Flour PUMP&VESSEL -.pdf

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A.

B.

C.

centrifugal

1-

Horizontal

2.

VerticaL

3.

In-1ine

Rotary

I

-

Gear

2-

cam

3

-

scre ,

Reciprocating

1. Piston

2- Plunger

(simplex

and Duplex)

3- Diaphragm

Ii.

?ump Drivers

A. Electric

motor

B.

Turblne (steam, gas,

oit)

lII-

Pump

Location

Consideratj-ons

A-

Close

to

source,

space available

and

size of

pump

1-

under

pipeway

2-

Adjacent to vessel

a- Trenches may be

requj-red

3. In tank area - outside diked area

a-

crouping

of

purl{)s

may be requi.red

b.

Avoid

direct runs from tank to

pump

suction

c. Check

tank settlement

-

affects suction

piping

clearances

1.2'-6" around

pump

(ninimum

$aIklray)

maintained by

rnanual

equipnent

Ffexibifity

Important

factor -

can affect

pu,np

location

and

vessel orientation

P3C-1-013

NIJMB ER

LESSON

9

PAGE

1

oATE

Rev.

1/80

'l'

FLUoR

P

IP INC

TRAIIIINC

)r

lluaLs

PIIASE

IIl

PI]HPS AND TURBINES



5.

B.

3.

4-

5.

6.

2.

Do

not

pocket

lines -

step continuouslY

dollrl

to

punP

3. Temporary

start-up strainers

required

4. Reducers

at

pump

nozzle

-

refer to

Fluor

standard

I,lhen

source

is

Lon,

PiPing

can

determine

elevation

of

punp

foundation

-

check

this in

your

studY.

Discharge

piping

1

. Tl'pes:

top, side

Nozzle

normally smaller

than suction

Piping

2-

Check

valve required

to

Prevent backflor,,

on

centrifugal

Pumps

not

mandatory on

positive

disPlacement

prrftps

-

Line

support

From

grade, pipe\ray,

pipeway

struts,

and

possibly separate

supports

Side

discharge

- requires more

sPace- Verify

requirements

during

PumP

study before

locating

PumP

-

vertlcal

purnps

_

orient discharge

to most

suitabte

and

econoni-

cal

focation

on sump tlpe,

verify

that

sump

is at

Proper

depth

to

accePt

pumps

Ir-1ine

pumps

Liqht

veight

pr.rmps

caD be supPorted

from

piPing;

heavy

Pumps

from

concrete

foundation

Reciprocating

pumps

Keep

discharge

pj.ping

close

to

grade,

may

require

hold-dovns

supporting

suction line6

a-

Top

suction -

normallY

b-

End and

side suction -

from

overhead

from

grade

or

from

Pump

founalation

'l'eLuon

PIPING

TRAINING

MANUALS

PHASE III

PUI'IPS

AND TIJRB]NES

NUI{BER

LESSOI

PlcE

'

DATE]

9

2

Rev-

1/80

7-

P3C-1-013



trLUOR

-:rrNG

.:N ALS

rurbine

Pir,iho

A.

steam

inlet -

checking

freezing

conditions

1.

Piping

should

come

from

9P

of

suPply

header

for

driest

steam

Possible-

2-

val.ves

located

Per

Fluor

standard

3.

Proper

suPPorts

Provided?

4.

Bootleg

Provided

for

condensate?

B.

Steafi

er<haust

1.

Line

to

toP

of

header

2-

Line(s)

stress

checked

i.

cfru"i

alrain

-

from

e:,haust

or

casing?

verify

this

fron

turbine

outline

NUMBER

LES5ON

9

pAcE 3

of 3

OAIE

Rev-

1/80

PHASE

lII

PI,I{PS

AND

IIJRBINES

P3C- t"'013



P34-

/

-o/9

s4

I

Pumps

and Turblnes

?.frrt

))

.ld-tt,

t'/i.

d'J

t1

{

I

3

a

{

9

e

o

+

tE1

r':\

s

r\

B

i

{

c

s

I

vl

ls

P./@B

Sfabrhzer

bo+foms

PumPz

FiBuro 1-'1.

Horizontal

conlrllugal

pumpg

shown on

llow

dlagram

Courtdy

ol

FIuo'

Enolne6r3

Constsuctors,

lnc.

and

q

v



+

d1

C

o

.:

o

q

E

G

o

oj

o

o-

o,

A

t

Er

Ei

o

€

o

-9

.t

-

s

PJ

ta

t-

t=

Ir

t-

-

s

s

5:

;

:

;.

3i

=

t

N

'\

N

=

-

-

PsC-/-O/'

sH,

5

Process

Piping

Deslgn

;.E

E

i

-E

=:

r

€

i;

:; i

l

;E

g;;

i= 3-ie

FeE;EEii

EE3:iF5

:.' :=

-:

EEsE iEE=

I

tr

_P,q

Effi1j

#

--

l

:le

i

t

I

:i

E

t

:

I

a

l=

l5

tl

t:

t;

li

t-

l=

I

IE

lr

t-

l6

IE

li

t;

It

E

rlr

li

2

B

a

t-

_t_t

I

ll

@I



6

lr

r

I

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I

r-1

(

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[rE

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i _or 2 E

EG

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iii::i:::::lEtE

1?1?:1::::::i

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{fi'.....r.,.1$

p

L ceee

cee

i.

d"ir.

rr:=

:::

ir :Flnt,t.++

.r.

r

litl I

I

Ele

i:

ilr;:'

;

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a

a

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9i

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il

:

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a

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is

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iz

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ti



P31-

a

a/3

Process

Plpins

D€slgn

Figure

1-32.

c,osg

seaton,

Type

vR

turdlne

Courtesy

of

Elllot

comPsny'

l r'r

; ,

jl

li'-

.-

g

r'.--'

t4:

j

.

F

-. re

1.33.

Turbino.

Courtesy

ol Elliott

Company'

Should

the

oPerating

PumJ'

l I an rmDulse

line

opens

the control

valve'

supply-

i:: sream

io the

turbine

immediately

withthistype

..a'r::siallation.

steam

traps

are

supplied

at

every

low

I}ri]lt

in

lhe

inlet

system

to

immedi:rtely

collect

any

c.:riensate

\ hich

maY

form'

i I rr bolh

manual

and

dutomatic

starl_up'

steam

1.,..

'f',r-fO

be

provided

to

keep

the

turbine

ca'int

Iter

of

condensate.

These

can

be

inltalled

either

a(

il.

*'ing

.

to"

poinL

rI

a

connection

is

provided

or

,

-

'""

",,Lt.L

oioine

'f

the

ccting

drain5

into

the

out_

l€t syslem.

The.€

must

be

rise which

*ould

form

a

would

collect.

a

trap

before

anY

vertical

pocket

where

cond€nsate

.

lnlet

BY'Pass

All

automatic

start_up

turbines

need

a l"

globc

bodv

valve

to

b)'pass lhe

control

valre

Mdn

operating

companies

insist

on

the

warm"up

b)_PdS

even

with

manual

start_uP.



Manhum

initialpr63ur.

(psr8)

. . .

... .

M.rimum

initiEr

t mpe6tu.. (.F).

.

..

.

.

yarimum

cxh.ust

pr.siur.s

(p6i8)

.. ..

.

sp..d r.ns

(rpm)...

...

Nlmb.rotstrs.s(impulseVpe).......

Numb€.

ol.o$s

ol rorating btades.

.

. .

.

.

lnletsizes

(in.)..........

l.l.t lodtion

(facing

Sovemo.)........

Lh.ust

slzc

(in.)........

Erhaust

location

(1.

H.

Siandard). .

..

..

Centedin€

heisht

(in.).

. . .

Approrim.tc

r..g.

oicapacities

(hp)-

.

. .

Approrim.tc

shlppln8 welght

(b.).

-

.

.. .

P,oc€ss Piping

Oesign

General Specificalions

7s4-/-d/3

sH.g

.ight

8

7@

750

vrc.l25

800-7000

lg

1

2

2,3&4

.ight

8

ro 14oo

r275

704

750

8CO-5760

2?

t

2

2 3,4 &6

riSht

10

t7

to

25Oo

2050

ac05o00

I

800.7350

700

750

rlght

L2

to 3500

26oO

ro

3000

2300

700

750

250

2

1

2

2,3,4

&6

2,3,4 &6

R. H.

opt'o.al

R.

H. optaonal

22

\7

S.. Butr.rin

H29ror ayRH.nd

AyiHH

d.r.it:

sr

All.rin tt32

ror AYR

d.r.it'

Approximate

Dimensions

(in

lnches)

45t/s

5tt/,

5t

t/a

555h

55./.

'ilill"?'lilil,lli'llll,TioYR.(''i'

din'|'o

aYiH md aYRaH

('

n'.n'|'o

,

Figure

1.35

App.o>imat6 drmsnsions,

othor

YR turblnes. Couri€sy

of

Elliot Company.

700

750

375

4oo.7350

t3

1

2

2,3,4&6

ight

a

17

to 30OO

2300

t2Y2

12Yz

r2Y2

t2j/2

t2t/2

t2,/"

l6'rl

t6Y.

l6t/.

l4

l7

22

t7

't7

7

at/z

12

9

9

161/,

19%

\at/.

ra.t



FUJOR

PIPIXG

TRAINIHG

rur{uALs

1.

2.

6.

SEOUENCE

FOR

RECEIVINC

CERTIFIED DI}IE}ISIONAL

OUILINE

Process

engineer

6ends

punp

calculation sheet to the

pump

mechanical

engineer- This

shouLd

be done

shortly

after

process

flov

diagrarns are

completed.

This calculation sheet contains the operating

conditions for

one

particular

6ervj.ce. the

process

engi.neer

may

aLso

request

punp

tlpe

if

he

has a

preference.

llechalical

engineer uormalLy determines

pump

tipe

ba6ed

on calculation

sheet

information-

He

fiUs in

the

I'Pump

specification Sheet-rr He will

only

fill in

information

noted

as

"to

be

corpleted

by purchaser."

3.

ltechanical engineer then selects

possible

vendorE

based

on avaifable

catalog

information.

4.

l.techanical engineer

fills

i.u

"pump

1i6t"

(6ee

attached sheet)- this

gives

Piping very

prelj.minary

information

thich

can be

used

for

plot

development or

possi-ble

p ..ulP

6tudy

work-

the

puilp

list

refers to

an

l,l-E-D- drawing nunber- This drawing

(see

attached 6heet)

provides

a

visual

picture

of

proposed

pump,

5.

llechanical engineering then

goes

ortt

"Reque6t

for

Quote"

to

several

vendors-

Each

vendor

fj.11s

in

their

portj"on

of

the

Punp

specification

sheet.

They

give

Fluor a

price,

pump

modeL, and size

r,rhich

they offer

for

that

particular

service. The vendors

send

the specification

sheets

and

quote

sheets

to Fluor

for

consideration-

tlechanj.cal

engineer $il1

seoal

revised information to Piping

if

vendor's

recomme[dation significantly inpacts

us-

ltore accurate infonnation

from

veardor

I

s catalog is noll available

-

7.

llechanical engineering

places

order

to

the selected venalor. Approximately

six to eight lreeks later Fluor

recej.ves a

C-D.o.

8.

t,Ihen

c-D-o.

is

"in-house,"

our

Vendor Data

Control

croup

eilI

send ?iping

and

other

di6ciplines

a

reference

copy-

c-D.O-

is

then routed

for

6quad

check-

Piping wonrt normally be included on the routing of the squad

check- However, ee

{ifl squad

check our reference copy and any

questions

or

problems

ve have

can

be

dj.scussed

with

the mechanical engineer- He

lhen can

include

our

corunenta ,/ith his when

he formal"ly

squad

checks

the

c.D.o.

Piping and other disciplines

wiLl

then receive a copy

of

'Isquad

check conulents" which is traEsmitted back to

vendor.

PIIASE

III

PI'T{PS

AND

TURBINES

NUI,{88 R

LESSON

9

pAG€

1

of

6

DATE

Rev. 1/80

P3C-1-014



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CENTRIFUGAL

PUMP

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PIPING

TRAINING

tIaIUALS

PHASE

III

PUTPS AND TLRBINES

NUMBER

LES5ON

9

PAGE

1 of

1

DATE

Rev-

1/80

STE?S TO

ACCOMPLTSH

PU}IP

EQUIPTEIIT

STUDY

updale

your

flo\r diagram from

|master.

1-

2.

3.

5-

6.

'1

-

8.

Cohpare

pump

outline

to flo\, diagra- (

such as

horizontal

centrifugal sho' 'n

calculate elevations-

a- ilozzles-

b.

Pump

anchor.

c.

and spec

sheet

to

surface

discrePancies

on

F.D.

and spec

sheet ca116

for

in-Iine.

a.

b-

v,lork

out

your

flexjbiLj.ty

bet\ieen

pumps

on 6cratch

Paper.

This could

determine

your

pump

spacing.

Best

guess

elevations

to

and from

other

equiPment-

Calcutate verticat

grovth.

From

force

nomograph

detennine

bend

leg

required

horizontally

betseen

pumps- Total vertical

force

on

nozzle

aLso incfudes

dead

$eight-

If

lhis creates

a

Problem.

a

spring

,

hanger

$riII

relieve dead

veight-

DetermiDe

if vertical Ieg is

adequate

to

absorb one-half

or

one_quarter

(if

you

branch from

the

center

in

hot/cold

situation)

of

tbe

growth

of

your

horizontal

Ieg

betveen

punps.

Nolg

ptunp

spacing

is

set

based

on

flexlbj.fity.

verify

this'

spacing

\'ri11

satisfy operation

and maj.ntenance

passagewaya

-

study

piping

transposition and

pj.ck pipeway

bay

that

$orks

out best

lrith

suction

source- If bay is empty of

other at

grade

piPing,

center

your

predetermiDed pump

spacing

in thal bay.

Comnence actual study-

You

nust

be accurate

and draw to

scale-

However.

don't \rorry about drafting

qualit)-,

linework,

or

lettering-

rrRough

and

di-rty

but legible

and

complete.

If

discharge

line

runs in

pipel'ay,

design

routing

so as

not

to restrict

pipeq,ay

designer

uhen he berths lines.

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PAGE

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DATE

Rev-

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PHASE

lII

TRTICAL

VESSEIS

'l'ruuon

PIPING

TRAINING

MANUALS

1.

2.

STEPS

TO

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VERIICAI

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Update

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b.

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uP

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study

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6.

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g.

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IESSE

ENGINEE:RING

DESIGN

GU,IDE

2-4.1.9

2#29

4-7A

22

9:9

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:,

qt

9

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t).in

A.

VESSEI,

ORIENTAT]ON

".:

6es6ion

is

to

help

you

becdtre

nore.failj-ILar

rrith

vegsel

orientation,

baseal

ou

Fluor

1

Thelmaterial

and.

instruction

-you

ret-dii'i

-'ffo[

this

lddi;i6;,.

iliolila"enable

you

to:

.

,1:

rj

xho ,

.ho i

,te

.

aSsirilate.:t}te.

inforuttioD

to

start

.a

-vesbel

,iiriintation

OBJEC?IVE

The

objective of this

the

Fluor approach to

Drarrings.

TBAY

TYPES

:,

2.

?roperly

piepare\orientdtirin

"iturlies

of both

vertii:al dnal horizontaL

vessels.

:

:.''

'

B.

BIIBBI,E;CAP

TRAY

ADV}NTAGES

,

I

DISADVAI{TAGES

1-

3-

I.

2.

1.

2-

3-

Very

efficient

l{eed not

be installed Leve}

"

)r: r'xr f,j'

_,i-

Corrosion

not

.a

factor

.-:.1}1,]^

.

:_.: r:1,

l,Iost

efficient

of

al1

tlpes

IDeapen6ive and

Iighhreight

Need

not

be in6tal1ed

]evel

Corrosion

not

a factor

Inexpensive

Lightweight

cood

for

heavl'

liquids

1.

2.:

4.

occasionally

1.

2-

3.

4.

1-

VAIVE TRAY

SIEVEJ TRAY

Cast iron

caps

break

ounting

bolts rust

None

l,lust

be

instafled

level

corrosion a factor

P38-1-013

Expensive



NUMEER

, PHASE, III

,j,Hofr?6ffi,ffi6sELs

c. REI{OVABLE TRAYS

D.

vessels

ln

heavy

(dirty)

.

service or

vith a high corro6ion rate

:of,ten

have

tray6

that

are

built in

sectLons- Ihese tray6 caE be dismaltled aDil

irejlovejFlhtgg[jh.tl]e

4v.es6e1

[6trho].es for

lleaDing,

repairing

or-

replacing.

i.t;.,r.i;ir,- lr,rr,

''

r.a

FIXED TRAYS

(Nonremovabl-e

)

problem

usually

E

E.

JRIEF.PROCESS

DESCRIfIIOT{ OF-

A

JTPICaL

DISTILLATI0}I

.OR

'FRACIIONATIoN

COLU}rN

Heat

for.vapor.lzation i6 6r.rpplied by

heating the crude

feeal

6tock ilr

a

furnace.l*$ilprehgated

crude

(f,eed)

is charged ilto

the'bottoD

of

the

fractionatloD

colunn onto

the feed tray at it6

boiltng

poi-nt,.at

a

pres6ure

sughtly above

atmo6pheric-

This is called

the

I'f1ash

zone.I

In

the

fLash zolre, the feeal separates

into liquial

and

vapors.

the vaPors

rise

up under the bubble-caps

and

bubble

out through

the reflux liquld

on

each

tray- The

vapors rise

through

the

col.uilrl

contacting the doi|trflowing

reflux strean at each

tray;

as a

result the

tightest material"s

concen-

trate at th€..top

of

the colunn

(overhead

vaPor).

The vapor out

the top

of

the colt n'i6

condeDsed

into

liquid

by the

o-H- conden6ar.

The liquid

is

then

acctrmulated

ilr

the o.H-

reflux

accunulator-. Part

of

the

liquid

is retumed to the column'6 top tray

as

reflux-

The

reflux flow6

across

each trgy.ro-nititq:xray dowa.

the cofulul

by say of

dosncoBers

and btrbble_caps-

rhe

poiii6ii

6i

ule ioLrann

bet$een

the

overhead

and the feed

i6 called

ttte

t'rectifying

lection-'r

Thi6 is

$here

the

cou.ntercurrettt flolt

of

reflura

and

vapor reach an. equili.brium-

This means

the

liquid

head

on

each traY

i6

just

enouqh

to allow

the vapor

to

rise through the

liquid aod

the

.

vapor

.ve1ocity,.:isr,:iust

fast enough to allolt

sone

of the liquid

to

droP

through

the

same opening ilr the

tray. The

heavier

materials

concentrate

at

the bottom of

the

column

(bottoms

)

and the intermediate

materials

in-bet\reen- De6ired

"6ide

cut"

products

are \rj.thdralrn

at

aPpropriate

1eve1s

(drar,-off6).

The

portion

of

the

column

betreen

the feed and the

botton

tray

is

calLed

the

"Etrippihq

section.t' This

is

\,rhere

additional

light

haterial-.

are

relea6ed

a6

vapor

(6tripped)

from

the

beavier

liquid

portion

of

the

feed

by

the

addition of

stripping stean ioto

the

Isurge

section'

of

the

column-

The

portion

of the

feed that reaches

the

bottom

of the vessel

is

the residue or bottoms

liquid.

fhe top tray must

be

continuously

fed

lrith coollDg

reflux

liqui.d or

the

trays vould

soon become

dry-

Reflux must

be

increased

as side cuts

are

dlra\am

off

at several

1eve1s-

Thd

inateriaL on

each tray is at its

boiling

point

and the dollnflowing

material

is

constantly

changinq

composition

as

it

picks

up heat from

the

rising vapors. The

vapor is

always

hotter

than

.the

liquid on the tray

from shich

it is rising. The

vapors

are

coDstantly

being cooled by the cooler

reflux on each

tray. The

vapor on

the

top

tray

is

condensed

into

liquid.

The

fiquid

that

is

not

returned

to

the

colum[

as ref].ux is

one finaL

product-

P B; --P13

l'.'

:.1,-.

.,Vesse16

have fl can

be steamed.but

in

place.

iirl

i

MAlqlLs



'l'rr-uoe

I

nrrrxc'

.l;1

TR^rilrNG

L |'

j

.

rUXUlt-S

' |

;

LI

r .

''yn

ri.i

r-

to

the

1.

2-

4.

5.

6-

7-

:.

10-

vessel

or

Drun Height

Process

NonBal

Instrument

NozzIe

Nozzle

liquid

Elevations

Levef

and

other

,

^|::.

Elevations

Custolner

Requirements

Ilanholes

are

generally

18 nominal

size

except for

columns

with removable

trays, in

uhiih a

savings may

be realized

by iltcieasing

the

size of the

manloIe to

permit

].arge

tray sectioD6

to be

removed.

In

those cases

generalLy

only

one

laiger rnanhole

i5

Provided,

preferably belolt

the

bottom

tray.

H. TADDERS

}ND PIATFORIIS

G.

I'IANHOI,XS

1-

Platforms

on

horizontal

vessels

anal

top

platforms

(above head)

on

vertical

vessels

should

be

square

or

rectangular.

P3B-1-013

I

-

custoher

via ?roject

l{alager,

Desiqn

coordinator

aod

Pipiug

Desiqm

supervisor*

*,',l,,,,

;i'

3,,

r

,

DATE

-J.

Revl

l.-r:_-1.,.'1

]oesroir

I

r

r,:_ i, r;.soIIPaE

,



I.

HORIZOTIIAI

VESSEL ORIENTATION

,cenerally,

vessel

anal

nozzle

orientation

should

be as

follows:

1.

rnlet

should

be at

the

opposite

end

of

vessel

f'om

tlle

liquid

and

-

".po.

outlets

to

prevent'

i'short

circuiting"

of

the floi'''

They

shouLd

also

be

maximurn

distance

aPart-

2.

3.

4.

The inlet

is normally

located

on the

end of

the

vessel

a 'ay

from

the

pipeway. This

arraugement

then locates

the

Ievel

instruments

next

.

to-

the- operating

aisie

for

good

accessiSility

Per

s?-5'1'1'

5- The

setting

of the

suPPort

Iegs on

a horizontal_

vessel

is

normally

done

by the

computer

tut

sometires

we

stutly

and

orient

-vessels

beiore'thi.s

information

is

available

to

Piplng'

A

good

"rule

of

thutnb[

to

follow

is:

Leeel

.instr\reetrts

anal

boot should

Ue

a1 tUe

opposiie;

eaa

of

vessel

from

inlet.

There

is

les6 liquid

turbulence

at

the

outlet

end'

They

should

also

be

maximum

distance

apart.

'

To

alLov for

the

horizontal

grouth

due

to

ther&al

eq>ansion,

one

irrpport

of the

vess;l

is anciored

anil

the other

end

i6 allo 'ed

to

qr'oi,

ly

".y

of a

slide

Plate

and

glotted

holes

at

the

opPo6ite

Juppo.ll

e'av.ntage

should

be

taken

of

this

vessel

growth by

making

it'vork

for

you-

-For

exaEple,

by

anchoring

the

vessel

at the

support

,,.ur""t

thu

iipevay

and

tetting

ihe

vessel

gros

al'ray

from-the

Pipe\day'

the grovth

oi'tt"

ves".t

i{i}l

cance}

out the

grosth

of

a

lioe

from

the

tipeway

to

the rmanchored

end

of

the vessel.

?3B-1-013

@

.- The

6ize

'ossovdrs

biti6iit lidildis.-"

rhe

si

alves

anal equlPnent.

anal

for c

"t

t1,"""

pf"if"i1trs.shoultl

be kept

to

a minimre-

.The

viaU.r

(z':s"

io.iioo"1si-a."a)

is usually

onty

e@ughtqir;eroit

oPening

of

t}re

""ot

oi"

"o.r".

or to

provl<le

a-niai.ntrm

of-18"incba;6

clearance

betveen

r,.ndiiir

.na

pipi"g

such

as level

controller,

gage

glasslrevel

,

...3.

-,1

proj;ction

of.rio'lzLes

erteudin{'

thi6ughtirtoi

pletforus

mirst

be

such

exteuding

t

plqtforus

are abovt

the.Diitfoi:m

lever.

. -l :.J1.i'4,".: .j l

.

"

not

be iupDo:'tedl

from

platforns

unless

abso-

slritch

or

saflty.:rilves

-

PlatforniDg

qee.+

not

eatentl

underneath

{itch

or

safety-valves.

PlatforniDg

need

not

extend

valves

and equiphent

to

Dake

then

accessible.

'

ila;it";;;;;";.y.-:,,rf

it

is

fo-und

necessary

to

6uPport

piping

i.o. i

pl"tforrn, t'otify

tfr"

vessel

GrouP.

The vessel

Designer

..qay-have

to

"be;f--trl,:'

ahe

platform

st{rport-'brackets

rto

rtake

the

added 1oad.



';,.

1.

r.

.l'

or

che

-ca11y

changing

6toring

Iiquids

and

&

€

vertical

the

horizontal

uithout internal

fractionation

6ervice

the

frac-

catalyst

(from

a

the

catalYBt

for

1.1-

3

Flat

B.ottom

oDen

toD:

For

storage

of

non-volatile

productg'

Flat

Bottoo

conical

top3

for

stoilge

of

loir

volatility

Pro'tuct-

Flat

Bottom

Floatinq

Roof:

For

storage

of

volatile

liquid6

'

Gas

tlolders:

These

have

flat

bottoms

an'l

roof6

or

dones

shich

rise

anE-EaII

ulth

the

quautitY

of

ga6

6tored'

1.I.4

SOUE

TSPES

OF STORAGE

VESSELS

P 9{9C,

a

spherical.

shaped

ves6el

6rPPorted

-by

a

series

of

fegs

around

the

"qo""ot, "'oi"f"o"tiias

presiurizea

gases? or

liquid

and

gas

-

?38-1-013

t.L.2

l€

gaae6



,:','{;ii".riirjl+i.

:'i

''l/FiJoR

DESIGN

driors

vessel

rxeixrentxc

oEslcN

GUIDE

VESSEL,}IOUEIICLATI'RE

.

{r

.i,t.

r

::

.ijj.,;r

P g :

shape

anal

has

special

BuUet:

A

largr

:;::;;:-;--,ri***..--:a

-

."

resenbleE

a

alroP

of

nercury

resting

on

a flat

surface,

t ,pe

glpports.

ilseat

to contaih

pres6urized liquids

'

rroitzontai

veasgl'

c6ntiini.ng,p.ieaiurlzetl{ases,

or

Uquid

and

gas

.

.

..-. 1,.1.

:r:

1.1.5

VESSEL AND

IANK

PArrS.

.

.

,i

:.

I ,

,.

,,The,:cyrilalrlcal.pgrtion

9f

a.yq96e1

I

c/.-

]L

L

.F

,'

Heroispharical

Head:

Bpher:.

conicaL Head3 .Heaal

foracd

ToricooicaL

.Ileail:

Heatl

forEed

in

the

6bape-of,

a

cone

aEd

having

a

ffiAG-ra6;-?angent

to

tlr.

cotre.

rnal

thelI.

-

n.t

u";a

r;i

i#;i iliit;ii

"i'iii4piiid

ii"ri.a

o"

a

shell-

skj-rt: Cyliniter

BlJlilar

to

6hcu,

ihtch

vessels-

skirt Vent6:

of alangerou6

skirt

Access

openinq:

Circular

hole6

in

the

;i."n;@;t

etc. tn6l&

of.

slirt-

ls

used

for

BrPPdrtlDg

vertical

rL

'/

SDall circuf.r

hole5

ln tbe

skirt

to

preveDt collection

gases

rithfu

thc

6klrt.

Base

Plate:

Flat

plate

relded

to

the botton

skirt

to allos

rorkman

to

of

ve6seL

Eupports

and

b"JCq

on

the

foundation-

anchor' BoIt

chairs:

.

GuBBets

.nat

p1ate6

selded

to ba6e

plate

and

ekirt

t.EilA;-Ei

a".h.r

bolt attaciuent-

lnchor Bolts:

Bolts

i-mbeatttetl

in

concrete

foundation

and

boLted

to

il;;r;E6r

bolt

chairs

-

sadalLes:

steel

supports

for itorizontal

vessels,

P3B-1-013

I

I



'l'Fi-rffi-'

DESIGN

-J

citidEs

$

.,1

iEssElj

ENGTNEERING

DESIGN

GUIDE

VESSEL IOI.IENCI.ATT'RE

"{

i

NUIIBER

2-1,1

PAGE

4

olTE

._5-?6

i,t,

.i

:l:

irsiile

Used

of

to

fractionatioD

prevent

vsPor

Iiquid

traY

of,

the

srDDort

icrli :]r

Gratirig

or

IIfi

iE-carlpisr:through-

ra8chig

rings, €tc.

,a

rtLre

he6b

pad

helal

Ln

placc

bettree tito

light

elisLaator

iliiengages

liquids

contaiue'l

irr

the

vapor'

66e

othcr

t 'Pc

of

sqrport

$hlcb

vapor

or

U6ed

to

6ubp;;t

to('er

packi-ng

such

a6

catalyst,

@i<ts

-

rtre

oiet

skirt Pircproofhq:

BrLch

or

concr'te

aPPIicd

iJi'Ide'

artd

outside

of

;Ef.a

6Ee""rE-a"rage

to 6kirt

in

the

event

of

a f ire

'

'

'

1?tatfort6:

-. '.tfottt

bolteat

to.

'nd

sirpPorted

by

cl'ips

o

the outalde

'

:fffifr;"et]'-c.a.Lirv

bcltid

justLeloi'

a

oanholc.

aid

't

rcricf

;1r;;

i;tiU.t'rai".e

oi

conacctiong

a'ttch

n'r't f,requ'at

scrv''ce

'

Lealtler6 and

caqes:

ItLurg-ttDe

ladders

with

cagc6

bu1lt

of

structural

-

-'ita

t"ltias

tlbeD

cuDbirrg

t}e la'liler

'

These

shap.s

to

Pravent

a

Dan

ar

"..

fott"a

to

anat supported

by

clip-

on

the

out6jde

of

the vessel'

Ir6eal

fo

aecesE

uP

arA

alown

to

tJle

Platforlns'

trays,

bubble

caPs,

etc-

1.1.6

ASI'E

BOII.ER

}ND

PRESSI'RE

VESSEL

CODE

Standard

rules

for

the

construction

of,

boilers

and

pressure

vc66e1s

divtated

into

sections

shich

establL6heE

desigEr forDulas'

loaterial

Eelection,allosablestressvalueE,rnetho'IsofcoDstructio['itrsPec-

iioo ulra

norra."t."ctive

examj.nation

procedures

for

preasure

contaliment

vessel-

column

Davitr

a hoi-stiDg

&vice

attached

by

heans

of

a socket

to the

iffiifitii..,i.I;;-;il;

-

used

eor

haniliaq

relLer

valves'

bubble

P3B-1-013

r

v.ssel.'

A Derforatea

tray

whLch

Provlde8

equal

dlstrilutlon

,ressel

are",

Bl-sere

o thc

tray

extend

above

the

to

fgrD

cavLtatLon

in

the



'{c1:r.,1i..1

I

j

.

supDo;t

Leqs:

LcgE

vertlcal

.vesEel6.

Bade of

plpe.

Itarlhole Hlnoea

or Davlt6:

Itlnqe6

i.nd cover

platc

which

alLoss

cover

rianhole opeEilg.

or

structural

EbaPes,.used

to

slqrPort

bol-tirlg

used

or davit8

attached

.lo-.tlaDhoie

ffar,g.

plate to be

dtl.urld-dsldc

'fron

t-he

rnsuletioD Rinqs.

,

Ri.ngs

nade

of flat

bar

or

angte,

.attached

aroutrd

EF;iiEilc-ifiroferenEe)

of

verticar

vessels

and

siiaccd-aPProaiuatery

l2-;

-[- 7t'

'apart;

uee<t

io

et4port-the

eelqht

of

the veeaef

iD6uletloa'

vacuum Stiff.ner

Rilqs

t{irgs

Dade

of

flat

bar or

plate,

or

structural

"h-;E;;Ii;a=;ffi-the

circunference

of

ttt€

vessel.

rhe6e

rlngs

are

insialled

on

ves6els

operatlng

untler

e8ternal

Pressure

i order

to

prevent collapse

of

thl

vesseL.

vacute

stLffener

rings

are

also

uti.Liz.d

a6

LDEulation

6ulrPort

ringE.

FractioBatinq

Travs:

Circular

flat

plates

bolted

to

the

6heII

ihside

;f-i.."i$ftio-[EluDns -

useal

to obtain

vapor

liquid

contact

lrhich

results

in

fractlonation-

Dortacorler6:

Rectanqular

flat

plate6 bolted

to 5hel1

and

trays,

inside

6?-?ilfif6.,ation

coiunns-

used for

directing

process

liquld

and

to

prevent blPassing

of

vaPor.

P38-t-013

E



'l'puuon

.,tlflIqil,.r

,Tf,AlNlNG,1,

I,IANUAI.s

P}IASE

III

HoRrzmEGSsELs

IIA}IDOUT

NUMEER

LE55ON

piee

OATE

5of5

Rev. 1/80

J.

'rD

=

Vessel

diameter,

"L"

=

vessel lenqth

rrs(

=

Distance from

tan- to centerline of

Normal

shefl thickness

vessel6

s=L/s

3.

Take the

pump

out of the

punp

roe and locate

vessel

out

of

the operating

aisle.

Do Dot

pocket pwlp

6uction

Lines- The vessel

or

be increased

to

elimjrate

a

pocket

condition-

RTACTORS AND AIVANCED

DESIGN

VESSELS

tan-

to

tan.,

support Ieg

it

near

t}le

base

of the

skirt height

may

have to

Thin shel1

thiclxless vessels

s

=

Dl4

Note:

In this case the vessel

head acts as a sti.ffelrer

to the shell

6. Vent is

located at the opposite

end

of

the vessel from

the

steam out

and

a

maximum

tlistance

a$aY-

SKTBT

TCIGITI AND

HEIGIIT OF TIORIZOMAL

VESSELS

Skirt height and

height of horizontal vessels

are sho'rn ou

the flo ,

diagrah-

The

Process Englneer

determines irhat the

skirt

height

rill

be

by the N-P-S-H-

(Net

Positive

suction

Head)

-

This

is

the

liquid head

required

to

keep

t}1e

punp

suction

pri,iled-

Ptutp

suction

lines fron the

vessel bottoms

shall

have a

8.0.?-

minimun of 8'-0" above

H-P-F-S-

If

this

requirement

is not met, there

are three aLternatives:

l.

The

vessel

or skirt height

can be increased

to

meet the 8'-0u

head

rooro requirement-

2- Block the

operating ai6le

vith

a

lot

suction

line.

K.

tleaq,

\ra1l,

vessels sith heni-spherical

heads

are a speciaf

design

challenge.

Careful

consideration

should

be given

to

1adder6,

platforns,

pipe

supPorts,

etc. No

velding

to the shell- welding

to the

heads

and

skirt

only.

P3B-1-013



'1.

ruuon

PIPING

TRAINING

I.IANUALS

PIIASE ]II

NIJMB

E

R

Lrssot

7

PAGE

1

DATE

Rev.

HORIZOMAL

VBSSEI,S

HANDOOT

t/

B.

A.

1.

2-

3-

4.

1.

2-

3.

1-

2-

3.

4-

VESSEL ORIENTATION

OBJECTIVE

The objective

of this

session is

to

help

you

become

rnore

famlliar

sith

the Fluor

approach to

vessel

orientation, based

or Fluor Standard

Drawings.

The haterial

anal

instruction

you

receive

from thj.s session shoulal enable

you

to:

1.

K oq

hos

to

assimilate

the

information

to start

a vessel

orientation

study.

2-

lroperly

prepare

orientati.on studies of both vertical

and horizontaL

vessels.

TRAY TYPES

BIEBLE.CAP TRAY

ADVANIAGES DI SADVANIAGES

1-

2.

Very

efflcient

Need

not be

in6talled

level

corrosi.on

not a factor

uost efficient of all

tlpes

Ine>q)ensive

and

lightr,,eight

Need

not be installed level

Corrosion nol a factor

Inexpensive

Lightweight

Good

for

healy

liquids

Expensive

Heavl' and

bulky

cast iro[ caps

occasionally

break

ltounting bolts rust

VA],VE TRAY

SIEVE

TRAY

1-

None

1.

2.

tlust

be install-ed leve1

corrosion

a

factor

P3B-1-013



'l'FLUoR

PIPING

IRAINING

IIANUALS

PHASE

III

NUMBE

R

LESSON

7

PAGE

3

DATE

Rev.

HORIZONTAI

VESSELS

HANDOT}T

7/

1.

2-

3.

6-

F.

INFORI.IATION REQUIRED TO START

IESSEL ORIENTATION

INFORI'IATION

*Prirary

source

Designer

SOURCE

to

the

-

Piping

Design super-visor

or Roller

Board

-

P

j.ping

Design supervisor

anal Fluor

Standards. Job

Book*

-

Project

llanager,

Desiqn

coordunator

or Piping

Design

supervisor*

- Piplnq

Design Supewisor

- vessel

Design

supervisor

or

Piping

Design

supervisor*

- Floi,sheet*,

Process

Engineer or

vessel

Dra',ring

(vertical)

-

vessel

Dralring*

or

Process Engineer

-

Vessel

Drat

ing, Flow

Diagram*

or Process

Engineer

-

vessel

Dra\.ring,

?rocess

or

Instrument

Engineer,

Instrument

standard

Drarings*

-

custoher

via Project l'lanager,

Design

coordinator

and

Piping

Design

supervisor*

FLov Dlagrafis

Job Specifications,

Drafting

Instruction6 and

standards

?relirinary

Job

Informatiotr

Room

vessels

and top

platforms

(above

head)

on

be

square

or

rectangular.

Flovsheet

Transpositioo

vessel

Drasing

or

vessel

Quote

Dralring

skirt

Height

or Druin Height

Process

Nozzle

Elevatiotls

Nomal

Liquid Levef

and

other

Iiquid Levels

9. Instrlment

Nozzle

El,evations

Requlrements

0.

Customer

G.

}IANHOLES

I{anholes

are

generafly

18rr nominal

size

except

for columns

\rith

removable

trays,

in

whiih a savings

may

be realized

by increasing

the size

of the

manhole to

permit

larqe

tray

sections

to

be

removed-

In those

cases

generally

only

one larger

manhole

is

provided,

preferably

beloH

the

bottom

tray.

I,ADDERS

AND

PLATFOR},IS

1-

Platforms

on horizontal

vertical

vessels

should

H.

P3B-1-013



lluMBER

2-1-1

PAGE

1 of 5

DATE

g-76

VESSEL ENGINEERING

D€SIGN

GUIDE

'l'ru.Pn

DESIGN

GUIDES

1.1.I

GENERAI,

VESSEL

NO}IENCI,ATT'BE

Process

Vessel:

A contailrer

for

han'lling

or

cheDLcally

changing

lIfrIE-li?@ses

uithin

a

process Ey6ten'

Storaqe

Vessel

enq

q 9leSglgE'

A container

for

storjng

liquid6

and

A"*-F;ffi

to

;-?;i1o"ijrgiEe

process svsteo'

vertical

vessel:

A ves6el

vhose

longitudi_nal

axiE

is

in

the

vertical

poBitlon-

tlorizontal

Vessel:

A

ve6ae1

uho6e

longitudiral

axis

ls

la

the

horizontal

'

position.

1.1.2

SOt{8

rr?Es

of

PRocEss

vEssELs

FractionationcolulEl.Generalliaverticalve66elcontaillngtraYsor

''t

txt ."ct_"

frorn

the

process 6ystelr

a

certain

packing t hen

in 6ervi(

requireal

fraction

Euch

aa butane

or

Propane

'

RefluxAccunulator:GenerallyahorizoEtalve66el'andt'ithoutiDterDaL

"".tf,tri=--"*;i."-ioir""i"

anal

tranebltB

back

to

a fractionation

:;i;; th"

fraction

which

is

Proce6sed

by

that

colunm

'

Reactor:

a vertLcal

vessel

contaitd'tg

catalyst'

tdhich

ih

service

i-iii6g""

the

nolecular

structure,

'nd

thcrefore

chaDge6

ttre

trac-

tions

in a

Proces6

sYste$'

Redenerato :

A

vertical

vessel

coDtalning

used

catalyst

(from

a

iiid)fri"r,

itt-"".oi""

t"gt"ttttc6

(restoreg) the

catalyst

for

re_use

in

the

reactor-

1.1.3

SOI{E

TYPES

OF SMRAGE

TANITS

Flat

Botton

oDen

Top:

For

storage

of

non_volatil'e

productE'

Flat

Botto$

cooic.l

Top:

For

ltorag€

of

lotr'

volatility

product-

Roof:

For

storage

of

volatile

liqui&'

Cas

Holders:

These

have

flat

bottoms

and

roof6

or

dones

whlch

rise

;A-?;TIti-t}r

the

guantity

of

gas

6torcd'

SOI.IE

TYPES

OF

STORAGE

IESSELS

sbheres: tr

sDherical

shaped

ves6e1

supPorted

by a

series-of

legs

#ffi=;.-.;;;;i,

*r'ilt'"o"t'in"

preiiurized

qases' or liquid

and

gas.

r-1,4

P3B-1-013

E"



'l'ruron

DESICN

cut0cs

VESSEL ENGINEERI

G DESIGII

GUIDE

VESSEL

NO}'ENCLATI'88

NU|{BER

2-1-1

PAGE

4

DAIE

5-76

Seal

?ans:

column

6hell

bypassing

up

Distrilutor

Tray:

a

perforated tray

which

provideE

equal

alistri.butLon

;i-iIqnIa

ov.r

the vea6el

area-

RLeers

on

th.

tray

ettenal

abov€

the

Itqqtd Lev.l

to

perEit

lr 63age

of vaporE rislng

uprrard-

chi-onev

Trav:

A tray coqroscil

of

chimncy6

e8teldlng

above

th. Uquid

ledI;f

the tray

pemlttirg

pa66age of the vaPor6 upra.d-

the tray

collectd

aual

r.movea

afl

liquLl

product

from

a

al,ccLfic

Portion

of

the

vessel-

FIat

pLates

bolted

or

lrelded to Lnside

of

fractionation

belou

dor,Dcomer of

loeest

tray-

Used to

Prcvent

vapor

through

the

alo$ncoDer.

vortea

Breaker:

I alevice

locateal

E6

IEIlon

ceuerally

coasL6ting

the

6hape of

a cro66.

fhe vorte8

Iiquid

pa6sing

th 'ouqh

the outlet

ilsLde

a ves3el

at

tbe

outlet

of

plate.

sctdctl together

to

fotn

brelker

preventa

cavLtatLon

jn

the

coEnactlon.

ui6t

Elinlnator:

I xire

mesh

pad

hcld

ln

place

betue.n

two

liqht

srla;:--fr;-E.t

elLoLnator

disengagea

liqulats

contalned

in

the vaPor-

support

Grld:

Grati.ng

or

sooe

other tlPe

of

Blqrport

-uhlch

vaPor or

ITfrIE-5laas

throuEh. u6ed

to

6upport

to er

PactLng

such

as catalyst

ra6chig

rings,

etc.

Shirt

Fir.prooflrrg:

BrLck or concrete

applLed

hEide aDd

outsL'le

of

;II.t

t.Eeve-"Ld"ra9€

to .kirt

Ln the

evEitt of

a

fLr.i.

P1atfo 'Es: Platforo6

boltcat

to

aad

4Pporteit by

ctiPs

ou the outsi-de

6?ltle ve-r""l.

cenerally

located

Just

belo,

a oaDhole,

aat

at

rell.f

vrlves

or othea valv.6

or

connections

l,lrlch

nacal

frequeDt

6ervLcc.

Ladiler5 apd

Caqes:

Rung_tlDe

lqdders

lrith cage6

bulLt of

Etructural

;Eapcs

to

p;evcnt

a D.n

f,rom

fallilg

whe

cli-ubirtg

the Ladder.

These

are bolteal

to and supported

by cliPs

on

the outside

of

the vess61_

uaed

for

acce6E

r{,

and

down

to

the Platforns.

Colunn Dry :

A

hoisting

device

attached by

means of

a socket

to

the

JiiZfionatioo

col;mns

-

used

for

handling

reli.ef

valves.

bubble

bubble cap6,

etc.

1.1.6

AS}IE

BOILER

AND PRTSSURE

VESSEL

CODE

top of

tral,s,

standard

rules for

the construction

of

boilers

and

Pressure

vessels

divlded into

section6

$hich e6tabllshes

design forDulas,

material

selection,

alLowable

stress

values, methods

of

construction,

insPec_

tj,on

anal

nonilestructive

exanination

procedures

for

Pressure

contaii'nent

vessef.

P3B-1-013

I

I

I



'l'rluoa

PIPING

TRAINING

TTANUALS

PHASE

III

NUMBER

LEssoN

7

PAGE

5 Of

oATE

Rev-

HORIZONTAL

VBSSELS

-----ffiotn

5

L/

rrD

=

vessel

diameter,

'rl-r

=

vessel

length

,,S,,

=

Distance

from

ta -

to centerline

of

Normal shelf

thickness

vessels

s=L/5

Thin shell

thicknes6

vessels

s

=

Dl4

Note:

In this

case

head acts

as

to the

shell

tan. to tan.

support

Ieg

the

vessel

a stiffener

5.

vent

is

located

at the

and

a

lnaximlnn

alistance

opposite

end

of the

vessel

from the

steam

out

a$ay.

HORIZONTAL

VESSELS

.

(.

skilt

height

and

height

of horizontal

vessels

are

shown

on the

flos

diaoram.

The

Procesl

Enqineer

determine6

what

the

skirt height

t'til}

be

Uy itre

N-p.s.tt.

(Net

Positive

suction

Head).

This

is

the liquid

head

requi.red

to

keep

the

Pump

suction

primed-

PumP

suction

lineE

fron

the

vessel bottoms

sfratl

i'r"vl a

B-o-P. ninimui

of 8'-0" above

H.P'F'S'

If

this

requi.rement

is

not met, there

are

three

alteroatives:

1.

The

vessel

or

skirt

height

can be

increased

to meet

the

8'-0'

head

room

requirement.

SKIRT

}IEIC}l1 AND

IIEIGHT

OF

2. Block

the

operating

aisle

with a

1o r

suction

3. Take

the

pump

vessel

out of

1ine.

it near the

base

of the

Do not

pocket

ptstP

suction

lines

be increaseal

to eliminate

a

pocket

REACIORS AND

ADVANCED

DESIGN

VESSE1S

Hea\rr-

\raI1 vessels

with

hemispherical

heads

are

a speclal

design

chal]enqe_

careiul

consideration

should be

given

to

ladder6,

platforms,

Pipe

supports,

etc.

No

\,,elding

to the

shell.

|elding

to

the

heads

and

skirt

only'

out

the

of the

pump

rot,

and locate

operating

aisle.

The

ves6e1

or

skirt

height

may

have

to

condition.

P3B-1-013

I



'l'rluon

PIPING

TRAIXING

flANUALS

PHASE

IIl

HORIZONTAI

VESSEiS

HANDOI'T

NUI.,IBER

Lgssox

7

PAGE

1 Of

1

DATE

Rev.

1/

STEPS

TO

ACCOI{PLISH

HORIZON]AL

VESSEL

STIJDY

2-

1-

4-

6.

7-

a.

b-

c.

Update

your

floi,

diagram

from

rllaster,l

Compare

vessel

outlille

to

flow

diagram

-

a-

Vessel

I.D,

b-

Tangent

to

tangent

dilnension

c.

N.L.L-

d.

Size,

rating

and quantity

of

nozzles

Calculate

elevations

centeru.ne

of

vessel

based

on

mini-oum

height

on

f1o ,

aliaqram

Process

nozzles

based

on

vessel

outtine

-

verify

or

6et

instrument

nozzles

based

on

standard

dra\ring

flolr

diagram

and

instrunent

Determine

vhat

items

require platform

or

Iaalder

access

study piping

transposition

Drav

vessel

outline

to

scale

and

get

xerox

copies

On these

copies

do

rgug\

skeqches

of

piping

and

nozzle

arranqements,

comDrne

anal

change

sketches

for

optijnun

design

using

piping

iogic.

Pipj.ng

logic

considerations

or

priorities

.

F1olr

diagran

Stress

Economics

Support

and stability

Lines

run

at

standard

Looks

Operation,

Daintenance

Job

standards

efevations per

unit

plot

drawing

and

safety

Your

order

of

inportance

will

change

in

each

situation.

For

instance

econonics

-

vrould

be

more

important

than lgoks

on

a large

a1loy

line-

'

on

a smaLl

carbon

steel

1ine,

looks

nay be

more

irnporiant

than

economics-

Conunence

actual

study.

you

must

be

donrt

worry

about

draftihg qualiry,

dirtyr' but

legible

and complete.

accurate

and

drav to

scafe;

houever,

li.Ilework,

or lettering.

,,Rough

and

9.

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Flour PUMP&VESSEL -.pdf

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