO5500 (1) 8409 Gr. NO5500 (1)

NOTE:(1) Use annealed material only.

CbSSTemp., 'F

-20 to 100200300$00500

500550700750800

55030095010001050

1100115012001250,300

13501400,4501500


150

275 720 950 1440 2150 3500 5000255 550 855 1325 1990 3310 5520230 525 830 1250 1570 3120 5200200 500 800 1200 1500 3000 5000170 550 770 1155 1735 2590 4520

14012511095SO

55503520

.

.

575 755 1145 1720 2570 4750570 750 1140 1705 2045 4740555 750 1130 1590 2520 4700530 i 710 1055 1595 2550 4430505 575 1015 1520 2535 4230

455 550 975 1450 2435 4050450 500 900 1350 2245 3745395 515 775 1150 1930 3220355 455 725 1090 1520 3030350 450 720 1050 1500 3000

325 430275 355205 270130 17550 80

955 1510 2 5 5 5825 1370 2285510 1020 1595390 550 1050155 310 515

50353025

55454035

545550405250125

100705050

150 245 410100 170 28595 155 25575 125 205

WORKINGiPRESSURE! :YCLASSES

300 450 500

Reprinted from ASME 816.5-1996 and 1998,by permission of The American Society of MechanicalEngineers. All rights reserved


TABLE Z-3.8 RATINGS FOR GROUP 3.8 MATERIALS

NominalDesignation Forgings Castings PIlater

54Ni-16Mo-15Cr B 584 Gr. N10276 llI(41 B 575 Gr. NlOZ76 (l)(4)

60Ni-2ZCr-9Mo-3.5Cb B 564 Gr. NO6625 l3)(5) B 443 Gr. NO6625 (3)15)

62Ni-28Mo-5Fe B 335 Gr. NlOOOl (1)(21(6l B 333 Gr. NlOOOl 0)(61

70Ni-16Mo-7Cr-5Fe B 573 Or. N10003 (2)(3l B 434 Gr. N10003 (3)

6lNi-16Mo-16Cr B 674 Gr. NO6455 (1)12116) B 575 Or. NOM55 (l)wl

42Ni-21.5Fe-3Cr-2.3Cu B 664 Gr. NO8825 (3)(7) 8 424 Gr. NO8825 (3)(7l

NOTES:(1) Use solution annealed material only.(21 The chemical composition, mechanical properties, heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturingprocedures, tolerances, tests, certification, and markings shall be in accordance withASTM B 564.

(3) Use annealed material only.141 Not to be used over 1250°F.(51 Not to be used over 1200°F. Alloy NO6625 in the annealed condition is subject to severe loss

of impact strength at room temperatures after exposure in the range of 1000DF to 1400°F.(61 Not to be used over 800°F.(7, Not to be used over 1OOO’F.

C1W.STemp.. ‘F 150 300 400 800 900 2500

-20 to 100 290 750 1000 1500 2250 3750 6250200 260 750 1000 1500 2250 3750 6250300 230 730 970 1455 2185 3640 6070400 200 705 940 1410 2115 3530 5880500 170 665 885 1 3 3 0 1995 3325 5540

600 140 605 805 1210 1815 3025 5040650 125 590 785 1175 1785 2940 4906700 110 570 755 1135 1705 2840 4730750 95 530 710 1065 1595 2660 4430800 80 510 675 1015 1520 2540 4230

850 65 485 650 975 1460 2435 4060900 60 450 600 900 1350 2246 3745950 35 385 515 776 1160 1930 3220

1000 20 365 485 725 1090 1820 30301050 . . 360 480 720 1080 1800 3000

1100 325 430 645 965 1610 26851150 275 365 550 825 1370 22851200 . . 185 245 370 555 925 15451250 145 195 295 440 735 12201300 . . . 110 145 216 325 540 900

L L

WORKIING-r

PRESSURES 6IY CLASSES8, priig


-\

I-,

R

,-.





47Ni-22Cr-9Mo-18Fe 8 572 Gr. ND6002 (l)(Z) 8 435 Gr. NO6002 (1)

NOTES:(1) Use solution annealed material only.(2) The chemical composition, mechanical properties, heat treating requirements, and grain size

requirements shall conform to the applicable ASTM specification. The manufacturing proce-dures, tolerances, tests, certification, and markings shall be in accordance with ASTM B 564.

CISSTemp., ‘F 150 300 400 600 900 1500 2500

-20 to 100200300400500

290260230200170

750 1000 1500 2250 3750750 1000 1500 2250 3750680 905 1360 2040 3395600 795 1196 1795 2990575 770 1150 1730 2880

600 140 660 745 1120 1660,650 125 660 745 1120 1680700 110 560 7 4 6 1120 1660750 95 530 710 1065 ,696800 80 610 675 1015 1525

850900950

10001050

503520

485 650 975 1460 2435450 600 900 1350 2245386 515 775 1160 1930365 486 725 1090 1820360 480 720 1080 1800

1100115012001250,300

1350140014501500

326 430 646 965 ,610 2686276 365 550 825 1370 2285

. . 205 276 410 620 1030 ,715180 246 366 645 910 1515140 186 275 410 685 ,145

WORKI PRESSURE: Y CLASSES dg

2795 46602795 466027952880 44302540 4230

105 140 205 310 51575 100 150 2 2 5 38060 80 115 175 29040 55 85 125 206

-

625062505880

4800

408037453 2 2 030303000

860830485






25Ni-46Fe-ZlCr-5Mo B 672 Gr. NO8700 (l)(Z) B 599 Gr. NO8700 (1)

NOTES:(1) Use solution annealed material only.12) The chemical composition, mechanical properties, heat treating requirements, and grain size

requirements shall conform to the applicable ASTM specification. The manufacturing proce-dures. tolerances, tests, cenification, and markings shall be in accordance with ASTM B 564.

ClassTemp., “F

-20 to 100200300400600

600650

150

275260230200170

140125

WORKING PRESSURES BY CLASSES, psig

300 400 600 900 1500 2500

720 960 1440 2160 3600 6000720 960 1440 2160 3600 6000680 905 1360 2040 3400 5670640 855 1280 1920 3205 5340610 615 1225 1835 3060 5100

595 790 1190 1780 2970 4956570 760 1140 1705 2645 4740

Reprinted from ASME 616.5-1996 and 1996, by permission of The American Societybf MechanicalEngineers. Ail rights reserved


GENERAL INFORMATION S,ECTlON 9

TABLE 2-3.11 RATINGS FOR GROUP 3.11 MATERIALSNominal I I I

Designation Forgings

44Fe-25Ni-ZlCr-Mo B 649 Gr. NO6994 (l)(2)

NOTES:(1) Use annealed material only.

Castings Plates

B 625 Gr. NO6994 (1)

(2) The chemical composition. mechanical properties. heat treating requirements, and grain sizerequirements shall conform to the applicable ASTM specification. The manufacturing proce-dures. tolerances, tests, certification. and markings shall be in accordance with ASTM B 6M.

Cla=Temp.. +

-20 to ‘100200300400500

600650700

150

245230210190170

140125110

WORKING PREBSURE

300 400

640 865600 600545 725496 660455 610

430 576420 560410 545

se

IIV CIASSES, prig

600 900 1500 2500

126012001065

995916

665 1296640 1266620 1230

1920 3205 53401605 3006 50101630 2720 45301490 2465 41401370 2266 3610

216021052060

360035103420

Reprinted from ASME 816.5-1996 and 1996. by permission of The American Society of MechanicalEngineers. AN rights reserved


SECTION 9. GENERAL INFORMATION



26Ni-43Fe-22Cr-5Mo 5 621 Gr. NO8320 (l)(Z) S 620 Gr. NO8320 (1)

47Ni-22Cr-20Fe-7Mo S 581 Gr. NO6965 H)(2) S 582 Gr. NO6985 (1)

NOTES:(1) Use solution annealed material only.(2) The chemical composition, mechanical properties, heat treating requirements. and grain size

requirements shall conform to the applicable ASTM specification. The manufacturing proce-dures, tolerances, tests. certifio+cn. and markings shall be in accordance with ASTM 8 564.

ClW5Temp., ‘F

-20 to 1002003 0 04 0 05 0 0

2602 4 0225200170

6 0 0 1406 5 0 1257 0 0 1107 5 0 9 58 0 0 8 0

WORK6

3 0 0

6706 2 5565635500

4 7 54654 5 04 4 5430

UG

1PRESSURE

8 9 58 3 07807156 6 5

6 3 56 2 06005 9 0575

is f

1

1-f CLASSES

660

1345, 2 4 5117510751000

960930900685865

;, PS

I

ig

900

20161870, 7 6 016101500

14251395135013301295 i

33603 1 1 5293526802500

23752320225022152160



2 5 0 0

56005 1 9 046904 4 7 04 1 7 0

39603870375036903600

_..


TABLE 24.13 RATINGS FOR GROUP 3.13 MATERIALSNominal


49Ni-XC,-18Fe-6Mo 6 581 Gr. NO6975 (l)(Z) 6 662 Gr. NO6975 (1)

Ni-Fe&Z-Ma-Low Cu B 564 Gr. NO8031 13) 6 625 Gr. NO8031 (3)

NOTES:(1) Use solution annealed material only.(2) The chemical composition, mechanical properties, heat treating requirements, and grain size

requirements shall conform to the applicable ASTM specification. The manufacturing proce-dures, tolerances. tests, certification. and markings shall be in accordance with ASTM 6 564.

(3) Use annealed material only.

Y CL&ES, psig

I

WORKING PRESSURES B

I I300 I 400 600 900

1500 22501410 21161325 1 9 8 51265 10007-1190 1780

1125 16851105 16601086 ,630,066 ,695,016 ,625

150ClW3

Temp.. ‘F 1600 2500

3750 62503630 58803310 55203170 52602970 4950

28102765272026602540

46604605463044304230

-20 to 100’200300400500

600650700750800

2 0 0260230200170

1401251109580

705660

940865845790

750735726710675

635695

560555545530510 II


Stayfards of The Tubular Exchanger Manufacturers Association 225




47Ni-22Cr-19Fe-6 MOB 561 Gr. NO6007 (l)(2) B 562 Gr. NO6007 (1)

NOTES:(1) Use solution annealed material only.(21 The chemical composition. mechanical properties, heat treating requirements, and grain size

requirements shall conform to the applicable ASTM specification. The m.+nufacturing proce-dures, tolerances, tests, certification, and markings shall be in accordance with ASTM B 564.

ClassTemp., ‘F

-io to 1002w300400500

150 300 4 0 0

275 720 9 6 0 , 4 4 0 2160245 645 8 6 0 , 2 9 0 1935230 600 7 9 5 ,196 1795200 560 7 5 0 1125 1685170 535 7 1 5 1070 1605

600 140 520 6 9 0650 125 510 680700 110 505 675750 9 5 5 0 0 870BOO 8 0 4 9 5 660

8 5 0 6 6 485 6 6 0900 5 0 4 5 0 6 0 0950 3 5 385 5 1 6

1000 2 0 365 4 8 5


WORKII PRESSURE IY CLASSES,

1035102010151005

995

976900775725

, P?;ig

900

15551535152015051490

,4601350,1601090 I

1500 2500

360032302990

6000538049804 6 8 04460

28102675

2590255525302510

2435 40602245 37451930 32201820 3030

Reprinted from ASME 816.51996 and 1998. by permission of The American Society of MechanicalEngineers. All rights resewed

43204260422041804140



Designation Forgings CaStillgS Plates

33Ni-42Fe-210 B 564Gr. N08810,,, B409 Gr. NOBBlOIl~

NOTE:(1) Use solution annealed material only.

-2oto 100 230 600 BOO 1200 1800200 205 540 720 1080 1620300 195 505 675 1015 1520400 185 460 540 960 1440500 170 455 610 910 1370

600 140 440 585 880 1320650 125 425 565 850 1275700 110 420 560 640 1250750 95 415 550 625 1240800 80 410 545 815 1225

85090095010001050

400 530 795 1195 1990395 530 790 1190 1980385 515 775 1160 1930365 485 725 1090 1620325 435 650 975 1625

11001150120012501300

,500

320 430 640 965 1605275 365 550 825 1370205 275 410 620 1030180 245 365 545 910140 185 275 410 685

135014001450

65503520

.

105756040

1401008055

205 310 515 8 6 0150 225 380 630115 175 290 48565 125 205 345

WORK11

300

PRESSURE IBYClASSES

409

rig

900 1500

30002700253024002280

21952125210020652040

Reprinted from ASME 816.5.1996and 1998,by permission of The American Society of MechanicalEngineers. All fights reserved

50004500422040003800

36603540350034403400

33203300322030302710

26752285171515151145

StsndardS Of The Tubular Exchanger Manufacturers Association,,

227




35Ni-lSCr-l%Si B 511 Gr. N08330,1,(21 B536 Gr.NO8330lll

NOTES:(1) Use solution annealed material only.(2) The chemical composition. mechanical propenies. heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturingprocedures. tolerances, tests. certification, and markings shall be in accordance withASTM S 564.

228

ChSSTemp.,'F 150 300 400 600 900 1500 2 5 0 0

-2oto100 275 720 960 1440 2160 3600 8 0 0 0200 245 636 850 1270 1910 3180 5 3 0 0300 226 590 785 1175 1766 2940 4 9 0 0400 200 550 735 1105 1655 2760 4 6 0 0500 170 525 700 1050 1575 2630 4 3 8 0

600 140 500 670 1006 1505 2510 4 1 8 0650 125 490 655 980 1470 2450 4 0 6 0700 110 480 645 965 1446 2410 4 0 2 0750 95 470 625 940 1410 2350 3 9 2 0800 80 465 620 925 1390 2315 3 8 6 0

85090095010001050

,1001150120012501300

65503520

. .

455 605 SO5 1360 2270 3 7 8 0445 590 886 ,330 2215 3 6 9 0385 515 775 ,160 1930 3 2 2 0365 485 725 ,090 1820 3 0 3 0310 410 616 926 1645 2 5 7 0

240 320 4 8 0 720 1205 2 0 0 5185 245 370 655 925 1545145 195 290 435 725 1210,15 155 235 350 585 9 7 595 130 190 285 480 7 9 5

1350140014501500

75 100 150 2 2 0 370 6 1 555 75 110 186 280 4 6 545 60 95 140 230 3 8 535 45 70 100 170 2 8 5

WORK11 PRESSURESl BYCLASSES i, Pda

Reprinted from ASME 816.5-1996 and 1998, by permission of The American Society of MechanicalEngineers. All rights resewed


SECTION 9GENERAL INFORMATION

TABLE 2-3.17 RATINGS FOR GROUP 3.17 MATERIAL

Nominal I I IDesignation Forgings Castings PI&.X

ZSNi-20.5Cr-3.SCu-2.5Mo A 351 Gr. CN7M (1)

NOTE:(1) Use solution annealed material only.

WORKING PRESSURES BY CLASSES, LX

I

+300t600

I600520465420390

800690620L565520

480

12001035930a45780

360 720 I;ig

900

18001555139512651165

1080

f

l-

1500

30002590

t

233021101945

1800

ClsrsTemp., ‘F

-20 to 100200300400500

600 I150

230200180160150

140

2500

500043203880352032401

Reprinted from ASME 616.5-1996 and 1998, by permission of The American Society of MechanicalEngineers. NuI rights reserved



CHARACTERISTICS OF TUBING

1.112

-i-

Keigh I.h. in ly by the following f.wtors:Aluminum.. .............................................. 0.35Titanium ................................ ................ 0.58A.I.S.I. 4CQ Series S/Steels ........ .._........ 0.99A.I.S.I. 3W Series S/steels .................... LUZ

** Liquid Velocity = p; g 2tET&d

Aluminum l3m~ .................................. LO4 Nickel ............................. .._ ..................... 1.13Aluminum Bras ........... .._ ....................... 1.06 Nickel-Copper ........................................ 1.12Nickel-CJumne-Inn ................................ LO7 Copper and CupNic!els .................... 1.14Admiralty ............................... ..-........ _. .... 1.09

in feet per sec. (Sp. Gr. of Water at MPF. = 1.0)


:.:/ ! ;,


TABLE D-7M

CHARACTERISTICS OF TUBING

-

A l u m i n u m 0.35 A l u m i n u m B r o n z e 1 .O4 Nicke I......,,....,,,.,............._..............T i t a n i u m . 0.58 A l u m i n u m B r a s s ..__......... 1.06A.I.S.I. 400 Series S/Steels

Nickel-Copper ,..,.............................0.99 N i c k e l - C h r o m e - I r o n 1.07

A.I.S.I. 300 Series S/Steels .._...Copper and Cupro-Nickels .,..,_......,

1.02 Admirality ..._.......................,......,.. I.09kz. Per Tube Hour

‘* Liquid Velocity = C y sp. Go, ofLiquid in meten per sec. (sp. Gr. 0f water at 15.6 deg C = 1.0)



1

_

_

-<

R

-



INTERNAL WORKING PRESSURES (PSI)OF TUBES AT VARIOUS VALUES OF ALLOWABLE STRESS

%7Inches

TubeGageB W G 2,000 4,000 6,000

Code Allowable Svess (PSI)

6,OW 10,000 12,000 14,000 16,000 16,000 20,OOC

114 27 269 539 609 1079 1349 1618 1866 2156 2428 269626 305 611 916 1222 1528 1633 2139 2444 2750 305624 378 757 1135 1514 1693 2271 2650 3029 3407 376623 434 669 1304 1739 2173 2606 3043 3478 3913 434722 492 964 1476 1966 2460 2952 3444 3936 4428 492021 570 1140 1711 2281 2862 3422 3992 4563 5133 570420 630 1261 1891 2522 3153 3763 4414 5045 5675 630619 776 1552 2329 3105 3861 4658 5434 6210 6987 776318 929 1859 2789 3719 4648 5578 6508 7438 6366 9297

3m 24 246 492 736 964 1231 1477 1723 1969 2216 246222 317 635 952 1270 1568 1905 2223 2541 2856 317621 366 732 1099 1465 1831 2196 2564 2930 3297 36632u 403 606 1210 1613 2017 2420 2624 3227 3631 403419 492 964 1476 1968 2460 2952 3444 3936 4428 492018 563 1167 1751 2334 2918 3502 4065 4669 5253 563617 706 1412 2116 2624 3530 4236 4942 5646 6354 706016 804 1609 2414 3219 4024 4829 5634 6439 7244 604915 907 1814 2722 3629 4536 5444 6351 7258 8166 907314 1075 2151 3227 4303 5379 6454 7530 8606 9662 10758

l/2 22 234 469 703 936 1172 1407 1641 1676 2110 234520 296 593 869 1186 1483 1779 2076 2372 2669 296619 360 720 1080 1440 ,601 2161 2521 2861 3241 360216 425 650 1276 1701 2126 2552 2977 3402 3828 425317 511 1022 1534 2045 2557 3068 3680 4091 4603 511416 560 1160 1741 2321 2901 3462 4062 4642 5223 580315 650 1301 1952 2603 3264 3905 4556 5207 5856 650914 765 1531 2297 3062 3828 4594 5359 6125 6891 765613 696 1792 2666 3564 4481 5377 6273 7169 8066 696212 1056 2112 3168 4224 5261 6337 7393 8449 9505 105662

__.

518 20 234 469 703 936 1172 1407 1641 1676 2110 234619 264 566 652 1136 1420 1704 1968 2272 2556 284018 334 669 1003 1336 1672 2007 2342 2676 3011 334517 400 601 1202 1603 2004 2405 2606 3207 3608 400916 453 907 1361 1615 2268 2722 3176 3630 4063 453715 507 1015 1522 2030 2537 3045 3553 4060 4568 507514 594 1166 1763 2377 2971 3566 4160 4754 5349 594313 692 1384 2076 2766 3460 4153 4845 5537 6229 692112 810 1621 2432 3242 4053 4664 5674 6465 7296 610711 907 1814 2722 3629 4536 5444 6351 7258 8166 907310 1035 2070 3105 4140 5175 6210 7246 6261 9316 10351




-rTube

%,%-

le Allow

2.000 4PJ 8.ow 10,000d

stress (P

12,CCG 14,000 18,Obl 16,000

20 193 387 581 775 989 116318 275 551 a27 1102 1376 185417 329 859 989 1318 1646 197818 372 744 1117 1489 1662 2234I5 415 a31 1247 1883 2079 249514 485 971 1458 1942 2426 291313 563 1127 1891 2255 2818 336212 857 1315 1973 2631 3289 394811 733 1457 2201 2Q35 2669 440310 633 1887 2601 3335 4189 50039 937 1874 2611 3749 4888 5823a 1087 2135 3203 4271 5339 6407

135719302306

2911339939464aG45137583885817475

155122052837297933273685461052825671667074988643

174524612967335237434370507459208805

64369811

20 185 330 495 861 826 991 1157 132218 234 469 703 936 1172 1407 1641 187617 279 569 a39 1119 i399 1679 1959 223918 315 631 947 1263 1579 ia95 2211 252715 352 704 1057 1409 1761 2114 2488 ~361614 410 621 1231 1842 2052 2483 2874 328413 475 951 1426 1902 2377 2653 3329 380412 553 1108 1660 2213 2787 3320 3874 442711 616 1232 1846 2464 3060 3837 4313 4929IO 698 1398 2094 2792 3490 4166 4866 55849 762 1564 2347 3129 3912 4894 5477 6259a 686 1778 2664 3553 4441 6329 8216 7108

2110251926433171

4260 47554960 55345645 8161

7042 78247994 8662

20 144 286 432 576 720 864 ma 1152 12981s 203 407 811 815 1019 1223 1427 1831 163517 243 486 729 973 1218 1459 1703 1946 216918 274 548 622 1097 1371 1845 1919 2194 246615 305 811 918 1222 1526 1633 2139 2444 275014 355 711 1066 1422 1778 2133 2469 2644 320013 411 a22 1233 1845 2056 2467 2676 3290 370112 477 955 1432 1910 2388 2a85 3343 3821 429811 530 1081 1592 2123 2854 3185 3718 4247 477610 600 1200 1801 2401 3001 3602 4202 4602 54039 871 1343 2014 2636 3357 4029 4700 6372 80438 780 1520 22al 3041 3801 4682 5322 8082 6843


1939275732973724415948566637657873398338937310879

16522345279931593523

144020392432274230563556411247786309

67157803



iic;i%-201816I51413121110987

2,000 4,000 6,000 0,000 10,000 14,000

114 220 343 456 572 667 601 916 103i 1145161 323 465 647 609 971 1133 1295, 1456 1616217 434 651 669 1095 1302 1519 1736 1953 2170241 463 724 966 1207 1449 1690 1932 2173 2415200 561 541 1122 1402 1683 IQ63 2244 2524 2505323 647 071 1294 1619 1942 2265 2599 2913 3236374 749 1124 1409 1674 2249 2624 2999 3374 3749415 631 1247 1663 2Q79 2405 2011 3327 3743 4159469 $38 1407 1876 2345 2814 3293 3752 4221 4690523 IO46 1569 2092 2615 3136 3662 4165 4709 5231590 1190 1771 2361 2951 3642 4132 4722 5313 5903660 1301 1952 2603 3254 3905 4556 5207 5959 650Q

r 16.000 16,COO 20,000

231 463 694 926 1157 13aQ 1621 1952 2084 2315308 617 925 1234 1543 1351 2160 2468 2777 3066341 663 1025 1367 1709 2051 2393 2735 3076 3416384 769 1164 1539 1924 2200 2693 3076 3463 3840429 956 1295 1713 2142 2570 2999 3427 3656 4264432 964 1447 1929 2412 2694 3377 3859 4342 4624

171 343 515 666 658 1030 1201 1373 1545 1717227 465 663 911 1139 1367 1595 1623 2051 2279252 504 766 1008 1260 1512 1764 2Ol6 2269 2521263 566 649 1132 1415 1699 1992 2265 2649 2831314 6B 943 1259 1573 1697 2202 2517 2931 3146363 706 1059 1413 1766 2119 2473 2926 3179 3533

235

1-w? 1412111098

2 1412111099



TABLE D-IOMODULUS OF ELASTICITY

- -100 2OQ

zi F.528.1 27.629.5 29.030.4 29.830.7I

30.1- -29.0 28.527.6 27.125.6 25.417.9 17.69.9 9.6

30.8 30.226.3 27.830.9 30.329.6 29.129.8 29.3- -16.9 16.614.9 14.615.9 15.615.4 15.021.9 21.5

31.2 rr0.s27.8 27.314.9 14.613.9 13.429.3 28.8

zi zi

-

28.1

-

27.4 26.8 26.1 25.5 24.8 2411 23.4

28.8 28.228.7 27.5- -

Jo0xi27.C28.:29.429.7

Fi26.725.017.39.2

29.927.429.928.628.6

900 loo022.2 20.123.5 22.824.8 23.925.6 24.624.7 22.7

25.2 21521.4 19.722.6 22.1

llO(

17.822.123.023.720.4

19.117.521.7

27.0 26.4 25.924.8 24.2 23.827.1 26.4 26.025.9 25.3 24.926.1 25.5 25.1

1201ir321.221.822.5la.2

iiz15.321.2

z23.225.324.324.5-

24.0-

-iG 700 a00

26.4 25.3 23.925.3 24.8 24.126.9 26.3 25.527.7 27.1 26.328.0 27.3 26.1

zi 25.6 24.725.2 24.6 23.024.1 23.7 23.116.0 15.4

28.726.428.827.627.8

cl13.414.212.619.6

29.025.913.49.9

27.3-

28.2 27.625.9 25.428.3 27.127.1 26.527.3 26.7

14.512.813.711.9 11.218.8

28.6 27.925.5 24.912.8

26.7 26.1 25.5 25.1 24.5

-

26.224.5-

23.8 23.0

AUSTENITIC STN STLLOW CHROMES THRU 2% I

28.229.7

16.314.415.414.621.1

xi26.914.412.428.5

271

28.8 28.329.0 28.6

27.3 26.726.1 25.724.7 24.316.9 16.6a.7 a.1

29.5 29.027.1 26.629.5 29.128.3 27.928.5 28.1

16.0 15.614.1 13.815.0 14.714.0 13.320.7 20.2

29.8 29.326.6 26.214.1 13.811.5 10.728.1 27.8

27.6 27.0 26.626.8 26.0 25.3

2-l/4 CR-1 MO 4 3 CR-l MO 30.6INT CR-MO (5-9X CR) 30.9

12. 13. 15 4 17% CR 29.2LOW NI STEELS THRU 3-1/2X 27.8

NI-CU ALLOY 400 (N04400) 26.090-10 CU-NI (C70600) la.0ALUMINUM 10.0

NI-CR-FE ALLOY 600 (NO66OO) 31.0NI-FE-CR (NO6aOO k NO6610) 28.5NI-MO ALLOY 8 (NlOWl) 31.1NI-MO-CR ALLOY C-276 fN10276) 29.8NICKEL 200 (NO22OO) . 30.0

x15.016.015.522.0

31.428.015.014.4

COPPER & AL-BRONZECOMYERCLAL BRASSADMIRALTYTITANIUM70-30 CU-NI (C71500)

NI-MO ALLOY E-2 (~10665)NI-FE-CR-MO-CU (NOaa25)MUNTZ (C36500)ZIRCONIUM (R60702)

27.5 26.724.4 23.8

26.2

-

22.8

-

17-19 CR STN STL 29.0AL-6XN STN STL (NOa367) 28.3Al-29-4-2 29.0

REFERENCES:ASME SECTION II, D. 1998 EDITIONR.k MOEN (COLLECTED PAPERS. LETTERS k DATA)HUNTINGTON ALLOYS, INC. BULLETIN #15Ml-76T-42ALLEGHENY LUDLUM STEEL CORP.CABOT-STELLITETELEDYNE WAH CHANG ALBANY

INTERNATIONAL NICKEL CO.ASTM SPECIAL TECHNICAL PUBLICATION # 181CARPENTER TECHNOLOGYTRENT TUBEAIRCO INC__, .._.SANDVIK TUBE



TABLE D-10 MMODULUS OF ELASTICITY

C STL. C-MO, MN-MO

kPo X lot6

21.1 1 37.6 93.3 1146.9 ~204.4~260.0 ;

2ot.3~199.9~~96.s~l93.1~168.9~186.2 11AUSTENITIC SIN STL 195.1 193.1

LOW CHROMES THRU 2% 204.8 203.42-l/4 CR-l MO & 3 CR-l MO 211.0 209.fINT CR-MO (5-9X CR) 213.0 211.;

12. 13. 15 & 17% CR 201.3 199.9LOW NI STEELS MRU 3-l/2% 191.7 190.3

NI-CU ALLOY 400 (N04400) 179.3 177.990-10 CU-NI (C70600) 124.1 123.4ALUMINUM 66.9 68.3

NI-CR-FE ALLOY 600 (~06600) 213.7 212.'NI-FE-CR (NO6800 & N08810) 196.5 195.1NI-MO ALLOY 8 (NlOWl) 214.4 213.cN&MO-CR ALLOY C-276 (N10276) 205.5 204.'NICKEL 200 (N02200) 206.8 205.f

COPPER & Al-BRONZE 117.2 116.:

COMMERCLAL BRASS 103.4 102.;ADMIRALTY 110.3 109.fTITANIUM 106.9 106.;70-30 CU-NI (C71500) 151.7 151.c

315.6 371.1 426.7 482.iiiihli&185.5191.0

I 181.3 I 175.8 171.0186.8 181.3

I176.5

193.1 186.2 180.0 170.3

80.0 176.5 170.3 160.073.7 169.6 158.6 147.5-lTt-66.2 163.4 159.3 155.8;10.3 106.2

~200.6 197.2 195.1 192.4:202.0 198.6 196.5 193.7

i114.5 112.4 110.3 107.6i100.7 99.3 97.2 95.1'107.6 106.2 103.4 101.4i103.4 100.7 96.5 91.7:148.2 145.5 142.7 139.3

NI-MO ALLOY 8-2 (~10665) 216.5 215.1 211.0 207.5 205.5 202.0NI-FE-CR-MO-CU (N08825) 193.1 191.7 188.2 185.5 183.4 180.6MUNTZ (C36500) 103.4 102.7 100.7 99.3 97.2 95.1

L

ZIRCONIUM (~60702) 99.3 95.8 92.4 85.5 79.3 73.8NI-CR-MO-C6 (~06625) 206.8 202.0 198.6 196.5 193.7 191.7

7 MO (S32900) 199.9 198.6 193.1 189.67 MO PLUS 15329501 199.9

TP 439 STN STL 199.9AL-6XN STN STL (N08367) 195.1 193.7 188.9 184.8 180.0 175.8N-29-4-2 199.9SEA-CURE 213.72205 (S31803) 199.9 198.5 194.4 190.3 186:l 183.43RE60 (S31500) 199.9 197.9 189.6 184.8 179.2 174.4

j37.e 593.3 648.9

38.6 122.7 105.557.2 152.4 146.264.8 158.6 150.369.6 163.4 155.156.5 140.7 125.5

48.2 131.7 114.535.8 120.7 105.552.4 149.6 146.2

82.0 178.6 174.4166.9 164.1 16O.C182.0 179.3 174.4174.4 171.7 167.5175.8 173.1 168.9

184.1164.1

180.6 176.5

173.1 168.9 165.:

152.4

REFERENCES:ASME SECTION II, 0. 1998 EDITIONR.A. MOEN (COLLECTED PAPERS, LETTERS & DATA)HUNTINGTON ALLOYS, INC. BULLETIN #lSMl-76T-42

INTERNATIONAL NICKEL CO.ASTM SPECIAL TECHNICAL PUBLICATION # 181CARPENTER TECHNOLOGY

ALLEGHENY LUDLUM STEEL CORP. TRENT TUBECABOT-STELLITE AlRCO, INC.TELEDYNE WAH CHANG ALBANY SANDVlK TUBE



TABLE D-l 1MEAN COEFFICIENTS OF THERMAL EXPANSION

-2w -100 ,w 263 xul IW son wo 700 6u9 900 loC0 ,,@I 1209 ,Jo 140Fihw c4RwN sn a C-YN m 5.60 5.90 650 6.67 6.67 7.07 7.23 7.42 7.59 7.76 7.89c-9 m.c-l/2 WI & 1 CR-,/2 YO 5.64 164 57, 6.09 a43 6.74 7.06 7.20 7.W 7.7, 7.66 aM)C-UN-51 STL, 1 ,/4-I/2 NO &.I CR-I IAO 5.53 5.69 a26 66, 6.9, 7.17 7.41 7.59 7.77 7.9, a07 6.2,"N-U0 STL 5.M) am 7.06 7.25 7.43 7.58 7.7o 1.63 7% 0.05 6.11 a232-10 & 3-l/2 N, 62, 6.Y 676 6.96 7.16 7.32 7.47 7.6,- - -, ~, - --~ t I I

2-l/4 CR-1 uo 5.60 5.90 6.50 6.70 6.90 7.07 7.23 73 7.56 7.62 7.72 7.62 7.90 7.97s CR-I/2 IJO 560 5.90 6.50 6.73 6.67 6.97 7.05 ,.,S 7.24 7.32 7.4, 7.46 7.56 7.647CR-l/2 YO a 9 CR-I uo 5.64 5.68 5.85 6.02 a,5 6.29 6.49 6.5, a62 6.71 6.62 6.96 7.M 7.0812 CR (t 13 CR 5.10 SAQ 59~ 6.15 ay1 a.0 6.46 6.5, 6.60 6.67 6.72 a76 6.63 6.6615cR&17cR17-19 CR UP 4391

6.,7 6.44BE.6 6.65 6.71

,Au WUOES OF TP 516 d: 317 9lN Sit 6.54 6.76 6.97 9.21 9.42 9.50 9.76 9.90 10.02 10.16 10.29 I0.u) 10.52Au GRUXS OF TP 304 STK ST,. 655 6.19 9110 9.19 9.37 9.U 9.69 9.62 9.95 10.07 10.16 lo.29 10.39uLwEsoF7P 32, $lN 9n 9.02 9.16 9.26 9.34 9.42 9.46 9.55 9.61 9.67 9.73 9.79 9.85 9.90MLCRAoE6oflP ?87$lN m a62 a92 9.22 9.45 9.65 $43 9.97 IO.66 10.22 10.33 10.8 (0.54 10.662s CR-12 N,. 23 CR-12 N, a 2s CR-20 N, 6.67 9.02 9.10 9.11 9.,6 9.21 9.25 9.26 9.32 $37 9.4, 9.47 9.54At-6x74 (NW67) 6.50 ass 6.61 6.72 6.62 6.07 8.95 9.05 9.16 9.29 9.40 9.5,AtWIN"" (xm3) 11.60 12.04 i2.54 ,285 13.15 13.45#uY,N"Y f&l611 llsoil2.06 12.m 12.91 ,122 13.52M#WY (CWiXS I.2.3 k 7)NI-CU (NiuIM)NI-CR-E (WWCQ) IM-FE-CR (timem it NwlO)WI-FE-CR-MC-CU (NwS25)NW0 (ALLOY B)NI-W-CR (AL@+, C-276) (N10276)t#CKEL (MLOY 2UO)(NO22W)226S(S3lsoS)

JREM) (Wsm)70-M CU-N, (C7,SC.J)90-10 b 66-20 CU-N,COPPERERASS

7.9s a.?4 6.66 6.76 a92 9.M) 9.11 9.20 9.3l 9.40711 7.71 7.65 7.97 8.69 8.20 830 6.406.0$ A24 655 64, 6.4, 6.47 6.57 6.666116 6.50 6.54 6.7, 6.9, 7.&S 7.22 7.U

6.20 6.39 6.77 7.21 7.52 7.74 7.9, 6.05 6.16 6.27 83 6.60 6.70 a647.w 7.06 7.25 7.50 7.65 7.80 7.90 6.02

6.03 8.25 6.45 8.61 6.76 6.90 9.0, 9.166.50 6.70 6.90 9.10

I

8.90

-

,LU",N"Y BRONX 9.w7Y0(532wo) 5.66 6,C., 6.10 6.20 6.35 6.SO 6.59 6.&3 7.06 7.25 7.44 7.637YOPtUS (9329%) 6.39 647 6.94 7.22 7.49 7.68 7.88 7.96 6.06 a,2

WPER-SILKmN ,o.mu)LIIRAlY ,,.MZIRCWIUY 3.20 .x4 5.70 3.90 4.10CR-NI-FE-YO-CU-CB (NW 2CCB) 6.30 a33 9.40 9.M)III-CR-UO'CB (KLOI 625)(X6625) 5.20 6.20 6.70 7.12 1.20 7.50 755 7.4s 7.52 7.64 7.70 780 6.00 6.20 6.35u. 23-4-2 5.20SEA-CURE 5.38 5.43 5.62 5.81 S.ea 5.95

REFERENCES:AWE SECTION II, 0. 1998 EDITIONRA. MOEN (COLLECTED P A P E R S. LETTERS dt DA T A )HUNTINGTON ALLOYS. INC. BULLETIN #lSMl-76T-42ALLEGHENY LUDLUM STEEL CORP.CABOT-STELLITETELEDYNE WAH CHANG ALBANYBRIDGEPORT BRASS COMPANYSABIN CROCKER. PIPING HANDBOOK. 4TH EDITION

INTERNATIONAL NICKEL CO.ASTM SPECIAL TECHNICAL PU8LlCATiON # 181CARPENTER TECHNOLOGYTRENT TUBEAIRCO. INC.SANDVIK TUBENATIONAL BUREAU OF STANDARDSD.G. FURMAN, JOURNAL OF METALS


10.6j10.499.9:

10.7:9.629.64-

7.6,8.16-

a50

-


TP 304 mc snTP 316 h 317 STN STLTp 321 h 347 STN ST1TP 310 SYN STL

NI-UO ALLOY 6NI-MO-CR LilLOY C-276 (N10276)ALUYINUU NLCFf 3W3&WIN"" ALLOY 6061MANIUU &RAW 1.2.3 a 7)

MUIRWYNML BFNSSCOP?ER90-10 CU-NI

ZIRCONIWCR-U0 MLOY XM-27CA-Nl-FE-UO-CU-C9 (ALLOY ZCCB)NI-CR-UO-03 (#LLOY 625)AL 29-e-2S&CUREAl-6XN (NO6367)

TABLE D-12THERMAL CONDUCTIVITY OF METALS

3a.E12.6 12.9 13.98.6 a7 9.16.7 6.8 7.4

7.1

6.1 6.45.9 6.4

12.3 102.8 Ku.:36.1 96.9 99112.7 12.5 121

1 2 . 916.9 1 11.6 1 12.3 1

K--!4.6!3.0tR8!a719.0-17.2I&O!2.315.914.8

iTi

11.8Il.011.4la611.511.0

i;;;18.911.610.19.6

a29.2

Il.2-

b7.027.0

-

8.6

13.7

-

l-

3.52.20.20.28.7

7.36.11.65.94.a

z

2.21.51.91.12.01.3

Tii12s21.419.719.718.4-17.216.120.915.914.8

116

12.712.012.311.6

2.5 33.19.8 20.92.1 12.60.6 11.10.0 10.4

8.7 9.39.e IO.4

1.i

,9sat

9.1 9.6

11.3-

51.033.0

12.8 13.3 13.712.1 12.6 13.1

33.822.0l-r13.2 13.8 14.311.6 IZI 12.710.9 11.4 11.6

10.0 I 10.7 IIl.0 11.5 12.1

11.4 11.6

t-t53.0

gj17.616.716.517.216.6-16.215.616.915.114.8

iiIi

14.513.814.113.6

iiijii-16.215.315.015.616.0-15.615.215.515.014.8

G

14.914.214.614.1

-15.615.cI4.615.315.6-15.515.015.315.114.6

ii?

15.314.615.014.5

- - -

14.9 15.5 161313.2 13.8 14.512.4 12.9 13.6- - -

-

-

11.5

-

-

-

12.0

-

-

-

12.t

-

REFERENCES:ASME SECTION II, 0, 1998 EDITIONHUNTINGTON ALLOY. INC. BULLETIN #1%41-76T-42A.I.M.E. TECH. PUBLICATIONS NOS 291. 360 & 648ALLEGHENY LUOLUM STEEL CORP.TELEDYNE WAH CHANG ALBANY

AMERICAN BRASS CO.TRENT TUBEAlRCO, INC.CAEOT-STELLITECARPENTER TECHNOLOGY

TRANS. A.S.S.T. VOL. 21, PAGES 1061-1078BABCOX a! WILCOX co.

INTERNATIONAL NICKEL CD.SANDVIK TUBE


.-\

i?

r\

?

,F .

A

.-.

r-3


TABLE D-12 MTHERMAL CONDUCTIVITY OF METALS

r 7- ! :

18.9s7.054.134.131.8-es27.936.227.525.6

E-

EE;;a35333.133.131.2

29a27.934.627.325.6

zi

22.0 22.820.6 21521.3 222m.l 20.9

57J36.221.8192la0-16.1la0

58538122.620.1163

TF;19.0

19.6-

88357.1

-

16.6

-I-

19.7-

91.;641

-

17:

-

EE-35.033.732.032.030.5

z27.733227.025.6

zi

23.522.323.021.6

-

23.920.919.7

;i;199

20.1-

-

la

-

-13.8I.62I.6

1.7'35i.5i.6

z-

I.2tt.7!.7

1.7!.OI.4

J.9

-

9.C

gLs1.9I.6I.81.7

;;;r.0123.13.6

Is

il5.91.43.5

5.62815

9:

-

i.8I.6iJI.4

;aI.9!J

-

0.6

a.O.5.ld

i

5.3.O.I

:7Ll;5

II

15.6 371.1

t4.3 42.6Il.0 39.616.9 36.056.5 35.a332 323

z¶.6 29.827.5 27.759.6 38.627.5 27.525.4 25.6

23.0 232

25.7-IO.7184Fl.0t5.012.4

G27.957.427525.6

Tz

19.6 20.4 21.118.2 19.0 19.9163 19.7 20.6175 Ia4 19219.0 19.9 x1.8la3 19.0 19.6

562 55.0 z31.0 32.7 34.3192 20.1 20916.6 17.5 184II7 16.6 17.3

13.3 142 T15.1 15.9 17.0

19.4 19.4

54.04A665.9?2.7 81.3433 46.719.622.0

19.4-

84.851.9

-

15.7

-

I 7c

x21n2121

2I2:2!212:

21

22:

2

22

/ 1

-L

3231x31x

2227312f2?

24

24zz!2:

2;'X

I2l

i 1'

/ 81:

2726252527

2626262623

25

26252625

I CR-l/Z Ml & l-j/4 CR-I/Z U(!-l/4 CR-7 uoi CR-112 NO

I CR-l/z “0I CR-1 Ins-1/2 NicKaI2 CR & 1.3 CR15 CR

17 CR17-19 CR op 439)PxMNrnIp 316 a 317 m mrP321&347 STN SnrF 310 5TN 5lL2m5 (s31603)3Sf60(5315co)

14.9 15.1 15.7 16.6 175 16.411.6 21.6 12.6 13.8 14.9 15.7

12.3 13.2 14.0 14.9

10.6 11.1 11.6 12.1 12.8102 11.1 12.1 13.0 14.0

177.1 177.9 18D.3182.11B16166.3 167.7 171.3 174.1 176.422.0 21.6 20.8 m2 19.9 19.6

121.1 123.8 136.7 145.41223128.1133.3139z3m.4 36s.4 387.7 367.75l.S 53.7 53.8 64.0312 323 36.3 39.6

152 16.1 17.0 17.8 18714.9 163 17.7 192 m.4

1223MB19.613.2

9.9 10.0 lo.7 118 12.5 13.2152 1911163 16.6 178 la9 m.1 211

13.7

HI-EE-CR--W-W kdo8825)NMloMLoYBNI-W)-CR KLW C-276 000276)

MWL awsUIFQER90-10 W-WI70-M Cu-w (C71rn)7~(u2900)7uoRJE(532950)

WNR2lwmlwCR-WI AILW XN-27CR-NI-FE-LIO-W-CB(ULOI20CB:Nl-CR-UO-CS(WP625)AL m-4-2SEA-aIREAL-ani(w&?67)

I I I I

REFERENCES:ASME SECTION’ II, 0, 1998 EDITIONHUNTINGTON ALLOY, INC. BULLfTlN #15Ml-76T-42AI.M.f. TECH. PUBLICATIONS NOS 291. 360 & 648ALLEGHENY LUOLUM STEEL CORP.TfLfOYNf WAH CHANG ALBANVTRANS. AS.S.T. VOL. 21. PAGES 1061-1078fimcox % WILCOX co.

AMERICAN BRbSS CO.TRENT TUBEAIRCO, INC.CABOT-STELLITECARPENTER TECHNOLOGYINTERNATIONAL NICKEL CO.SANOVlK TUBE



Diameter

Inshcl

OMX)0.1260.2500.3750.5UO0.6250.7500.875

0.000.000.010.030.060.030.130.17

Diamew

Iochu

4.wl4.1254.2604.3754.w4.6254.7504.075

w;gop”lbichlurPOETI&

3.563.794.024.264.514.765.035.29

Diamla

IO&l

a.cm6.1256.250a.3756.500a.625a.7506.875

w;goJ-TllicknoIrPotmda

14.2614.7015.1615.6216.0816.5717.0517.54

Diameter

lnchu

12mo1 2 1 2 612.26012.375126cO12.62512.75012.675

3207327533.4224.1134.6025.5036.2136.92

l.ooO 0.22 s.cCo 5.57 9.Mo 16.04 13.ooo 37.641.125 0.28 5.125 &as 0.125 la.55 13.125 36.371.250 0.35 5.260 6.14 9.250 19.06 13.259 33.101.375 0.42 5.375 6.44 9.376 19.58 13.375 39.65lSO0 0.50 5.6cO 6.74 9.5w 20.10 135M) 40.591.625 0.59 5.625 7.05 9.625 20.63 13.625 41.351.750 0.63 5.750 7.36 9.750 21.17 13.750 42111.875 0.78 5.875 7.69 9.075 21.72 13.675 4266

2.cCQ 0.89 6.0x ,a.02 iO.CCO 2227 14.ooo 43.662.125 1.01 6.125 a.36 IO.125 2 2 . 6 3 14.125 44.442.260 1.13 6.250 6.70 10.250 23.40 14.250 45.232375 1.26 6.375 9.05 10.375 23.96 14.375 46.032.500 1.39 6.XQ 9.41 10.500 24.56 14.6co 46.632625 1.53 6.625 9.78 10.625 25.15 14.625 47.642750 1.68 6.750 10.15 10.750 25.74 14.760 48.462.675 1.84 6.875 10.53 10.675 26.34 14.675 49.28

3.Doo 2.00 7.cco 10.01 11.002 26.95 15.m K1.123.125 2.16 7.125 11.31 11.125 27.57 15.125 50.963.250 2.35 7.250 11.71 11.250 26.19 15.250 51.803.375 2.64 7.375 12.11 11.375 ?a.82 15.375 52.653.500 2.73 7.500 12.53 Il.500 2S.46 15.500 53.513.625 " 2.93 7.625 12.95 11.625 30.10 15.625 54.383.760 3.13 7.760 13.38 11.750 ~30.75 15.750 66.25

3.875 3.34 7.375 13.61 11.875 31.41 15.375 56.13

WEIGNTS OF CIRCULAR RINGS AND DISCS’)Example:Requked: WelgMOfaRlng~ODx361/2‘IDx2l/~Thick43'dbmetwdiscl'thkkw&~hs36 1/Tdbmeterdlxl'thlckw~hsRing 46.x26 l/Y Y l'welgh¶

+il&S;S

Rlng46-X361/2'x21/2'wighs216.45lbs641.13lbs

Aluminum ..~.............................."....._ ................... 0.35'Titadm ....I." ....................................................... 0.58A.LS.1. 400 Series SiSkdr .... ..~...................~ ..... 0.99A.I.S.I. 3M Sedc, SlSurl~ .................. ..~........_. I.02Alumi,,,",, Bronze ... ..~......................................". 1.WNaval R&d Bn,, ....................................... ..~ ..... 1.07

Mvnrz taernl _........." ............................................. 1.07Nickel-Cimmc-Inn .................... ..-................. .. 1.07Admiralty i.........._........_................"." ................. 1.09Nickel ....................................... ..~..............- ....... 1.13Nickel-Copper .................................................... 1 .I2CoPpr 8r CuPm Nickclr ........... .._.........._........u. 1.14



0c3

T*BLE o-1 2-(oo”ll”“.d)

62 WEIGHTS OF CIRCULAR RINGS AND DISCS

Diameter

lllchcr

lS.CCO16.125IS.25016.37516.50016.625IS.75016.675

“p;$Thickncsr

Pounds

57.0257.9268.9259.73w.6461.5662.4953.43

Diameter

[ncher

21.m21.12521.25321.37521.5w21.62521.75021.675

w;goy?hic!acn

Polmds

96.2399.40lW.53101.77102.96104.16105.37106.69

Diameter

lnchcr

2s.m26.12526.25026.37526.50026.62626.75026.675

Wpg$

IhicknerrPOtBIdS

lM.57162.02153.43154.95156.42167.80159.36160.66

Eimcer

Inches

31.wa31.12531.25031.37531.50031.62531.76031.675

“pF,pc

ThickrussPound,

214.05215.76217.62219.26221.01222.77224.53226.31

17.cQO 64.37 22.Ow 107.61 27.ooO 162.36 32.W 226.0817.125 65.32 22.125 109.03 27.125 163.66 32.125 229.6717.250 66.26 22.260 110.27 27.250 165.40 32.250 231.6617.375 67.24 22.375 111.51 27.375 166.92 32.375 22&c17.KxI 66.21 22.5w 112.76 27.500 168.45 32.600 235.2717.625 69.19 22.625 114.02 27.625 169.96 32.626 237.a17.750 70.16 22.750 115.26 27.750 171.52 32.750 23S.go17.675 71.17 22.675 116.55 27.675 173.07 32.675 240.73

1S.ct-a 72.17 23.1X0 117.63 2S.wl 174.63 33.Ow 242.5616.125 73.17 23.125 119.11 26.125 176.19 33.125 244.4019.250 74.19 23.250 12u.40 26.250 177.76 33.250 246.2516.375 75.21 23.375 121.70 26.375 179.34 33.375 246.1116.500 76.23 23.500 123.01 28.5al 160.92 33.500 249.9716.625 77.27 23.625 124.32 28.625 162.51 33.625 251.6416.750 70.31 23.760 125.64 28.760 16411 33.750 253.7116.675 79.35 23.975 126.9s 29.675 165.71 33.675 255.60

19.m 80.41 24.oM) 129.30 29.cal 167.32 34.wO 257.4919.125 61.47 24.125 129.64 29.125 166.94 34.125 259.3819.260 62.64 24.250 130.96 29.250 190.57 34.250 261.2919.375 63.61 24.375 132.34 29.375~ 192.20 34.375 263.2019.500 6470 24.500 133.70 29.SQY 193.64 34.653 265.1219.625 65.79 24.625 135.07 29.625 195.46 34.625 267.0419.750 66.90 24.750 136.44 29.750 197.14 24.750 268.9719.675 67.43 24.675 137.62 29.675 196.60 34.675 270.91

m.#J 69.10 25.m 139.21 3n.Oa xx).47 35xoO 272.66a.125 90.21 25.125 140.61 30.125 x)214 35.125 274.6120.250 91.24 25.250 142.01 30.250 2fJ3.62 35.250 276.77a375 92.47 26.375 143.42 30.375 205.51 35.375 276.7320.xX) 93.61 25.500 144.64 3aca 2u7.20 35.500 280.71273.625 94.75 25.625 146.26 30.625 2ca.90 36.625 2626920.760 95.90 25.750 147.69 30.750 210.61 36.750 264.6720.675 97.06 25.975 149.13 30.675 212.33 36.675 266.67

StandardS Of The Tubular Exchanger Manufacturers Association 243


TABLE D-,~cQnlLln”.d)

WEIGHTS OF CIRCULAR RINGS AND DISCS

DkWrW

lncbts

36.00036.12536.25026.37536.50036.62526.7%36.675

W$t$ylhicknerr

Pomdr

288.67290.68292.69294.71296.74296.763co.62302.67

Dimmer

lnchu

4l.ow41.12541.25041.37541.5w41.6%41.7%41.675

“2i&=llxickacsr

Poxmds

374.42376.713JS.w381.30363.61385.83388.25390.58

DiamctcrW&k&g

Dimeterlllicknot

“ig$=

‘Ibickouahchu POUKIS Inch POlllId

46.wo 471.32 Sl.cw 579.3446.125 473.88 51.125 562.1946.250 476.45 51.250 585.M46.375 478.03 51.375 5a7.9046.5w 461.62 51.xX) 590.7646.625 434.21 51.625 593.6346.750 486.61 51.750 596.5146.675 469.42 51.675 5%.3n

37.cul 304.93 42.000 392.91 47.m 492.03 52co3 602.2937.125 3c6.sS 42.125 395.25 47.125 494.65 52.125 605.1937.253 309.06 42.250 397.69 47.250 497.26 52250 606.0937.375 311.14 42375 399.96 47.375 499.91 52.375 611.9037.Eco 313.23 42543 402.32 47.500 502.55 52.500 613.9237.625 315.32 42625 404.69 47.625 505.20 52.625 616.8537.7% 317.42 42.750 407.07 47.750 507.86 52.750 619.7937.675 319.52 42.675 409.45 47.675 510.52 52.875 622.73

3a.m 321.M 43.ow 411.64 43.m 513.19 63.ccil 625.6736.125 323.75 43.125 414.24 46.125 515.67 53.125 626.6336.250 325.88 43.250 416.65 46.250 516.55 53.250 631.5936.375 328.01 43.375 419.06 43.375 521.24 53.375 634.5638.500 330.15 43.503 421.46 46.500 523.94 53.500 637.5338.625 332.30 43.625 423.90 46.625 526.64 53.625 640.5238.750 334.46 43.750 42s.34 48.750 529.35 53.766 643.5138.675 336.62 43.375 426.76 46.675 532.07 53.075 646.50

”39.wl 338.79 44.000 431.22 49.wo 534.80 54.cw 649.5139.125 340.96 44.125 43348 49.125 537.53 54.125 652.5239.250 343.14 44.250 436.14 49.2% 540.27 54.250 656.5339.375 345.33 44.375 438.60 49.375 643.01 64.375 658.5639.500 347.53 44.5w 441.06 49.5cO 545.77 54.500 661.5939.625 349.73 44.625 443.56 49.625 643.53 54.625 664.6339.750 361.94 44.750 446.05 49.750 551.29 54.750 667.6739.675 354.16 44.675 446.54 49.675 554.07 54.675 670.73

4o.m 356.38 45scO 451.05 5o~ocO 556.65 55mO 673.7940.125 358.61 45.125 453.56 60.125 559.64 55.125 676.8540.250 360.85 45.250 456.07 60.250 562.43 55.250 679.9240.375 363.10 45.375 456.60 50.375 565.23 55.375 6830340.500 265.35 45.500 461.13 50.500 568.04 55.500 666.0940.625 367.61 45.625 463.66 30.625 570.86 55.625 669.1940.750 369.67 45.750 466.21 50.750 573.66 55.750 692.2940.675 372.14 45.675 466.76 50.875 576.51 55.075 695.39




56.wo 898.51 6l.wO 828.8156.125 701.63 61.125 832.2166.250 704.76 81.250 836.8266.375 707.90 61.376 839.0356.500 711.04 61.500 842.4566.626 714.19 61.625 645%56.750 717.34 81.750 849.3256.876 720.51 61.875 852.78

57.Mx) 723.68 620x 856.2167.125 726% 82.125 859.6657.250 730.04 82.250 863.1357.375 733.23 82.375 866.605r.m 736.43 62.600 870.0757.625 73Q.64 62.626 873.5657.760 742.85 62.750 877.0557.875 746.07 82.876 8ao.55

58.coo 749.29 .63.wo 884.05$8.126 752.63 63.126 887.5658.250 756.77 63.250 891.0858.375 759.01 63.375 894.6158.5% 762.27 63.500 898.1458.625 765.63 63.625 901.6858.750 768.80 63.750 905.2258.875 772.07 63.875 908.78

59.ax 775.35 64.ccil 912.34 69.OQO 1060.46 74.0x 1219.7269.125 778.64 64.125 915.91 69.125 1064.31 74.125 1223.8469.250 76194 64.250 919.43 69.250 loM1.16 74.250 1227.9769.375 785.24 64.375 923.06 69.376 1072.02 74.375 1232.1159.m 768.55 64.500 926.65 69.500 1075.88 74.500 1226.2659.625 791.87 64.626 930.24 69.625 1079.76 74.625 1240.4159.750 795.19 64.750 933.85 69.750 1063&l 74.750 1244.6759.875 798.52 64.675 937.46 69.875 1087.53 74.875 1248.73

6o.cco60.12560.2%60.37560.603%.82560.75060.875

801.86 6s.m 941.07805.20 65.125 944.69808.66 66.250 948.32811.91 65.375 951.96815.28 65.5x 955.61818.65 65.625 959.26822.03 65.750 862.91625.42 65.875 Q66.5a

Diameter

IRciw

%.wo66.12666.25066.37666.60066.62566.75066.876

WcightpcrInchof

ThicknurPounds

970.25973.93977.62981.31965.01966.7199243Q-X.15

Diamctcr

inches

7l.ccm71.12671.25071.37571.5w71.62571.75071.875

"STllli&rPounds

1122.831126.761120.751134.721138.701142.681146.671160.67

67.CCG 999.88 72.wO 1154.6867.125 1003.81 72.126 1168.6967.250 lcw.35 72.250 1162.7167.375 1011.10 72.375 1166.7467.600 1014.85 72.605 1170.77

! 67.625 1018.62 72.625 1174.6167.750 1022.39 72.760 1178.8667.875 1026.16 72.875 1182.91

68.wo 1029.94 73.wl 1186.9866.125 1033.73 73.125 1191.0468.250 1037.53 73.250 1195.1263.375 1041.34 73.375 1199.206a.500 1046.15 73.5% 12Q3.2963.625 IO-B.96 73.625 1207.3968.750 1052.79 73.750 1211.4968.875 1056.62 73.875 1215.60

70.c0o 1091.42 75.wQ 1252.9170.126 1095.32 75.125 1267.0970.250 1099.23 75.250 lZl.2770.375 1103.15 75.375 1265.4770.m 1107.07 75.500 1269.6770.625 1111.00 75.625 1273.8870.750 1114.93 75.750 1278.0970.875 1116.88 75.875 1282.31




Dimmu

inches hchu

76.OD3 1286.54 61.CCXl 145l.33 6s.ooo 1547.38 Sl.ooO 1644.5076.125 1290.76 61.125 1465.90 85.125 165217 91.125 la49.5776.250 1295.02 81.250 1470.42 86.m 1656.97 91.250 la54.6576.375 1299.27 61.375 1474.95 85.375 1661.78 91.375 1859.7376.500 1303.52 61.500 1479.4s e6.5m 1666.59 91.500 la64B376.625 1307.79 81.625 1464.03 66.625 1671.41 91.625 1669.9276.750 1312.06 81.750 1488.59 86.750 1678.24 91.750 1a75.0376.675 1316.33 al.675 1493.13 66.875 16a1.07 91.675 laaO.14

166s.911690.761695.611700.461705.341710.221715.101719.99

1724.891729.791734.701739.621744.551749.481754.421759.26

77.um77.12577.25077.37577.50077.62577.75077.076

1320.621324.911329.211333.511337.631342.141346.471350.60

a2.m62.12582.25382.37682.50082.62582.75082.675

1497.701502271506.841511.431516.021520.611625.221529.83

87.wO67.12587.26087.375a7.5m87.625a7.7$087.675

92.wQ92125922509237592.50092.6259275092.675

1885.26law.391895.521900.661805.811910.~1916.131921.29

7a.m76.12578.2%78.37578.50078.62578.75076.876

1355.141359.491363.841368.211372.571376.951361.331385.72

s3.ow83.12563.25063.37583.50083.62583.75083.675

1534.451539.071543.711546.351652.991557.641562.301566.97

aa.cco68.125aa.88.375ffl.60088.62566.75088.675

93.wOS3.125LB.25093.375w.Kx)83.62593.76093.675

1926.471931.651936.841942.941947.241952451957.67196289

79.m79.12579.26079.37579.5m79.62579.75079.875

1390.111394.521398.931403.341407.771412.M1416.631421.09

a4.m84.12564.25364.37564.50084.62584.75064.975

1571.651576.331581.011565.711593.411595.121599.&11606.56

69.00089.12689.25089.375a9.5009.62589.75089.875

1764.321769.271774.241779.211764.191769.161794.1a1799.18

94.cco94.125s4.2.5094.37594.50094.62594.75094.975

1968.121973.361976.601983.661889.111994.2J31999.652iw.93

ao.ooo 1425.53 85.0x 1609.29 so.oca lm4.19 95.000 mo.2280.125 1429.99 65.125 1614.03 90.125 1809.20 95.125 2Q1.5.5160.250 1434.45 85.250 1s1a.77 90.250 1614.22 95.250 2U20.8180.375 1438.92 a5.375 1623.52 93.375 1619.25 95.375 2026.1260.500 1443.40 85.500 1628.26 90.500 (624.29 95.500 2Q31.4320.625 1447.69 85.625 1633.9-l 93.625 1829.33 95.625 2036.7660.750 1452.36 65.750 1637.81 90.750 lS34.38 95.759 2042.0680.875 1456.88 as.875 1642.59 90.875 1639.44 95.875 2t.U.42



WEIGHTS’OF CIRCULAR RINGS AND DISCS

2272.162277.m2263.422269.062294.712300.3723c6.032311.70

2052.762068.112063.472c68.63207d.202u79.582ca4.9620Q0.35

ios5.752101.162106.572111.%2117.412122.642128.262133.73

2502.692506.602514.5125M.432526.3625322Q2536.242544.18

2744.372750.662756.742762.942769.152775.362731.582787.80

lnchu

101.ccu101.125101.250101.375lOI.5co101.625101.750101.675

Diametsr

Inches

106.Mx)106.1251%.2YJ106.375106.500106.625lffi.750106.875

Diameter

hchcr

%.ooo96.12596.25096.375%.50396.62586.75086.875

lnchu

llI.CCO111.125111.2%111.375Ill.500111.625111.750111.875

97SQJ97.12597.25097.37697.50397.62597.75097.075

102.Mo102.125102.250102.375102.500102.625102.750102.675

107.m107.123107.250107.375107.500107.625107.750107.675

2550.142556.102562.0725sa.c-l2574.0325ml.02

112wl1121251122s112375112.500112625112750112875

2794.0428co.2828c.3.522612782819.042625.312531.562637.86

%.ooo 2139.18 103.m 2363.M lOS.CCO 2598.03 lu.Qx 2644.1598.125 2144.65 103.125 2266.76 108.126 2604.04 113.125 2wJ.45Se.250 2150.11 103.250 2374.52 iOa.250 2610.07 lI3.w) 2866.7598.375 2155.59 103.375 2380.28 106.375 2616.10 113.375 2653.0698.500 2161.07 103SW 2366.04 lOfl.xO 262214 113.500 2869.3698.625 2166.56 103.625 2331.80 108.625 2628.18 113.625 2875.7098.750 2172.05 103.7&Y 2397.58 108.750 E34.24 113.750 2882.0398.876 2177.56 103.675 2403.36 ice.875 x40.30 113.675 2888.37

99.m 2163.06 104.000 2409.14 109.000 2645.36 114sca 2894.7299.125 2188.58 104.125 2414.94 lOS.125 2652.43 114.125 2901.0799.m 2194.10 104.250 2420.74 109.250 2658.51 114.250 2907.4399.375 2199.63 104.375 24X55 108.375 2664.60 114.375 2913.7999.500 2205.17 104.500 243236 lOQ.!XO 2670.70 114.500 2920.1699.625 2210.72 104.626 2438.19 106.625 2676.80 114.625 2926.5499.750 2216.27 104.750 2444.02 109.750 2682.90 114.760 2932.9399.875 2221.82 104.875 2449.85 106.875 2689.02 114.875 2939.32

lCO.CCO 2227.39 105.ooo 2456.70 11o.ca100.125 2232% 105.125 2451.55 110.125IW.250 2238.54 105.250 2467.40 110.250100.375 2244.13 105.375 2473.27 110.375100.503 2249.72 105SCXJ 2479.14 110.5%100.625 2255.32 105.626 2465.02 110.625lca.750 2260.93 Ic-5.750 2490.90 110.7%loo.875 2266.64 105.875 2496.80 110.875

2696.142701.272707.412713.&2719.70

115.%0 Bd5.72115.125 2952.13115.250 2958.54115.375 2964.96115.5% 2371.39115.625 2977.63115.750 2984.27115.875 2990.72


SECTION 9

248

GENERAL INFORMATION

TABLE D-14CHORD LENGTHS &AREAS OF CIRCULAR SEGMENTS

A=CxD2

k=2[h(D-h)]“’


,,,,


TPlBLE D15CONVERSION FACTORS



rAl%ED-r6+o”u”“ed,

CONVERSION FACTORS


SECTION 9GENERAL INFORMATION

CONVERSION TABLESFOR WIRE AND SHEET METAL GAGES

Value, in appmdmre decimals of M inch.

)w

i

_

’ ,

;ACfoe

0.p“umbu

0.454

%Z0.340

:3

:

Stanclards Of The Tubular Exchanger Manufacturers Association 251

SECTION 10 RECOMMENDED GOOD PRACTICE

RECOMMENDED GOOD PRACTICERGP SECTION

This section of the TEMA Standards provides the designer with additional information and guidance relativeto the design of shell and tube heat exchangers not covered by the scope of the main sections of theStandards. The title of this section, “Recommended Good Practice”, indicates that the information shouldbe considered, but is not a requirement of the basic Standards.

When a paragraph in this section (RGP) is followed by an R, C, and/or R, this RGP paragraph is anextension or amplification of a like numbered paragraph in the RCB secbon of the main Standards. Similarly,other suffix designations following RGP indicate other applicable sections of the main Standards.


RECOMMENDED GOOD PRACTICE

RGP-G-7.11 HORIZONTAL VESSEL SUPPORTS

RGP-G-7.111 L O A D S

RGP-G-7.1111 LOADS DUE TO WEIGHT

SMMw SMSwr

n Y--h f-Y

SECTION 10

IRVFw

FIXEDSADDLE

RVFwrFIXED

SADDLE

RVS,SLIDINGSADDLE

FIGURE RGP-G-7.1111

1. CALCULAE COMPONENT WEIGHTS AND WEIGHT OF CONTENTS (OPERATING AND TESTING).

2. CALCULATE VERTICAL SADDLE REACTIONS&LONGITUDINAL SHELL MOMENTS DUE TOWEIGHT FOR THE EMPTY, OPERATING t-a TEST CONDITIONS CONSIDERING ACTUALCOMPONENT WEIGHT AND LOCATION.

RVFwr = VERTICAL REACTION @ FIXED SADDLE DUE TO WEIGHTRVSw = VERTICAL REACTION @SLIDING SADDLE DUE TO WEIGHTSMFv,r = LONGITUDINAL SHELL MOMENT @ FIXED SADDLE DUE TO WEIGHTSMSwr = LONGITUDINAL SHELL MOMENT @ SLIDING SADDLE DUE TO WEIGHTSMMw = MAXIMUM LONGITUDINAL SHELL MOMENT BETWEEN SADDLES DUE TO WEIGHT

RGP-G-7.1112 EARTHQUAKE FORCES

N-4MSFm

FIXEDSADDLE

RVFm RVSm

I - - - - - - L - - - - - J

FIXED SLIDINGSADDLE SADDLE

FIGURE RGP-G-7.1112

RV3.nSLIDINGSADDLE

SLIDINGSADDLE

1. CALCULATE SEISMIC REACTIONS AND MOMENTS.

Cs = SEISMIC FACTOR SMMm = SMMwr x Cs RHSEQ = RHFwr x CsRLFm = TOTAL EXCH WT x Cs RVFm = (RLFm x H) / L MSFED = RHFEQ x HRLSm = 0 (SLIDING SADDLE) RVSEQ = (RLFEQ x ii) IL MSSm = RHSEO x HSMFm = SMFm x Cs RHFEQ = RVFwr x CsSMSEQ = SMSw x Cs


SECTION 10 RECOMMENDED GOOD PRACTICERGP-G-7.1113 WIND LOADS

MSFw b - - A - - p MSSwFIXED

SADDLE RVFw SLIDING

FIXED SLIDING SADDLE

SADDLE SADDLE

FIGURE RGP-G-7.1113

1. CALCULATE WIND LOADS (CALCULATE TOTAL WIND FORCE).FLw = WEFF x HEFF x EFFECTIVE WIND LOAD (AS DETERMINED BY APPROPRIATE CODE)FHw = HEFF x LER x EFFECTIVE WIND LOAD (AS DETERMINED BY APPROPRIATE CODE)RLFw = FLw (MAY BE CONSIDERED NEGLIGIBLE FOR SMALL EXCHANGERS)RLSw = 0 (SLIDING SADDLE)SMFw = LONGITUDINAL SHELL MOMENT @ FIXED SADDLE DUE TO TRANSVERSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE)SMSw = LONGITUDINAL SHELL MOMENT @ SLIDING SADDLE DUE TO TRANSVERSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE\SMMw = ‘MAXIMUM LONGITUDINAL SHELL MOMENT BETWEEN SADDLES DUE TO T~iAiSVEkSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE)

RVFw = (RLFw x HE&!) / L RHSw = FHw x ((El + OSL) / LEFF)RVSw = (RLFw x HEFF/~) / L MSFw = RHFw x Hw/2RHFw = FHw x ((A + 0.5L) / LEFF) MSSw = RHSw x HEFF/~

RGP-G-7.1114 THERMAL EXPANSION LOADSLOADS CAUSED BY LONGITUDINAL GROWlH BETWEEN FIXED 8 SLIDING SADDLES

FIXEDSADDLE

I

SLIDINGSADDLE

FIGURE RGP-G-7.1114

1. CALCULATE LOADS DUE TO THERMAL EXPANSION (WHERE p = COEFFlClENT OFFRICTION BETWEEN FOUNDATION AND BASE PLATE AT SLIDING SADDLE).

RLFw = RVSwr x w SMSEXP = RLSw x HRLSw = RVSwr x & SMMmxp = RLSEXP x HSMFEXP = RLFEXP x H p FOR STEEL = 0.6

fi FOR LUBRICATED PLATE = 0.1


,‘1

_-

/-.

.?

,, li

.a


RGP-G-7.1115 COMBINED FORCES

SECTION 10

RLSw RHSEFF-’ W1. I

MSFEFFFIXED

SADDLE

I-------------ARVFw RVSEFFFIXED SLIDING

SADDLE SADDLE

MSSEFFSLIDINGSADDLE

FIGURE RGP-G-7.1115

1, CALCULATE THE COMBINED SADDLE REACTIONS FOR THE FOLLOWING CASES OR AS APPROPRIAEIN DESIGN CRITERIA:. DEAD WEIGHT EMPTY . DEAD WEIGHT EMPTY + EARTHQUAKE. DEAD WEIGHT OPERATING . DEAD WEIGHT OPERATING + EARTHQUAKE. DEAD WEIGHT FLOODED . DEAD WEIGHT FLOODED + EARTHQUAKE. DEAD WEIGHT EMPTY + WIND . DEAD WEIGHT OPERATING + THERMAL EXPANSION. DEAD WEIGHT OPERATING + WIND OR ANY OTHER APPROPRIATE COMBINATION. DEAD WEIGHT FLOODED + WIND

2. CALCULATE RESULTANT SADDLE LOAD 8 SHELL MOMENT FOR WINDIEARTHQUAKE CASES:RVFEFF = LARGER OF (RVFd+ RHF# OR (RVFw 2+ RHFd )”RVSEFF = LARGER OF (RVSwr*+ RHSW*)‘~ OR (RVSw*+ RHSE&‘~SMFm q LARGER OF (SMFd+ SMFvv’f’ OR (SMFwr*+ SMFm=)”SMSEFF = LARGER OF (SMSw’+ SMSw’)‘” OR (SMSw?+ SMSd ,‘”SMMEFF = LARGER OF (SMMw?+ SMMw’)‘” OR (SMMd+ SMME~‘)‘~

RGP-G-7.1116 EFFECTIVE REACTION LOAD SADDLE ANGLE

L /

FIGURE RGP-G-7.1116

1. CALCULATE THE EFFECTIVE SADDLE ANGLE FOR EACH SADDLE FOR ALL WIND AND EARTHQUAKE CASES.

2. EFFECTIVE SADDLE ANGLE = ((ACTUAL SADDLE ANGLE DIVIDED BY 2) - ARCTAN(RH/RV)) x 2(SEE FIGURE RGP-G-7.1116).



RGP-G-7.112 STRESSES

ONCE THE LOAD COMBINATIONS HAVE BEEN DETERMINED, THE STRESSES ON THE EXCHANGER CAN BECALCULATED. THE METHOD OF CALCULATING STRESSES IS BASED ON “STRESSES IN LARGE HORIZONTALCYLINDRICAL PRESSURE VESSELS ON TWO SADDLE SUPPORTS”, PRESSURE VESSEL AND PIPING: DESIGNAND ANALYSIS, ASME, 1972, BY L.P. ZICK

SI’ = LONGITUDINAL STRESS AT SADDLES

7SI” = LONGITUDINAL STRESS

(TENSION AT TOP, COMPRESSION AT SADDLE WITHAT BOTTOM) STIFFENER 7

SI= LONGITUDINAL STRESS -

i

LS,= CIRCUMFERENTIAL

/-

AT MIDSPANCOMPRESSION ATBOTTOM OF SHELL S, = TANGENTIAL SHEAR IN HEAD

i Se = CIRCUMFERENTIALSTRESS AT HORN l!_ Sz = TANGENTIAL SHEAR - RESULTSOF SADDLE IN DIAGONAL LINES IN SHELL

FIGURE RGP-G-7.112


RECOMMENDED GOOD PRACTICE SECTION 10

RGP-G-7.1121 LONGITUDINAL STRESS AT MID SPAN (Sr)

LONGITUDINAL STRESS

s,=*(w) ,!$

LONGITUDINAL STRESS (METRIC)

S,=*( ;y”,“’ ) x10’; kPa

WHERE

SMMEFF = MAXIMUM EFFECTIVE SHELL MOMENT ATMID SPAN (SEE FIGURE RGP-G-7.1115) in-lb (mm-kN)

r = OUTSIDE SHELL RADIUS, inches (mm)ts = SHELL THICKNESS, inches (mm)

RGP-G-7.1122 LONGITUDINAL STRESS AT THE SADDLE WITHOUT STIFFENERS (S?)

THIS AREA IS INEFFECTIVEAGAINST LONGITUDINAL SENDINGIN AN UNSTIFFENED SHELL

fg

4a--=+

LONGITUDINAL STRESS LONGITUDINAL STRESS (METRIC)

SMFEFF or SMSEFF lb SMFEFF or SM.&Fs1’ =* SlN*A 1 -$ SI’ =* x 106, kPa

d tsA+ SINACOSA - 2 yq’-

‘[

SIN’A

x( 7 COSA) 1 nrz ts A + SINACOSA - 2 7

?i(y-COSA)I

WHERE

SMFEFF , SMSEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXEDOR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb. (mm-kN)

r= OUTSIDE SHELL RADIUS, inches (mm)ts = SHELL THICKNESS, inches (mm)A = % EFFECTIVE SADDLE ANGLE. radians “---I

EFFECTIVE SECTIONMODULUS OF ARC



RGP-G-7.1123 LONGITUDINAL STRESS AT THE SADDLE WITH STIFFENER RINGS OREND CLOSURES CLOSE ENOUGH TO SERVE AS SIIFFENERS (SI-)

LONGITUDINAL STRESS

S,” =* SMFEFF or SMSEFF

WHERE

LONGITUDINAL STRESS (METRIC)

lb,-$ S,” = * (

SMFEFF or SMSEFFlir2 ts ) x10’. kPa

SMFEFF , SMSw = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXEDOR SLIDING SADDLE ISEE FIGURE RGP-G-7.1115) in-lb, (mm-kN)

r= OUTSIDE SHELL RADIUS, inches (mm) SECTION MODULUS = d tSI inches3(mm3)ts = SHELL THICKNESS. inches (mm)

IF THE SHELL IS STIFFENED IN THE PLANE OF THE SADDLE OR ADJACENT TO THE SADDLEOR THE SADDLE IS WITHIN A 5 r/2 OF THE END CLOSURE, THEN THE ENTIRE SECTION MODULUSOF THE CROSS SECTION IS EFFECTIVE.

ALLOWABLE STRESS LIMIT FOR St 3’ 8 52”

TENSION -THE TENSILE STRESS + THE LONGITUDINAL STRESSL%JE TO PRESSURE TO BE rE%% ~~~-iiii~%%%3LETENSION STRESS OF THE MATERIAL AT THE DESIGN TEMPERATURETIMES THE JOINT EFFICIENCY OF THE GIRTH JOINT

COMPRESSION -THE COMPRESSIVE STRESS IS TO BE LESS THAN THE BFACTOR IN THE CODE FOR LONGITUDINAL COMPRESSIONOF THE MATERIAL AT THE DESIGN TEMPERATURE.


A

A

A

A


C) SHELL STIFFENED BY END CLOSURE (A <r/Z)

I , I

TANGENTIAL SHEAR STRESS TANGENTIAL SHEAR STRESS (METRIC)

S? =Kz(RVFw or RVSEFF)

rtsle

’ ina sz=Kz(RVFw or RVSEFF)

rts xlO’,kPa

MAXIMUM SHEAR AT 0 = a

WHERE

RVFEFF , RVSEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXEDORSLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (mm-kN)

8, degrees

p = (180 - $ ), degrees

a=n-&(i+&) ,radians CONSTANT 1(2 FORVARIOUS VALUES OF g

r q OUTSIDE SHELL RADIUS, inches (mm)1s = SHELL THICKNESS, inches (mm)

ALLOWABLE STRESS LIMIT - THE MAXIMUM TANGENTIAL SHEAR STRESSFOR CASES A, B. & C IS TO BE LESS THAN 0.8 TIMESTHE MAXIMUM ALLOWABLE STRESS IN TENSIONOF THE SHELL MATERIAL AT THE DESIGN TEMPERATURE.



RGPC-7.1125 CIRCUMFERENTIAL STRESS AT HORN OF SADDLES UNSTIFFENED (Ss)

CIRCUMFERENTIAL STRESS AT HORN OF SADDLE

RVFEFF OR RVSEFF) 3K$RVFw OR RVSEFF) lb4ts(b + lots) - 2tsz I G2

OR

FOR Ls < 8r

Sa= -(RVFEFF OR RVSEFF) 10 ~(RVFEFF OR RVSEFF) lb

4ts(b + lots) - Lsts 2 8 z2

CIRCUMFERENTIAL STRESS AT HORN OF SADDLE (METRIC)

FOR Ls 2 8r

s3= -1r RVFER OR RVSEFF) 3K$RVFw OR RVSEFF)4ts(b+ lots) - .?tsz 1 xlO’,kPa

__

OR

FORLs<SrRVFw OR RVSEFF) ffi ~(RVFEFF OR RVSEFF

4ts(b + 1015) - LSfS! jj x106,kPa

WHERE

RVFEFF. RVSEFF = MAXIMUM EFFECTIVE VERTICAL REACTIONAT THE FIXED ANDSLIDING SADDLE RESPECTIVELY, lb (kN)

r = OUTSIDE SHELL RADIUS, inches (mm)b = WIDTH OF SADDLE, inches (mm)

Ls = SHELL LENGTH BETWEEN TUBESHEETS OR BETWEEN SHELL FLANGES ORBETWEEN SHELL FLANGE TO HEAD TANGENT LINE, inches (mm)

KS = CONSTANT FROM FIGURE RGP-G-7.1125

MAXIMUM ALLOWABLE STRESS LIMIT FOR 53 = 1.25 TIMES ALLOWABLE STRESS IN TENSION FOR THE SHELLMATERIAL AT DESIGN TEMPERATURE.



Figure RGP-G-7.1125VALUE OF CONSTANT &

A = Distance from tubesheet or shell flange or head tangent line to center of saddle, inches (mm)r = Outside radius of shell, inches (mm)

OSM0.u.a i+l+

L”“““‘~““““‘:“““~“~““““’0.0 0.5 1.0 1.5

RATIO A/r



RGP-G-7.1126 STRESS IN HEAD USED AS STIFFENER (S,,

SECTION 10

If the head. stiffness is used by locating the saddle close to the head, tangential shear stress shouldbe added to the head oressure stress. The tangential shear has horizontal components whichcause tension across the head.

(RVFcf~ or RWd % lbs, = ?--

rth ina

central Angle Q = x - &(; + -$), radians

g = (180 - 8/Z), degrees

y1= 3 ----sinsa8 [x 1- a + sin a COSQ0, degrees

Constant K4 Value For Various Saddle ContactAngles, 0

Where tt, = thickness of head, inches (mm)

Allowable Stress

or RVS cd YQ

1x 106, kPa

rth

The tangential shear is to be combined with the pressure stress in the head and should be lessthan 1.25 times the maximum allowable stress in tension of the head material at design temperature.



RGP-G-7.1127 RING COMPRESSION IN SHELL OVER SADDLE (S,)

The sum of the tangential fdrces on both sides of the saddle at the shell band causes a ringcompression stress in the shell band. A width of shell equal to 5t.s each side of the saddle plus thesaddle width resists this force. Wear plates of greater width than the saddle may be used to reducethe stress,

e = (180 - e/2), degrees

Rine Comoression Stress Rinp Comoression Stress (Metric)

(RVF, or RVSca) K, lbs, = I -

ts(b + lots) in*

Central Angle a = x - -&t + $), radians

KS =1 + cos a

Ir - a + sinacosa

Constant XC5 Value For Various Saddle ContactAngles, 9

140° I 0.697150° 0.673

Where b = saddle width, inches(mm)

The maximum compressive stress should be less than 0.5 times the yield stress of the materialat the design temperature. This should nof be added to the pressure stress.


0000 RECOMMENDED GOOD PRACTICE

RGP-G-7.113 DESIGN OF SADDLE PARTS

DETERMINE MAXIMUM LOADS FROM APPLICABLE LOAD CONDmON

THERE

SECTION 10

ARE MANY TYPES OF BASETHE

PLATE, WEBFOLLOWING APPROACH IS OFFERED

& GUSSET ARRANGEMENTS.AS ONE OF MANY.

BASE PLATE

C A L C U L A T E P R O P E R T I E S O F S A D D L E A B O U T X - X & Z-Z AXIS

A=AREA. in2(mm’ )Ix-x. Iz-z=MOMENT OF INERTIA ABOUT x-x OR z-z. in’tmm’ 1Sx-x. Sz-z=SECTION MODULUS ABOUT x-x OR z-z . in’(mm’ 1

C H E C K W E B & G U S S E T S A S C O M B I N E D C R O S S - S E C T I O N F O R B E N D I N G

BENDING STRESS ABOUT BENDING STRESS ABOUTx-x AXIS x-x AXIS (METRIC)

h-X ,bS b = sx_x *%a

Sb = h-x- X lO”.kPoSX-X

WHERE Mx-x =(RLFEFF OR RLSEFF) X JEFF , in-lb (mm-kN)Sb < 90% YIELD STRESS

BENDINGz ‘:“A’xss” ABOUT BENDING STRESS ABOUTZ-L AXIS (METRIC)

MZ-2 lbS b = 5z_z B x2 Sb :MZ-Z

52-2X 106. kPo

WHERE Mz-z = (MSFEFF OR MSSEFF). in-lb (mm-kN)Sb < 90% YIELD STRESS



CHECK WEB & GUSSETS AS COMBINED CROSS-SECTIONFOR COMPRESSION

STRESS IN COMPRESSION,

STRESS IN COMPRESSION.

sc= RVFEFF or RVSEFF lbA ‘q

sc = RVFEFF or RVSEFFA

x IO’, (kPa)

STRESS LIMIT = ALLOWABLE COMPRESSIVE STRESS

COMBINE STRESS FROM BENDING AND COMPRESSION(t-3

ACTUAL BENDING STRESS + ACTUAL COMPRESSIVE STRESS < ,ALLOWABLE BENDING STRESS ALLOWABLE COMPRESSIVE STRESS -



RGP-G-7.12 VEfiTlCAL VEiSEL’SUiPOliTS

SECTION 10

THE VESSEL LUGS DESCRIBED IN THIS PARAGRAPH INCORPORATE TOP PLATE, BASE PL4TE ANDTWO GUSSETS. OTHER CONFlGURATlONS AND METHODS OF CALCULATIONS ARE ACCEPTABLE.

APPLIED LOADS

TENSIONLOAD

UPLIFT

W q TOTAL DEAD WT. PER CONDITIONANALYZING (EMPTY, OPERATION,FULL OF WATER, ETC...), lb (kN)

N = NUMBER OF LUG SUPPORTSdB = BOLT CIRCLE, inches (mm)M = OVERTURNING MOMENT AT THE SUPPORTS

DUE TO EXTERNAL LOADING, in-lb (mm-kN)

MAXTENSION= g - f ,lb(kN)(UPLIFT)

4MIFW> dB- NO UPLIFT EXISTS

MAX COMPRESSION = -& + f , lb (kN)

RGP-G-7.121 DESIGN OF VESSEL SUPPPORT LUG

SUPPORT WITH TWO GUSSETSLL = LOAD PER LUG(TENSlON OR COMPRESSION), lb (kN)EC = LOCATION OF LOAD REACTION, inches (mm)Ht = DISTANCE BETWEEN TOP PLATE

AND BOlTOM PLATE, inches (mm)Tb = THICKNESS OF BOTrOM PLATE, inches (mm)

Tt = THICKNESS OF TOP PLATE. inches (mm)

Tg = THICKNESS OF GUSSETS, inches (mm)TP = TOP PLATE WIDTH, inches (mm)GE = BOTTOM PLATE WIDTH, inches (mm)

bw q BEARING WIDTH ON BASE PLATE(USE 75% OF GB IF UNKNOWN), inches (mm)

p= LLXECHt

, tb (kN)


SECTION 10 RECOMMENDED GOOD PRACTICERGP-G-7.122 BASE PLATE CONSIDER BASE PLATE AS A SIMPLY SUPPORTED BEAM SUBJECT TO A

UNIFORMLY DISTRIBUTED LOAD o, lb (kN)

Ms = NQ+W*a , in-lb (mm-kN)

WHERELL

o = Q+ZTg&(-$)

FOR TENSION DUE TO UPLIFT, CONSIDER BASE PLATE AS SIMPLYSUPPORTED BEAM WITH A CONCENTRATED LOAD LL, lb (kN)AT ITS CENTER

MT=LL(Q + Tg)

4 zin-lb (mm-kN)

BENDING STRESS BENDING STRESS (METRIC)

*Sb= (bS$rb)2 x.106, kPa

RGP-G-7.123 TOP PLATE

Sb < 90% YIELD STRESS

M* = GREATER OF MB OR MT

ASSUME SIMPLY SUPPORTED BEAM WITH UNIFORM LOAD

P PM = o(Q+ Tg)*

in-lb (mm-kN)

WHERE

I IBENDING STRESS

RGP-G-7.124 GUSSETS

lbSb= (TP)?(Tt) ’ -$

Sb < 90% YIELD STRESS

a =ARCTANGB-Tp

e=eccentricity=EC~-$!.

BENDING STRESS (METRIC)

Sb = cTp;;(Tt) x IO: kPa

degrees

, inches (mm)

MAX. COMPRESSIVE STRESS AT B MAX. COMPRESSIVE STRESS AT B (METRIC)

SC =LL 12 LL /2

GB x Tg x (COS a)2X(, +*) *

GB ’ m2 SC = GB x Tg x (COS c@ x (1 +$ )x l@, kPa

SC 5 THE ALLOWABLE STRESS IN COMPRESSION(COLUMN BUCKLING PER AISC)



RGP-G-7.2 LIFTING LUGS (SOME ACCEPTABLE TYPES OF LIFTING LUGS)

RGP-G-7.21 VERTICAL UNITS

/---

RABBIT-EAR LUG

t

i

IIIII

f

-4

--

i .___ _

p

f

COVER LUG

+%JTAILING LUG-_-_a

TAILING TRUNNION

TAuRUNjQ.4 TRUNNIONS SHOULD BE CHECKED FOR BENDING 8 SHEAR.VESSEL REINFORCMENT SHOULD BE PROVIDED AS REQUIRED.



RGP-G-7.24 LIFT PROCEDURE

1. ESTABLISH LIFT PROCEDURE.LIFT PROCEDURE IS ESTABLISHED BY CUSTOMER.THIS STEP MAY NOT BE NECESSARY FOR ROUTINE LIFTS.

EXAMPLE :

TOTAL WEIGHT

R

2. CALCULATE WEIGHT TO BE LIFTED.

3. APPLY IMPACT FACTOR.1.5 MINIMUM, UNLESS OTHERWISE SPECIFIED.

4. SELECT SHACKLE SIZE.NO IMPACT FACTOR IS APPLIED UNLESS CUSTOMERSPECIFIED. SHACKLE TABLES ARE AVAILABLE FROMSHACKLE MANUFACTURERS.

5. DETERMINE LOADS THAT APPLY (SEE ABOVE FIGURES).



6. SIZE LIFTING LUG.THICKNESS OF LIFTING LUG IS CALCULATEDBY USING THE GREATER OF SHEAR OR BENDINGRESULTS AS FOLLOWS:

I

I___

0 m-l +-I-- -p

1 r ---

t = REQUIRED THICKNESS OF LUG, inches (mm)

Sb = ALLOWABLE BENDING STRESS OF LUG, psi (kPa)

S = ALLOWABLE SHEAR STRESS OF LUG, psi (kPa)

L = WIDTH OF LUG. inches (mm)

h = DISTANCE. CENTERLINE OF HOLE TO COMPONENT, inches (mm)

p = DESIGN LOAD/LUG INCLUDING IMPACT FACTOR, lb. (kN)

I = RADIUS OF LUG, inches (mm)

d = DIAMETER OF HOLE, inches (mm)

REQUIRED THICKNESS FOR SHEAR REQUIRED THICKNESS FOR SHEAR (METRIC)

Pt =

2(S)@ - d/2), inches

Px 10 6

t= ,mm2(S)(r - d/2)

REQUIRED THICKNESS FOR BENDING REQUIRED THICKNESS FOR BENDING (METRIC)

t =Bph

Sb(L)z, inches t=

Sph

Sb(L):!x 106, mm

USE GREATER OF THICKNESS REQUIRED FOR BENDING OR SHEAR.

NOTE: COMPONENT SHOULD BE CHECKED AND/OR REINFORCED FOR LOCALLY IMPOSED STRESSES.


RGP-G-7.3 WIND AND SEISMIC DESIGN


For purposes of design, wind and seismic forces are assumed to be negligible unless the purchaserspecifically details such forces in the inquiry.

When such requirements are specified by the purchaser, the designer should consider their effectson thevarious components of the heat exchanger. These forces should be evaluated in the designof the heat exchanger for the pressure containing components, the heat exchanger suppotts and thedevice used to attach the heat exchanger supports to theanchor points. Methods used for thedesign analysis are beyond the scope of these Standards; however, the designer can refer to thesdected references listed below.

References:

(1) ASME Boiler and Pressure Vessel Code, Section Ill, “Nuclear Power Plant Components.”

(2) “Earthquake Engineering”, Fi. L. Weigel, Prentice Hall, Inc., 1970.

(3) “Fundamentals of Earthquake Engineering”, Newark and Rosenbluth, Prentice Hall, Inc., 1971.

~(4) Steel Construction Manual of the American Institute of Steel Construction, Inc., 8th Edition.

(5)~~e;D$>lS%t$/?‘?~~ Reactors and Earthquakes”, U.S. Atomic Energy Commission Division

(6) “Earthquake Engineering for Nuclear Reactor Facilities (JAB-101)“. Blume, Sharp and Kost, JohnA. Blume and Associates, Engineers, San Francisco, California, 1971.

(7) “Process Equipment Design”, Brownell and Young, Wiley and Sons, Inc., 1959.

RGP-RCB-2 PLUGGING TUBES IN TUBE BUNDLES

In U-tube heat exchangers, and other exchangers of special design, it may not be possible or feasible toremove and replace defective tubes. Under certain conditions as Indicated below, the manufacturer mayplug either a maximum of 1% of the tubes or 2 tubes without prior agreement.

Condition:

(1) For U-tube heat exchangers where the leaking tube(s) is more than 2 tubes away from the periphery ofthe bundle.

(2) For heat exchangers with limited access or manway openings in a welded-on channel where the tube islocated such that it would be impossible to remove the tube through the access opening in the channel.

(3) For other heat exchanger designs which do not facilitate the tube removal in a reasonable manner.

(4) The method of tube plugging will be a matter of agreement between manufacturer and purchaser.

(5) The manufacturer maintains the original guarantees.

(6) “As-built” drawings indicating the location of the plugged tube(s) shall be furnished to the purchaser.



RGP-RCB-4.62 SHELL OR BUNDLE ENTRANCE AND EXIT AREAS

This paragraph provides methods for determining approximate shell and bundle entrance areas forcommon configurations as illustrated by Figures RGP-RCB-4.62tl,4.62t2,4.6221, 4.6222,4.6231and 4.6241.

Results are somewhat approximate due to the following considerations:

location of tubes at the periThe presence of untubed lanes through tK

hery of the bundle.e bundle.

(3) The presence of tie rods, spacers, and/or bypass seal devices.

Full account for such concerns based on actual details will result in improved accuracy.

Special consideration must be given to other configurations. Some are listed below:

1IIG(4)

(6)

2 7 4

Nozzle located near the bends of U-tube bundles,Nozzle which is attached in a semi or full tangential position to the shell.Perforated distribution devices.Impingement plates which are not flat or which are positioned with significant clearance offthe bundle.Annular distributor belts.

RGP-RCB-4.621 AND 4.622 SHELL ENTRANCE OR EXIT AREA

The minimum shell entrance or exit area for Figures RGP-RCB-4.6211, 4.6212,4.6221 and4.6222 may be approximated as follows:

A,=nD,h+F,

where

A 5 = Approximate shell entrance or exit area, inches 2 (mm 2)

D, = Nozzle inside diameter, inches (mm)

h = Average free height above tube bundle or impingement plate, inches (mm)

h = O.S(h, + it,) for Figures RGP-RCB-4.6211, 4.6212 and 4.6222.

h = 0.5(D I - OTL) for Figure RGP-RCB-4.6221.

h , = Maximum free height (at nozzle centerline), inches (mm)

h, = Minimum free height (at nozzle edge), inches (mm)

h,= h, -O.S[D,-(0, ‘-0, ‘)=]

D I = Shell inside diameter, inches (mm)

OTL = Outer tube limit diameter, inches (mm)

F , = Factor indicating presence of impingement plate

F I = 0 with impingement plate

.F 1 = 1 without impingement plate



P, =Tube center to center pitch, inches (mm)

D L =Tube outside diameter, inches (mm)

F, = Factor indicating tube pitch type and orientation with respect to fluid flowdirection

Fs =l.OfOr -& a n d +

F 2 = 0.866 for 4

F, ‘0.707for +

RGP-RCB-4.623 AND 4.624 BUNDLE ENTRANCE OR EXIT AREA

The minimum bundle entrance or exit area for Figures RGP-RCB-4.6231 and 4.8241 may beapproximated as follows:

where

A, = Approximate bundle entrance or exit area, inches 2 (mm 2,8 I = Baffle spacing at entrance or exit, inches (mm)

K = Effective chord distance across bundle, inches (mm)

K = D, for Figure RGP-RCB-4.6231

A p = Area of impingement plate, inches 2 (mm 2)

A,=0 for no impingement plate

ItI 2A,=.-.54

for round impingement plate

Ap=lp2 for square impingement plate

I p = Impingement plate diameter or edge length, inches (mm)

A, = Unrestricted longitudinal flow area, inches 2 (mm 2,


_


The formulae below assume unrestricted longtudinal flow.

A I = 0 for baffle cut normal to nozzle axis

A, = 0.5~1 b for Figure RGP-FlCB-4.6231 with baffle cut parallel with nozzle axis

A, = 0.5( D, - 0TL)c for Figure RGP-RCB-4.6241 with baffle cut parallel withnozzle axis

a = Dimension from Figure RGP-RCB-4.6231, inches (mm)

b = Dimension from Figure RGP-RCB-4.6231, inches (mm)

c = Dimension from Figure RGP-RCB-4.6241, inches (mm)

RGP-RCB4.625 ROD TYPE IMPINGEMENT PROTECTION

Rod type impingement protection shall utilize a minimum of two rows of rods arranged suchthat maximum bundle entrance area is provided without permitting direct impingement on anytube.Shell entrance area may be approximated per Paragraph RGP-RCB-4.622, FigureRGP-RCB-4.6221.

Bundle entrance area may be approximated per Paragraph RGP-RGB-4.624, FigureRGP-RCB-4.6241.



FIGURES RGP-RCB-4.6211,4.6212,4.6221 AND 4.6222

SHELL ENTRANCE OR EXIT AREA

SECTION 10

F I G U R E RBP-RCB- 4.0211 FIGURE RGP - RCB - 4.6212IMPINGEMENT PLATE - FULL LAYOUT IMPINGEMENT PLATE - PARTIAL LAYOUT

Lft D, --If I,, D, -It)

FIGURE RGP-RCB-4.6221 FIGURE RGP-RCB-4.6222NO MPINGEMENT PLATE- FULL LAYOUT NO IMPINGEMENT PLATE - PARTIAL LAYOUT

(D, - DTLv&\

Standards Of The Tubular Exchanger Manufacturers ik&5&iatio~ 277


FIGURES RGP-RCB-4.6231 AND 4.6241

BUNDLE ENTRANCE OR EXIT AREA

FIGURE R G P - R C B - 4 . 6 2 3 1PARTIAL LAYOUT- WITH OR WITHOUT IMPINGEMENT PLATE

VIEW “A A”

FIGURE RGP-RCB -4.6241:FULL LAYOUT - NO IMPINGEMENT PLATE

I

(0s -OTL)/2( 0 ;OTL)/2



RGP-RCB-6 GASKETSRGP-RCB-6.1 TYPE OF GASKETS

Gaskets made integral by welding are often harder in the welds than in the base material. Hardnesslimitations may be specified by the exchanger manufacturer.

RGP-RCB-7 TUBESHEETS

RGP-ACB-7.2 SNELL AND TUBE LONGITUDINAL STRESSES, FIXED TUBESHEETEXCHANGERS

The design of fixed tubesheets in accordance with Paragraph RCB-7.16 is based, in part, upon thetube bundle providing elastic support to the tubesheets throughout the tubed area. It is thereforeimportant to insure that the tubes can provide sufficient staying action against tensile forces andsufficient stability against compressive forces. Paragraph RCB-7.2 provides rules to calculate thetube loads at the periphery of the bundle only. The tubes at the interior of the bundle are notconsidered, but can become loaded both in tension and compression. Tensile forces are generallynot a problem if the requirements of Paragraph RCB-7.2 are met. Compressive forces might,however, create unstable conditions for tubes at the interior of the bundle. Typical conditions thatcan cause this are:

Loading: Tube side pressure and/or differential thermal expansion where the shell, ifunrestrained, would lengthen more than the tubes. (Positive P d per ParagraphRCB-7.161)

Geometry: Flexible tubesheet systems. Generally, those that are simply supported at the edge(F = 1 per Paragraph RCB-7.132) and have a value of F ,(Paragaph RCB-7.161)greaterthan 2.5.

_. -.

Methods similar to those provided in the following references can be used to predict loadings on thetubes at the interior of the bundle:

(1) Gardner, K.A., “Heat ExchangerTubesheet Design”, Trans. ASME, Vol. 70, 1948, pp. A-377-385.

(2) Gardner, K.A., “Heat Exchanger Tubesheet Design-2: Fixed Tubesheets”, Trans. ASME, Vo1.74,1952, pp. A-l 59-166.

(3)1~~~oAi~~_~~~,sign of Tube Plates in Heat Exchangers”, Proc. Inst. Mech. Eng., Ser. B, Vol. 1,

(4) Yu, Y.Y., “Rational Analysis of Heat-Exchanger Tube-Sheet Stresses”, Trans. ASME, Vol. 78,1956, pp. A-468-473.

(5) Boon, G.B. and Walsh, R.A., “Fixed Tubesheet Heat Exchangers”, Trans. ASME, Vol. 86, SeriesE, 1964, pp. 175-180 (See also Gardner, K.A., discussion of above, Trans. ASME, Vol. 87, 1965,pp. 235-236).

(6) Gardner, K.A., ‘Tubesheet Design: A Basis For Standardization”, Proceedings of the FirstInternational Conference on Pressure Vessel Technology: Part 1, Design and Analysis, pp.621648 and Part Ill, Discussion, pp. 133-135, ASME, 1969 and 1970.

(7) Chiang, CC., “Close Form Design Solutions for Box Type Heat Exchangers”, ASME75WA/DE-15.

(8) Hayashi K. “An Analysis Procedure for Fixed Tubesheet ExchanInternational Conference on Pressure Vessel Technology: Part 1,

ers”%,

Proceedings’of the Third

Inspection, pp. 363373, ASME, 1977.nalysis, Design and

,, (9) lM&k, R.G.1 “A New Approach to Exchanger Tubesheet Design”, Hydrocarbon Processing, Jan.

(10) Sfyh, K.P., “Analysis of Vertically Mounted Through-Tube Heat Exchangers”, ASME77 PGC-NE-19, Trans. ASME, Journal of Engineering for Power, 1978.

The allowable tube stresses and loads presented in Paragraph RCB-7.2 are intended for use with ananalysis considering only the peripheral tubes. These allowable stresses and loads can be modified ifthe tubes at the interior of the bundle are included in the analysis. Engineering judgement should beused to determlne that the bundle can adequately stay the tubesheets against tensile loadings andremain stable against compressive loadings.



RGP-RCB-7.4 TUBE HOLES IN TUBESHEETS

RGP-RCB-7.43 TUBE HOLE FINISH

Tube hole finish affects the mechanical strength and leak tightness of an expandedtube-to-tubesheet joint. In general:

(I) A rough tube hole provides more mechanical strength than a smooth tube hole. This isinfluenced by a complex relationship of modulus of elasticity, yield strength and hardnessof the materials being used.

(2) A smooth tube hole does not provide the mechanical strength that a rough tube holedoes, but it can provide a pressure tight joint at a lower level of wall reduction.

(3) Very light wall tubes require a smoother tube hole finish than heavier wall tubes.

(4) Significant longitudinal scratches can provide leak paths through an expandedtube-to-tubesheet joint and should therefore be removed.

RGP-RCBJ.5 TUBE WALL REDUCTION

The optimum tube wall reduction for an expanded tube-to-tubesheet joint depends on a number offactors. Some of these are:

(1)(2)(3)

(4)

(5)(6)

(7)

(6)

(9)

(19)

(11)

(12)

Tube hole finish

Presence or absence of tube hole serrations (grooves)

Tube hole size and tolerance

Tubesheet ligament width and Is relation to tube diameter and thickness

Tube wall thickness

Tube hardness and change in hardness during cold working

Tube O.D. tolerance

Type of expander used

Type of torque control or final tube thickness control

Function of tube joint, i.e. strength in resistance to pulling out, minimum cold work for corrosionpurposes, freedom from leaks, ease of replacement, etc.

Length of expanded joint

Compatibility of tube and tubesheet materials

RGP-RCB-7.6 TESTING OF WELDED TUBE JOINTS

Tube-to-tubesheet welds are to be tested using the manufacturer’s standard method.

Weld defects are to be repaired and tested.

Any special testing such as with halogens, or helium, will be performed by agreement betweenmanufacturer and purchaser.

RGP-RCB-9 CHANNELS, COVERS, AND BONNETS

RGP-RCB-9.21 FLAT CHANNEL COVER DEFLECTION

The recommended limit for channel cover deflection is intended to prevent excessive leakagebetween the cover and the pass partition plate. Many factors govern the choice of design deflectionlimits. Some of these factors are: number of tube side passes; tube side pressure drop; size ofexchanger; elastic springback of gasket material; effect of interpass leakage on thermalperformance; presence or absence of gasket retaining grooves: and leakage characteristics of thetube side fluid.The method shown in Paragraph RCB-9.21 for calculating deflection does not consider:

(1) The restraint offered by the portion of the cover outside the gasket load reaction diameter.

(2) Addtional restraint provided by some types of construction such as full face gasket controlledmetal-to-metal contact, etc.

(3) Cover bow due to thermal gradient across the cover thickness.



The recommended cover deflection limits given in Para raph RCB-9.21 may be modified if othercalculation methods are used whidh accomodate the eIect of reduced cover thickness on theexchanger performance.

42 Reference:

Q Singh, K.P. and Solar, AL, “Mechanical Design of Heat Exchangers and Pressure Vessel

F”\Components”, First Edition (1964) Chapter 12, Arcturus Publishers, Inc.

_.‘h RGP-RCB-1O’NOZZLES

RGP-RCB-10.6 NOZZLE LOADINGS

For purposes of desi n nozzle loads are assumed to be nedetails such loads in

8.p.IS mqutry as Indicated in Figure RGP-1%

Ii ible, unless the purchaser specificallyC -10.6.

FIGURE RGP-RCB-10.6

a------ MC

- vc6+

Since pipinvalues whtc.a

loads can impose forces and moments in three geometric planes, there is no one set ofcan be provided as a maximum by the manufacturer. Each piping load should be

evaluated as a combination of forces and moments as specified by the purchaser.

Nozzle reactions from piping are transmitted to the pressure containment wall of the heat exchanger,and could result in an over-stressed condition in this area. The effects of piping loads transmittedthrough main body flanges, supports and other components should also be considered. Forcalculation of the combined stresses developed in the wall of the vessel due to piping and pressureloads, references are listed below.

References:

(1) Welding Research Council Bulletin No. 107, “Local Stresses in Spherical and Cylindrical ShellsDue to External Loading”, K. R. Wickman, A.G. Hopper and J.L. Mershon.

(2) “Stresses From Radial Loads and External Moments in Cylindrical Pressure Vessels”, P-P.Bijlaard, The Welding Journal Research Supplement (1954-1955).

(3) “Local Stresses in Cylindrical Shells”, Fred Forman, Pressure Vessel Handbook Publishing, Inc.

(4) Pressure Vessel and Piping Design Collected Papers, (1927-1959) The American Society ofMechanical Engineers, “Bending Moments and Leakage at Flanged Joints”, Robert G. Blick.

(5) ASME Boiler and Pressure Vessel Code, Section Ill, “Nuclear Power Plant Components”.

(6) Welding Research Council Bulletin No. 198, “Secondary Stress Indices for Integral StructuralAttachments to Straight Pipe”, W.G. Dodge.

(7) Welding Research Council Bulletin No. 297, “Local Stresses in Cylindrical Shells Due To ExternalLoadinand E.8

s on Nozzles-Supplement to WRC Bulletin 107, J.L. Mershon, K.Mokhtarian, G.V. RanjanRodabaugh.

RGP-RCB-11 END FLANGES AND BOLTING

RGP.RCB-11.5 LARGE DIAMETER LOW PRESSURE FLANGES

When designing a large diameter, low pressure flange, numerous considerations as described inAppendix S of the Code should be reviewed in order to reduce the amount of flange rotation.Another point of consideration is the fact that this type of flange usually has a large actual bolt area



282

compared to the minimum requiraci area; the extra bolt area combined with the potential bolt stresscan overload the flange such that excessive deflection and permanent set are produced. Methodsare available to determine the initial bolt stress required in order to achieve a leak-free bolted joint.Once the required bolt stress is known, flange rotation and stress can then be calculated and, ifnecessary, the designer can take further action to reduce rotation and/or stresses.

RGP-RCB-11.6 BOLTING-ASSEMBLY AND MAINTENANCE

The following references may be used for assembly and maintenance of bolted flanged joints. SeeParagraphs Ea.24 and Ea.25

References:(1) Torque Manual. Sturtevant-Richmont Division of Ryeson Corp.

(2) Crane Engineering Data, VC-19OOB, Crane Company.

RGP-RCB-11.7 PASS PARTITION RIB AREA

Gasket pass partition rib area contributes to the required bolt load, therefore, its effects should beconsidered in the design of flanges. One acceptable method to include rib area is shown below.Other methods are acceptable.

Y’ = Y value of pass partition rib(s)*

n’ = mfactor of pass partition rib(s)*

b r = Effective seatingwidth of pass partition rib(s)*

r ( = Total length of pass partition rib(s)*

Pass Partition

IJ,,andW,,= As defined in ASME CodeSection VIII, Division 1Appendix 2 and modified below.

W m2= bnGY+b,r,Y‘

H,= ZP[bnGm+b,r,m’]

Seating width ofPartition Rib (N)

H = (G)*(P)(O.7854)

W”ll = H+H,

*Note:

(1) mand Yvalues for peripheral portion of gasket may be used if greater than m ‘& Y ‘.

(2) mand Y values are listed in ASME Code Section VIII Div. 1, Appendix 2 Table 2-5.1 or asspecified by gasket manufacturer


RGP-T-2 FOULING


RGP-T-2.1 TYPES OF FOULINGCurrently five different types of fouling mechanisms are recognized. They are individually complex,often occurring simultaneously, and their effects may increase pressure drop, accelerate corrosionand decrease the overall heat transfer coefficient.

(1) Precipitation Fouling

Crystallization is one of the most common types of preci itation fouling. It occurs in manyprocess streams, cooling water and chemical streams. 8rystallization scale forms as the resultof over-saturation of a relatively insoluble salt. The most common, calcium carbonate, forms onheat transfer surfaces as a result of the thermal decomposition of the bicarbonate ion and thesubsequent reaction with calcium ions.

(2) Particulate Fouling

Sedimentation is the most common form of particulate fouling. Particles of clay, sand, silt, rust,etc. are initially suspended in the fluid and form deposits on the heat transfer surfaces.Sedimentation is frequently superimposed on crystallization and possibly acts as a catalyst forcertain types of chemical reaction fouling.

(3) Chemica; keaction Fouling

Surface temperatures and theP.

resence of oxidation promoters are known to significantlyinfluence the rate of build up o thtsfoultng type. Coking, the hard crust deposit of hydrocarbonsformed on high temperature surfaces, is a common form of this type of fouling.

(4) Corrosion Fouling

Iron oxide, the most common form of corrosion product, is the result of an electrochemicalreaction and forms as a scale on iron-containing, exposed sutfaces of the heat exchanger. Thisscale produces an added thermal resistance to the base metal of the heat transfer surface.

(5) Biological Fouling

Organic material growth develops on heat transfer surfaces in contact with untreated water suchas sea, river, or lake water. In most cases, it will be combined or superimposed on other typesof foulmg such as crystallization and sedimentation. Biological growth such as algae, fungt,slime, and corrosive bacteria represent a potentially detrimental form of fouling. Often thesemicro-organisms provide a sticky holding medium for other types of fouling which wouldotherwise not adhere to clean surfaces.

RGP-T-2.2 EFFECTOF FOULING

There are different approaches to provide an allowance for anticipated fouling in the design of shelland tube heat exchangers. The net result is to provide added heat transfer surface area. Thisgenerally means that the exchanger is oversized for clean operation and barely adequate forconditions just before it should be cleaned. Although many heat exchangers operate for yearswithout cleaning, it is more common that they must be cleaned periodically. Values of the foulingresistances to be specified are intended to reflect the values at the point in time just before theexchanger is to be cleaned. The maior uncertainty is the assignment of realistic values of the foulingresistances. Further, these thermal resistances only address part of the impact of fouling as there isan increase in the hydraulic resistance as well; however, this is most often ignored. Fouling iscomplex, dynamic, and in time, degrades the performance of a heat exchanger.

‘~, ,“‘:, The use of thermal resistance permits the assignment of the majority of the fouling fo the side wherefouling predominates. It also permtts examination of the relative thermal resistance mtroduced by the

‘~ different terms in the overall heat transfer coefficient equation. These can signal, to the designer,where there are potential design changes to reduce the effect of fouling. It also permits thedetermination of the amount of heat transfer surface area that has been assigned for fouling. Higherfouling resistances are sometimes inappropriately specified to provide safety factors to account foruncertainties in the heat transfer calculation, the actual operatinexpansion. These uncertainties may well exist and should be re1

conditions, and/or possible plantected in the deagn, but they should

not be masked in the fouling resistances. They should be cleariy identffied as appropriate factors inthe design calculations.



Another inappropriate ap roach to heat exchanger design is to arbitrarily increase the heat transfersurface area to allow for ouling. This over-surfacing avoids the use of the appropriate foulingPresistances. In effect, the fouling for the exchanger is combined and no longer can be identified asbelonging to one side or the other.In order to examine the effect of fouling on the pressure drop, it is necessary for the purchaser tosupply the anticipated thicknesses of each of the fouling layers.

RGP-T-2.31 PHYSICAL CONSIDERATIONSA) Properties Of Fluids And Usual Propensity For Fouling

The most important consideration is the fluid and the conditions when it produces fouling.At times, a process modification can result in conditions that are less likely to causefouling.

B) Surface And Bulk TemperaturesFor many kinds of fouling, as the temperatures increase, the amount of fouling increases.Lower temperatures produce slower fouling build-up and deposits that often are easier toremove.

C) Local VelocitiesNormally, keeping the velocities high reduces the tendency to foul. Velocities on the tubeside are limited by erosion, and on the shell side by flow-induced vibration. Stagnant andrecirculation regions on the shell side lead to heavy fouling.

D) Tube Material, Configuration And Surface FinishThe selection of tube material is significant when it comes to corrosion. Some kinds ofbiological fouling can be lessened by copper-bearing tube materials. There can bedifferences between finned and plain tubing. Surface finish has been shown to influencethe rate of fouling and the ease of cleaning.

E) Heat Exchanger Geometry And OrientationThe geometry of a particular heat exchanger can influence the unfformlty of the lows onthe tube side and the shell side. The ease of cleaning can be greatly influenced by theorientation of the heat exchanger.

F) Heat Transfer ProcessThe fouling resistances for the same fluid can be considerably different depending uponwhether heat is being transferred through sensible heating or cooling, boiling, orcondensing.

G) Fluid Purity And Freedom From ContaminationMost fluids are prone to have inherent impuriiies that can deposit out as a fouling lsyer, oract as catalysts to the fouling processes. It is often economically attractive to elimrnatethe fouling constituents by filters.

H) Fluid Treatment To Prevent Corrosion And Biological GrowthFluid treatment is commonly carried out to prevent corrosion and/or biological growth. Ifthese treatments are neglected, rapid fouling can occur.

I) Fluid Treatment To Reduce FoulingThere are additives that can disperse the fouling material so it does not deposit. Addftivesmay also alter the structure of the fouling layers that deposit so that they are easilyremoved. The use of these treatments is a product quality and economic decision.

J) Cathodic ProtectionOne of the effective ways to reduce the possibility of corrosion and corrosion fouling is toprovide cathodic protection in the design.



K) Planned Cleaning Method And Desired Frequency

It is important that the cleaning method be planned at the design stage of the heatexchanger. Considerations in design involving cleaning are whether it will be doneon-line, off-line, bundle removed or in place, whether it will involve corrosive fluids, etc..Access, clearances, valving, and piping also must be considered to permit ease ofcleaning. The cleaning method may require special safety requirements, which should beincorporated in the design.

L) Place The More Fouling Fluid On The Tube Side

There are two benefits from placing the more fouling fluid on the tube side. There is lessdanger of low velocity or stagnant flow regions on the tube side, and, it is generally easierto clean the tube side than,the shell side. It is often possible to clean the tube side withtfyfexchanger rn place whrle it may be necessary to remove the bundle to clean the shell

RGP-T-2.32 ECONOMIC CONSIDERATIONS

Planned fouling prevention, maintenance and cleaning make possible lower allowances forfouling, but do involve a commitment to ongoing costs. The amount and frequency ofcleaning varies considerably with user and operation.

The most si nificantthat should % ,d”

rameters involved in deciding upon the amount of fouling allowancee prow ed are the operational and economic factors that change with time.

New fluid treatments, changing first costs and operating costs, different cleaning proceduresand the degree of payback for longer periods of being on stream should be some of the itemsevaluated in determining an appropriate fouling resistance. Failure to include the economicconsiderations may lead to unnecessary monetary penalties for fouling.

Companies concerned about fouling continually monitor the performance of their heatexchangers to establish fouling experience and develop their own guidelines for determiningthe appropriate fouling resistance to specify when purchasing new equipment.

Almost every source of cooling water needs to be treated before it is used for heat exchangerservice. The treatment ranges from simple biocide addition to control biological fouling, tosubstantial treatment of brackish water to render it suitable for use. The amount of treatmentmay be uneconomical and substitute sources of cooling must be sought. With today’stechnology, the quality of water can be improved to the point that fouling should be undercontrol as long as flow velocities are maintained and surface temperatures controlled.

RGP-T-2.4 DESIGN FOULING RESISTANCES (HR FT2 0 F/Btu)

The purchaser should attempt to select an optimal fouling resistance that will result in a minimumsum of fixed, shutdown and cleaning costs. The following tabulated values of fouling resistancesallow for oversizing the heat exchanger so that it will meet performance requirements withreasonable intervals between shutdowns and cleaning. These values do not recognize the timerelated behavior of fouling with regard to specific design and operational characteristics of particularheat exchangers.


1


Fouling Resistances For Industrial Fluids

Fuel Oil #2Fuel Oil #6Transformer OilEngine Lube OilQuench Oil

Gases And Vaoors:

0.0020.0050.0010.0010.004

Manufactured Gas 0.010Engine Exhaust Gas 0.010Steam (Non-Oil Bearing) 0.0005Exhaust Steam (Oil Bearing) 0.0015-0.002Refrigerant Vapors (Oil Bearing) 0.002Compressed Air 0.001Ammonia Vapor 0.001

CO 2 Vapor 0.001

Chlorine Vapor 0.002Coal Flue Gas 0.010Natural Gas Flue Gas 0.005

‘Z’

Liquids:Molten Heat Transfer SaltsRefrioerant Liouids

0.0005IO.001

Hydraulic Fluid 0.001Industrial Organic Heat Transfer Media 0.002Ammonia Liquid 0.001Ammonia Liquid (Oil Bearing) 0.003Calcium Chloride Solutions 0.003Sodium Chloride Solutions 0.003

CO 2 Liquid 0.001

Chlorine Liquid 0.002Methanol Solutions 0.002Ethanol SolutionsEthylene Glycol Solutions

IO.002(0.002 -



Fouling l&stances For Chemical Processing StreamsGases And Vapors:

Acid Gases 0.002-0.003Solvent Vapors 0.001Stable Overhead Products 0.001

Liquids:MEA And DEA Solutions 0.002DEG And TEG Solutions 0.002Stable Side Draw And Bottom Product 0.001-0.002Caustic Solutions 0.002Vegetable Oils 0.003

Fouling Resistances For Natural Gas-Gasoline Processing StreamsGases And Vapors:

Natural Gas 0.001-0.002Overhead Products 0.001-0.002

Liquids:Lean Oil 0.002Rich Oil 0.001-0.002Natural Gasoline And Liquified Petroleum Gases 0.001-0.002



Fouling Resistances For Oil Refinery Streams

1 Crude And Vacuum Unit Gases And Vaoors:

Atmospheric Tower Overhead Vapors

Light Naphthas

Vacuum Overhead Vapors

Crude And Vacuum Liquids:

Crude Oil

0.001

0.001

0.002

Oto250”F 250 to 350 ’ FVELOCITY FT/SEC VELOCITY Fl-/SEC

c2 2-4 >4 <2 2-4 >4

DRY 0.003 0.002 0.002 0.003 0.002 0.002

SALT* 0.003 0.002 0.002 0.005 0.004 0.004

DRY

SALT*

350 to 450 o F 450 0 F and overVELOCITY FT/SEC VELOCITY FT/SEC

<2 2-4 >4 <2 2-4 24

0.004 0.003 0.003 0.005 0.004 0.004

0.006 0.005 0.005 0.007 0.006 0.006

I *Assumes desalting @ approx. 260 o F I

Gasoline IO.002

Naphtha And Light Distillates 0.002-0.003

Kerosene

Light Gas Oil

Heavy Gas Oil

Heavy Fuel Oils

Asphalt And Residuum:

Vacuum Tower Bottoms

Atmosphere Tower Bottoms

Cracking And Coking Unit Streams:

Overhead Vapors

Light Cycle Oil

Heavy Cycle Oil

Light Coker Gas Oil

Heavy Coker Gas Oil

Bottoms Slurry Oil (4.5 Ft/Sec Minimum)

Light Liquid Products

0.002-0.003

0.002-0.003

0.003-0.005

0.005-0.007

IO.010

IO.007

0.002

0.002-0.003

0.003-0.004

0.003-0.004

0.004-0.005

0.003

0.002



Fouling Resistances For Oil Refinery Streams- continuedCatalytic Reforming, Hydrocracking And Hydrodesulfurization Streams:

Reformer Charge 0.0015

Reformer Effluent 0.0015Hydrocracker Charge And Effluent* 0.002

Recycle Gas 0.001

Hydrodesulfurization Charge And Effluent* 0.002

Overhead Vapors 0.001

Liquid Product Over 50 ” A.P.I. 0.001

Asphalt 0.005

Wax Slurries* 0.003

Refined Lube Oil 0.001

*Precautions must be taken to prevent wax deposition on cold tube walls.

Visbreaker:

Overhead Vapor 0.003

V i s b r e a k e r B o t t o m s 0.010

Naphtha Hydrotreater:

Feed 0.003

Effluent 0.002

Naphthas 0.002Overhead Vapors ~0.0015



Fouling Resistances for Oil Refinery Streams - continuedCatalytic Hydro Desulfurizer:

Charge

Effluent

H.T. Sep. Overhead

Stripper Charge

Liauid Products

0.004-0.005

0.002

0.002

0.003

n~nn7

HF Alky Unit:

Alkylate, Deprop. Bottoms, Main Fract. OverheadMain Fract. Feed 0.003

All Other Process Streams IO.002

Fouling Resistances For Water

If the heating medium temperature is over 400 a F and the cooling medium is known to scale, theseratings should be modified accordingly.


A

A~custi~‘&&nce Or’Coupling. ................ :........................ 95, 117Air Teet.. ........................................................................................ .24Allowable Working Pressure of Tubes.. ..................... 233, 234, 235Alloy, TEMA Definition.. ................................................................ .23Alloy Clad Tubesheets.. .......................................................... .a, 74Alloy Shells. Minimum Thickness.. ............................................... .3*Anodes ...........................................................................................26Area.

Bundle Entrance and Exit.. ..................................... .35, 274-278Segments of Circles ............................................................. ,248

ASME Cede Data Reports ........................................................... .f4

B

B Class Heat Exchanger, Definition.. ........................................... .23Backing Devices ...................................................................... 38. 39Baffles and Support Plates ............................................................ 31

cross, Clearances.. .......................................................... .a, 32Cross, Minimum Thickness.. ............................................ .32, 33cuts ........................................................................................ .3fH&as.. ............................................................................. .31, 122Impingement.. ......................................................................... .35Longitudinal .................................................... .... ............... ,33Spacing .............................................................................. 33, 34Special Ca*e*. ........................................................................ .34Special Precautions.. ..... ........................................................ .33Type.. ..................................................................................... 31

Bolted Joints ................................................................................. .19Bolting,

Dimensional Data.. ........................................... ........... .188. 189End Flanges.. ......... .._ .............................................. 93, 261. 262Foundation.. ............................................................................. fi’internal Floating Head.. .................................................... .38, 39Pass Rib Area.. ......................... ........................................... .282Size and Spacing.. .................... ............................................. .93Tightening.. ............ .................. ..... ........ ..... ............... ......... 19Type ............................. ........................................................... 94

Bundle Cleaning ........................ .... ......................... ............. ,21. 22Bundle Entrance and Exit Area.. .............................. ................... ,35Bundle Hold Down.. .................. ..... ....................................... ,36, 37By-Pass Valves.. ............................................................................ 16

c

C Class Heat Exchanger, Definition.. ........................................... .23Cast Iron, Service Limitation ........................................................ .25Channel Covers.. .......................................................... 88, 280. 28,Channel Cover Formula.. ....................... .._ .................................... 90Channel Cover Grooves.. ................................. ... ..... ............... .9oChannel Pass Partitions ......................................................... .88. 89Channels, Minimum Thickness .................................................... .98Channels, Type Designation &Size Numbering ........................ 1, 2Circular Rings and Discs,

Weights cf.. ............................................................. ...... 242.247Cirdular Segments. Areas of .......................................... ..... ..... ,248Cleaning Heat Exchangers.. ................ ............................. 18, 2,. 22Cleanliness. Inspection.. .................................. .......... ........... .f5, 19Cleanliness Provisions .................................................................. t7Clearance. cross Baffles & support Plates .................................. 32Clearance, Wrench & Nut.. ........ ......................................... . 88, 189Code Data Reports.. .................. .................................. ................ f4Compressibility Charts. Gener&zed Gas.. ..... .......... 156, 157, 158Compressibility, Gas.. ........................................ ........................ ,150

INDEX

Connections,Pressure Gage.. ......... ............................... ... ..... ............. .aProtection.. ................................................. .. .. ... ... 17Stacked Units.. .................................................................. .91. 92Thermometer.. ....................................................................... :.9;Vent and Drain.. ................................................................ .56. 91

Consequential Damages.. ............................................................ .14Construction Codes.. .................................................................... ,23Conversion Factors............................................. 169. 175. 249, 250Correction Factors for Mean Temperature

Difference.. ..................................................................... 134.146Correction Factors for Bolting Moment.. ...................................... ,93Corrosion and Vibration.. ............................................................... 14Corrosion Allowance.. ............................................................. .24, 25Counterflow Exchangers ............................................ 127. 133, 147COVXS,

Channel.. ................................................................. 88, 280, 28,Floating Head ............................................................. 40Shell ....

.38, 39.............................................................................. ...... .31

Critical Properties ............................................................... ,152. 182cross Baffles.. .......................................................................... .31-34

D

Damages, Consequential .., ........................................................... 14Data Reports.. ........................ ........................... .. .... .. ................ 14Defective Parts.. ......................................................... .. .......... .f4Definitions ........ _. ........................................................... .......... .... 10Density

Gases.. .......................................................... 150, 156, 157, 158Liquids.. .............................. .................................. 150.154,,55

Design Conditions.. ........................................................................ 16Design Pressures .......................................................................... 23Design Temperatures.. ............................................................. ... .24Diameters.

Baffle and Support Plate, Tube Holes 31Tubesheet Holes . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 0. 7,

Dimensions.Bolting.. .................. .. .... .. ............................. .. .188, 1.39Finings, Welding.. ........ .... ................................................ 165Flanges. ASME.. ........................................................... ,186. 187Pipe, Welded and Seamless ................................................. 184Tubing.. ................................................... .. .. ..... ,230. 231

Dirt Removal.. ............ ........... ........................................ 17Disassembly for Inspection ..... ..................................................... 20Dismantling Ctearance .......................................... ... .... ........ ... 17Double Tubesheets.. ................................... ............................ .55-eDrain Connections.. .......................................................... .18. 56, 91Draining Exchangers ......... .. ........................... .... ... .f6. 20Drawings.. ............................................................................... .13. 14Drift Tolerance, Tube Hole Drill.. ......................... ................... 72, 73Drilling Tolerance. Tubesheets .................................................... .71

E

Elasticity. Modulus of.. .................................... ................... ,236, 237End Flanges.. ................................................... ,25. 93, 94, 28,. 282Entrance & Exit Areas. Tube Bundles.. ........................ .35. 274.278Exchangers (See Heat Exchanger)Expansion Joints, Shell ................................................................ .62Expansion. Mean Coefficients of Thermal .......................... 238, 239Expanded Tube Joints.. ........................................... .22. 72, 73, 280

Standards of the Tubular Exchanger Manufacturers Association 291

INDEX

F

Fabrication Inspection .................................................................. .I3Fabrication Tolerances.. .............................................................. .6-9Facilities for Cleaning Heat Exchangers.. .............................. .21, 22Finish. Tube Holes ................................................................. 70, 280Fittings. Dimensions of Welding.. ............................. ................. ,185Fixed Tub&wets ........................................................ 46. 53. 62-70Flanges,

End ............................................................ 25, 93. 94, 281. 282ASME Standard.. .................... .............. ... ........ ......... ,186. 187Bolt Clearances ...... ............... ..................................... ,188, 189Split Type.. .............................................................................. .92PressureTemperature Rating .................................... 190-229Protection.. ................. ............ ............................................... .I5

Flexible Shell Elements.. ......................................................... .75-88Floating Heads ............................................................................... 38

Backing Devices.. ............................................................. .38, 39Packed.. ...................................................................... .40, 41, 42,nterna, ......................................................................... 38, 39, 40Nomenclature ................ .......... ........................... ................... .3Outside Packed.. ........... .......... ................................. ,40. 41, 42Packed Lantern Ring ............................................................... 42Tube Sundie Supports.. .......................................................... .40

Floating Tubesheet.. ..................................... . ................... .21, 53. 55Fluid Density ............................................................... 150. 154. 158Fluid Temperature Relations.. ............................................ ,126. 127Fouling.

Economics of.. ............................ .............. .................. .t26. 285Effect of .............. ................................................. 125. 283, 284Indication of ............................................................................. 19

Fouling Resistance.Chemical Processing Streams.. ................... ......... ........... ,287Industrial Fluids ..................................................................... 286Natural Gas-Gasoline Processing Streams.. ....................... ,287Oil Refinery Streams ........................................... ,288. 289, 290water.. .................................................................................... 290

Foundation Bolts ............................................................................ 17Foundations ................................................................................... 17

G

Gages, Standard Diameters.. ............... ....................................... .27Gaskets (Peripheral & Pass Partition) ......................................... ,43

Material.. .... ............................... i.. ...........................................43Replacement.. ......... ............................................................... .22Joint D&&s ...................................................................... .43, 44

General Construction Features.. ............................................ .15. 16Generalized Compressibility Chats.. ......................... 156, 157, 158Grooved Channei Covers.. ........................................................... .90Grooved Tube Holes ...................................................... ............. .7tGrooved Tubesheets.. .................................................................. .74Guarantees ......... ................................................................... .14, 15

H

Handling Tube Bundles ................................................................ .21Hardness Conversion T&la.. ..................................................... ,232Heat Content Petroleum Fractionr.. .................................... 151, 167Heat Exchanger Arrangement Diagrams, .................................... 2-5

parts and Nome”ciature.. ................................................. .3, 4, 5Standard Dimension Tolerance ............................................ .5-9

Heat Transfer.. ..... ......................... ............................................ ,124Heat Treatment, V-Tubes.. ........................................................... .28

I

Holes. ............................................................................................ .70Baffles and Support Plates.. ............................................ 31, 122Diameter and Tolerance, Tube.. .. ................................... ,70, 71Finish, Tube.. .................................................................. .70, 280Grooving ................................................................................. .71

Hydrostatic Test Pressure.. .......................................................... .23

Impingement Baffles,Bundle Entrance and Exit Areas.. .......................................... .35Protection Requirements.. ...................................................... .35Shell and Tube Side.. .............................................................. 35

Inspection, Cleanliness.. ......................................................... .t5, 19Inspection, Fabrication ....................................................... ......... ,13Installation of Heat Exchangers ............................................. .t7, 18Internal Floating Heads .................................................... ,38. 39. 40

J

Jacketed Gaskets ......................................................................... .43Joints,

Bolted.. .................................................................................... .I9Packed, Service Limitations.. ..................................... .a. 41, 42

K

Kettle Type Reboiler, Typical Illustration 2, 5

L

Latent Heats of Various Liquids ................................................. .168Leaks, Locating.. ..................................................................... .20. 21Leveling Heat Exchangers ........................................................... .I7Lifting Devices................................................................ 16, 269.272Ligaments, Tubesheets Minimum.. .................................. .70, 72, 73Load Concentration Factor, Flanges............................................. 93Longitudinal Balfles ...................................................................... .33

M

Material Warranties.. y.............. ....................................................... 14Materials- Definition of Terms ....................................................... 23Mean Coefficients of Thermal Expansion.. ......................... 2338, 239Mea,, Metal Temperature ..................................... 24, 128, 129, 130Mean Temperature Difference.. ................................. 126, 127, 133

(See also MTD)Metal Resistance, Finned & Bare Tubing.. ................................. 125Metal Temperature Limitations.. ................................................... .24Minimum Inside Depth Channels & Bonn&. .............................. .88Minimum Inside Depth Floating Heads.. ...................................... .38Modulus of Elasticity.. ............. ............................................ 236. 237MTD Correction Factors.. .................................................... 134-146

292 Standards of the Tubular Exchangei Manufacturers Association

430

Name P,?h ..................................................................................13Natural Frequencies. Tubes.. ....................................................... .97

0Nomenc,e,“re of tieat Exchanger Components.. .......................... .3Ncl?le”c,e,“,e ................................................................................ 1-S

Q, Nozzles,Connections ............................................................................. 91

GFloating Head .......................................................................... 40Loadings ........................................................... ............. .9*, 281

QaSplit Flanges ............................................................................ 92

Number and Size of Tie Rods.. .... ......................... ............... .35. 360

h3 0

8Operation of Heat Exchangers.. ............................................. .18. 19Operating Procedures ............................................................ .1.9. 19

8Outside Packed Floating Heed.. .. ................................... .4O, 41, 42

8 p0 ,,,~,,~ ,,,a

Packed Floating Heads ........ ............................................ .4O, 41, 42

6Pecking Boxes .................................................................. .26, 40. 4,Packing Material ............................................................................ 42

aParts, Replacement.. .............................................................. .15, 22Pass Partition Grooves.. ......................................................... .74, 90

et:Pass Partition Plates .............................................................. .88, 89Pass Partition Rib Area.. ............................................................. 282

QPerformance Failures .................................................................... 17Performance Guarantees.. ............. ............................................. ,I4

dPeriodic Inspection.. ................................................................ 19, 20Physical Properties of Fluids.. ......................... .......................... .15O

8Pipe,

Dimensions of Welded and Seamless.. ............................... ,184

Q Shells ....... ............................................................................... SOPipe Tap Connections .................................................................. ,91

0 Piping Loads ......................................................................... .92, 281Pitch, Tubes ......................... ..................................................

Q .,

,28, 29Plate, Shells.. ................................................................................. 30

0Plugging Tubes in Tube Bundles.. ....................................... .22, 273Postweld Heat Treatment.

0Floating Heed Covers.. ........................................................... .38Channels and Bonnets.. .......................................................... 89

GPreparation of Heat Exchanger for Shipment.. ............................ .I5Pressure Gage Connection.. ... .................................................... .91

@Pressure LOSS .............................................................................. 126Pressure-Temperature Ratings for Valves, Fittings,

dand Flanges.. ................................................................. 190.229

Pressure, Tube Working.. .................................................... 232.235

e Protection.

& ,~Impingement.. ......................................................................... .35Shipment.. ............................................................................... .lS

Pulling Mechanisms.. ............................................................... 21. 74

Q Pulsating Fluids ....................................................................... 18, 89

c

0R Class Heat Exchanger, Definition.. ......................................... .zSRatings. Valves. Fittings. and Flanges

0(See Pressure-Temperature Ratings)

Rebailer, Kettle Type. Illustration.. ................................................. ,5

r3 ‘,Recommended Good Practice, RGP Section ............................. 252Replacement Parts.. ..................................................................... .I5

6 Removing Tube Bundles .............................................................. .2tRing Flanges, Split.. .................................................................... .92

Q Rings, Weights cf.. ............ .................................................. 242.247

INDEX

Safety Relief Devices .................................................................... 18Sealing Devices ............................................................................. 36Seamless Pipe, Dimensions of .................................................. ,184Segments, Circular.. ................................................................... ,248Seismic Design .............................................................. 16. 255268Shell Covers. Minimum Thickness.. .............................................. 31Shells,

Diameters.. ............................................................................... SOIllustrations.. ........................................................................... .2-SLongitudinal Stress.. ......................................................... .67. 68Minimum Thickness.. .............................................................. .30Size Numbering &Type Designation.. ................................. .I. 2Tolerances ............................................................................... SO

Shipment, Preparation of Units .................................................... .t5Shop Operation.. ............................................................................ 13Shuttfng Down Operation.. ............................................................ 18Size Numbering of Heat Exchangers .............................................. 1Spacers and Tie Rods.. .......................................................... .35, 36spare Parts.. ..................................................................... ,lS, 22, 44Specific Gravity, ........................................................................... 150

Hydrocarbon Liquids ....................................................... 54. t 55Specific Heat ........................................................................ 150, 151

Gases, Miscellaneous, Atmospherio Pressure.. .................. ,165Gases et High Pressure.. ..................................... 150. 151, 166’Hydrocarbon Gases,

Atmospheric Pressure.. .......................... 150, 161, 162, 153Liquids, Miscellaneous .................................................. 150. 164Petroleum Fractions. Liquid ...................... .................. ,150. 159Petroleum Fractions. Vapor ......................................... ,150, 160

Specification Sheet, Exchanger ............................................. .1t, 12Split Type Nczzle Flanges.. .......................................................... .92Stacked Units.. ........................................................................ .91. 92StertinoOoeration.. ........................................................................Stresskeieving (See Postweld Heat Treatment)

t*

support Plates,HCl0S.. ......................................................................... ........... .31Spacing.. ...... ............................................................ 33, 34, 121Thickness.. ... .................................................................... .32, 33

supports.. .................. ..................................... .6, 7, 15, 15. 253-268

T

Temperature,Limitations, Mete.. .......................... ...... ..... .. .. .. ....... .24Multipass Flow.. .................................................................... ,127Shocks ..................................................................................... 19

Temperature Efficiency, ......................................................... 27, 128Counterflow Exchangers.. .................................................... ,1471 Shell Pass.. .......... ........................... ............................... ,1482 Shelf Passes.. .................................................................... ,149

Test Connections.. .. ... ...... .................................... .... .... .... ... 18Test. Pneumatic or Liquid.. ...... .............. ............................... .23. 24Test, Standard.. ....................................................................... 23, 24Test Fling.. ...................................................................................... 21Thermal Conductivity, .......................................................... 240, 241

Conversion Factors .............................................. 169. 249. 250Gases and Vapors, Miscellaneous ............... ............ ,172Squids. Miscellaneous ............................................ -17 1Liquid Petroleum Fractions ............. ........... ... .. .. ,170Metals.. ................ ........................ ................................ ,240. 241Pressure correction.. .................................................... ,173, 174Pure Hydrocarbon Liquids.. ........................................... ...... ,170

Thermal Expansion. Mean Coefficients of, Metals.. ........ ,238. 239Thermal Performance Test.. ...................................................... .. .14Thermal Resistance of Uniform Deposits (See Fouling)Thermal Relations.. ......................................... ........................... ,124Thermometer Connections.. ..... .................................. ....... ... .... .91

F:R33

Standards of the Tubular Exchanger Manufacturers Association 293

INDEX

Thickness, Minimum,Baffles .............................................................................. .32, 33Channels and Bonnets.. ......................................................... .88Channel Covers.. .................................................... 90, 280, 281Shells and Shell Covers.. ................................................. .30 31Tubes ................................................................................. 27. 28Tubesheets .............................................................................. 45

Tie Rods and Spacers, Number and Size.. ........................... .35. 36Tolerances,

Tube Holes in Tubesheets ............................................... .70, 71Tube Holes in Baffles .............................................................. 31Heat Exchangers and Parts ................................................... S-9Shells and Shell Covers ......................................................... .30Tubesheet Drilling .............................................................. 70, 71

Tube Bundles,Cleaning.. ................. ................................................... IS. 21. 22Handling.. ................. ............................................................... 21Plugging Tubes.. ............................................................. .22, 273Removal.. .................... . ........................................................... .21SUppOrts.. ................................................................................ .40Vibration.. ................................................................... 14, 95-123

Tube Expanding.. .......................... ............................................... .22Tube Joints,

Expanded.. ..................... ................................... .22. 72, 73, 280Loads ................................................................................. 69, 70Testing. Welded.. .................................................................. ,280Welded ..................................................................................... 74

Tube Support Plate Drillkig .......................................................... .3tiSee Also Support Plates)

Tube Wall Metal Resistance........................................................ 125Tube Working Pressure, lnternai .............................. ,233. 234, 235Tubes,

Characteristics.. ............................ ............................... ,230. 231Compressive Stress ............ .................................................. .69Diameters and Gages ......... .................................................. .27Expanding.. .............................................................................. 22Finned ...................................................................................... 27Leaks .................................................................................. 20, 21Length.. ............... .... .. .. ... ..................... ........................ .27Longitudinal Stress ............................................................ 67, 68Maximum Recommended Gages .... ................... ..... .27, 72, 73Natural Frequencies ................................................................ 97Pattern.. ................... .......................................................... 28, 29Pitch ........................................................................................29Plugging in Tube Bundles ..................................... .............. ,273Projection.. .............................................................................. .73Special Prec au (0”st ................................................................. 67Tube Wtil ReducBon.. ............................ ............................. .2SOU-Tubes ....................... ............... .. ....................... 28, 96. 104Unsupported Length, Maximum.. ............................ ........ .33, 34working Pressure. ,nterna,. ...... . ........................... 233, 234, 235

Tubesheats, .................................................................................. .45. .Application Instructions & Llmltatlons ..................................... 45Applied Facings.. .................................................................... .45Clad 8 Faced Tubesheets.. .................................................... .45Divided Floating Heads.. ........................................................ .46Double Tubesheeb ........................................................... .55-62Effective Tubesheet Thickness.. .... .................... .................. .45Fixed Tubesheets .................................................. 46, 53, 62-70Fixed Tubesheets of Differing Thickness ........... ............ .66. 67Formulae,

Bending.. .................................................................... .46-49Effective Design Pressures-Floating Head (Type p). .... ..5 5Effective Differential Design Pressure.. ....... ............. .65, 66Effective Shell Side Design Pressure.. ..................... .64, 65Effective Tube Side Design Pressure.. ............................ .65Equivalent Bolting Pressure.. ..................................... .63. 64

Tubesheets, Formulae. (continued)Equivalent Differential Expansion Pressure 62, 63Flanged Extension 5 3 . 54Shear.. .................................................................. .50, 51. 52Shell Longitudinal Stress ................................... 67. 68, 279Tube Allowable Compressive Stress.. ............................. .69Tube Longitudinal Stress.. ................................ 68. 69. 279Tubeto-Tubesheet Joint Loads.. ............................ .. .69. 70

Integrally Clad.. ....................................................................... .45Minimum Thickness.. ....................................................... ...... .45Packed Floating Tubesheet Type

Exchangers.. .................................. ...................... .40. 41, 42Shell and Tube Longitudinal Stresses.. ..................... .S7, 68, 69Special Cases.. ....................................................................... .70Tube Holes in Tubesheets .................... . ...........................70. 71Tube Joints-Expanded 8 Welded.. .......................... 22, 74, 280Tubesheet Pass Partition Grooves.. ................................. .... .74Tubesheet Pulling Eyes.. ........................................................ .74

Type Designation of Heat Exchangers ...................................... .t 2

U

Unsupported Tube Length, Maximum.. ................................... 33. 34“-Tubes, ........................................................................................ 28

Rear support.. ........................................................................ .34Heat Treatment.. ...................................................................... 28

Users Note.. ................................................................................... viii

V

Vent& Drain Connections.. .............................................. .tS, 56, 91Vibratiwl, ..............................................................

Acoustic Resonance or Coupling..14, 34, 35, 95.t,23

...................... ... ...... .95. 116Mechanisms Causing ............................................................ .95Designs & Conslderabons..... . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . ,121, 122S&&d References.. ................................................... 122. 123Tube Excitation.. .................................................... .... .97, 98. 99Tube Natural Frequencies.. ........................................ .97, 98, 99Turbulent Buffeting ........................................................ 116, 117Vortex Shedding ............................................ ........ ,116

Viscosity.. .................................................................................... ,151Conversion Factors ..................... ... ........... 151. 175, 249, 250Gases 8 Vapors. Atmospheric Pressure ................ ............. 181Gases &Vapors. High Pressure.. ........ .......... . .. .._ ........ 151, 182Hydrocarbons & Petroleum Fractions ,................., ........ 176.179Liquids, Miscellaneous ........... ..... ....................... ................ 180

W

Wall Resistance, Finned & Bare Tubes.. ................................... ,125Water Fouling Resistances ..................................................... .. ,290Weights of Circular Rings & Discs ...................................... 242-247Weights of Tubing ................................................................ 230, 231Welded and Seamless Pipe, Dimensions Of.. ............................ .I84WeldedTube Joints ............................................................... 74, 280

Standards of the Tubular Exchanger Manufacturers Association

Normas TEMA

Documents

Transcript of Normas TEMA