Shell and Tube Heat Exchanger

Table of contents

NO. PARTS1. Abstract/Summary2. Introduction3. Aims/Objectives4. Theory5. Apparatus6. Experimental procedures7. Results8. Sample Calculations9. Sample Error Calculations

10. Discussion11. Conclusion12. Recommendations13. References14. Appendices

Abstract/Summary

The objectives of this experiment are to evaluate and study the heat load and head

balance, LMTD and overall heat transfer coefficient, to calculate the Reynolds numbers at the

shell and tubes sides and to measure and determine the shell and tube sides pressure drop.

This experiment consists of five runs. For each of the run, three sets of data are obtained. A set

of data from each of the run is selected based on the best convergence of QC and QH (the ratio

of QC/QH is nearest to 1.0). From the selected set, the heat load and head balance, LMTD and

overall heat transfer coefficient, Reynolds numbers and pressure drop are determined. From

the results obtained, an ideal set to choose based on the ratio is majorly from set 3.

Introduction

A heat exchanger can be defined as any device that transfers heat from one fluid to another or

from or to a fluid and the environment. There are several types of shell and tube heat

exchanger:

Figure 1: Heat exchanger with fixed tube plates (four tubes, one shell-pass)

Figure 2: Heat exchanger with floating head (two tube-pass, one shell pass)

Figure 3: Heat exchanger with hairpin tubes

Basic Considerations in Choosing a Mechanical Arrangement of Heat Exchanger

There are four basic considerations in choosing a mechanical arrangement that provides for

efficient heat transfer between the two fluids or vapors, while taking care of such practical

matters as preventing leakage from one into the other. They are:

Consideration for differential thermal expansion of tube and shell

Means of directing fluid through the tubes

Methods of controlling fluid flow through the shell

Consideration for ease of maintenance and servicing

Advantages of Heat Exchanger

The main advantages of shell-and-tube heat exchangers are:

Condensation or boiling heat transfer can be accommodated in either the tubes or the

shell, and the orientation can be horizontal or vertical.

The pressures and pressure drops can be varied over a wide range.

Thermal stresses can be accommodated inexpensively.

There is substantial flexibility regarding materials of construction to accommodate

corrosion and other concerns. The shell and the tubes can be made of different

materials.

Extended heat transfer surfaces (fins) can be used to enhance heat transfer.

Cleaning and repair are relatively straightforward, because the equipment can be

dismantled for this purpose.

Applications of Heat Exchanger

Shell and tube heat exchangers represent the most widely used vehicle for the transfer of heat

in industrial process applications. They are frequently selected for such duties as:

Process liquid or gas cooling

Process or refrigerant vapor or steam condensing

Process liquid, steam or refrigerant evaporation

Process heat removal and preheating of feed water

Thermal energy conservation efforts, heat recovery

Compressor, turbine and engine cooling, oil and jacket water

Hydraulic and lube oil cooling

Many other industrial applications

Shell and tube heat exchangers have the ability to transfer large amounts of heat in relatively

low cost, serviceable designs. They can provide large amounts of effective tube surface while

minimizing the requirements of floor space, liquid volume and weight.

Aims/Objectives

To evaluate and study the heat load and head balance, LMTD and overall heat transfer

coefficient.

To calculate the Reynolds numbers at the shell and tubes sides.

To measure and determine the shell and tube sides pressure drop.

Theory

Heat load and heat balance

This part of the calculation is to use the data in Table 1 to check the heat load QH and QC and

to select the set of values where QC is closest toQH .

Hot water flow rate (HW )

QH = FH×CpH×(t1−t2 )

Hot water flow rate (CW )

QC = FC×CpC×(T 2−T1 )

Where:

QH = Heat load for hot water flow rate

QC = Heat load for cold water flow rate

FH= Hot water mass flow rate

FC=Cold water mass flow rate

t1= Hot water inlet temperature

t2= Hot water outlet temperature

T 1=Cold water inlet temperature

T 2= Cold water outlet temperature

LMTD

Calculations of log mean temperature difference (LMTD).

LMTD=( t1−T 2 )−( t2−T1 )

ln( t1−T 2)( t2−T 1)

Where, all variables are same with the above section:

R=−( t1−T 2)−( t2−t1 )

S=−( t2−t1 )−(T1−t1)

Both equations would determine the value of correction factorFT . Practically, FT value

obtained from the graph with respect to R and S value. In this case, the correction factor

would apply to enhance the LMTD value. So, equation below show the corrected LMTD can be

determined.

LMTD=FT×LMTD

Overall heat transfer coefficient, U

Overall heat transfer coefficient at which equivalent to U D can be calculated by using equation

below. In this case, the value of total heat transfer area A has been given and equal to 31.0 ft2

U= QA×LMTD×FT

Where:

Q= Heat rate with respect to the average head load

FT=Correction factor

Reynolds Number Calculation

Shell-side Re( s )for CW

Re( s )=De .Gsμ

Where:

De=de12

de=4 (1/2PT×0 .86 PT−1 /2 π .

do4

2

)

1/2π .do

At which:

PT=Pitch = 0.81inch

do=Tube outside diameter, inch

μ= Viscosity, taken at average fluid temperature in the shell, lbmft-1hr-1

Gs=WsAs (lbmft-2hr-1)

Ws= Flow rate in (lbmhr-1)

As= 0.029 ft2

Tube-side Re( t ) for HW

Re( t )=D .Gtμ

Where:

D= Tube ID = 0.04125 ft

μ= Viscosity, taken at average fluid temperature in the tube, lbmft-1hr-1

Gt=WtAt (lbmft-2hr-1)

Wt= Flow rate in lbmhr-1

At= 0.02139 ft2

Pressure drop

This part would determine the following:

HW : The measured tube-inside pressure drop DP (tube) which will be corrected and is

expected to be more than calculated tube-side pressure drop.

CW : The measured shell-inside pressure drop DP (shell) which will be corrected and is

expected to be more than calculated tube-side pressure drop.

Notice that, both calculated pressure and also measured pressure are considered in unit

mmH2O. In this case, since calculated pressure drop in both of shell and tube side have been

obtained during the experiment, so it’s only required conversion factor to change the value into

unit of mmH2O.

Conversion factor: x .bar×1×105Pa

1bar×

1mmH 2O

(9 . 81)Pa .

Where x is the calculated pressure value in unit bar.

Apparatus

HE 12: SHELL AND TUBE HEAT EXCHANGER PLANT

Experimental procedure

Step i)

1. All the pump suction valves (for PH, PC1, and PC2) are checked so that they are fully

opened all the time.

2. BVC2 is opened fully but CV2 is closed fully so that PC2 shall operate as a back-mixing

pump for tank T2 in the next experiment. Both CV1 and BVC1 are opened fully. Only PC1

shall be used here to pump CW into the Heat Exchanger in the next experiment. Do not

switch on any CW pumps (PC1, PC2) yet.

3. HV is closed fully but BVH is opened fully.

4. Pump PH for HW is started to circulate around tank T1 via only BVH.

5. The heaters are started and TlC5 is noted. When the HW in tank T1 is almost 70 C/158 ͦF (see TlC5), HV is opened fully. The HW flowrate is quickly adjusted ͦto about 25 USGPM by regulating its by-pass valve BVH.6. Both the CW pumps, PC1 and PC2 are switched on. The CW flowrate is quickly adjusted to about 10 USGPM by regulating the by-pass valve BVC1.7. The DP Selector Switch is switched to the DP (Shell) position.

Step ii)

a) The first set of temperature and flowrate readings are taken.

CW: Temperature - inlet/outlet, T13*(T1), T14*(T2):

Flowrate FC at FI(C*)

HW: Temperature - inlet/outlet, TI1*(T1), T12*(T2):

Flowrate FH at FI(H*)

Note that the CW inlet temperature (T1) is increasing gradually. The CW outlet temperature

(T2) varies together with the HW inlet/outlet temperatures t1/t2. It is important that all the

temperature and flowrate readings be taken almost simultaneously.

These readings are recorded appropriately in Table 1.

Also the respective inlet pressure and inlet pressure drop of the CW and HW flow

streams are recorded. For the pressure drop readings, DP (shell), DP (tube) at the panel

amount DPI*, use the DP signal Selector Switch appropriately as explained below:

CW: PG-C; DPI* for DP (shell) with the DP Selector Switch at the DP (shell) position.

HW: PG-H; DPI* for DP (tube) with the DP Selector Switch at the DP (tube) position.

To take the DP readings at DPI*, they are waited till they are fairly steady.

The DP reading is then taken at its highest reading (i.e. peak reading) just when it starts to

decrease.

b) The second and third sets of the above readings for RUN 1 are continued and taken

consecutively. The last set of temperature readings should be taken when all the

temperatures are fairly steady.

Step iii)

1. RUN 1 is completed, with three sets of the above readings.

2. All the CW pumps PC1 and PC2 are stopped.

3. The heaters are kept on for the next RUN.

4. With the HW pump PH still running, the discharge valve HV is closed fully but the by-

pass valve BVH is opened fully.

5. The DP Selector Switch is switched to the equalizing (vertical or “0”) position.

Step iv)

1. RUN 2, 3, 4 and 5 are repeated at different recommended nominal flowrate of CW (i.e.

FC) and HW (i.e. FH) using the following procedures check-list.

To continue with the next run

The HW pump PH is checked so that it is running with BVH fully opened and HV

fully closed.

With the heaters ON, the HW in tank T1is heated till it almost 70 C/150 F (seeͦ ͦ TlC5). HV is fully opened. The HW flowrate is adjusted until FH at Fl (H*) is almost at the recommended nominal flowrate for the RUN. This is done by regulating the by-pass valve BVH with HV fully opened. (However, if the flowrate is still too high even when its by-pass valve is fully open, its discharge valve, HV is gradually closed to get the required HW flowrate). The CW pumps PC1 and PC2 are started with CV1/BVC1/BVC2 are fully opened but CV2 is fully closed. FC at Fl(C*) is noted. FC is adjusted to the recommended nominal flowrate for the RUN by regulating the by-pass valve BVC1 with CV1 fully opened. (However if the CW flowrate (FC) from PC1 is still inadequate even when its by-pass valve BVC1 is fully closed, use the second CW pump (PC2) by gradually opening CV2 and simultaneously closing BVC2 to get the required CW flowrate). The DP Selector Switch is switched to the DP (shell) position.

The various readings for the RUN are taken.

To end a RUN after getting 3 sets of readings

All the CW pumps, PC1 and PC2 are stopped.

The DP Selector Switch is switched to the equalizing (vertical or “0”) position.

With the HW pump PH and the heaters stillON, HV is closed fully nut BVH is

opened fully.

PLANT SHUT-DOWN

1. The heaters are switched OFF.

2. All the pumps (PH, PC1 and PC2) are checked so that they are switched OFF.

3. The DP Selector Switch is switched to the equalizing (vertical or “0”) position.

4. The main power supply to the plant at the front of the panel/cubical is switched OFF. All

the pumps suction valves, discharge valves (HV, CV1 and CV2) and by-pass valves (BVH,

BVC1 and BVC2) are opened.

Results

RAW DATARUN 1

SET 1 SET 2 SET 3CW HW CW HW CW HW

Nominal Flow, USGPM FC: 10

FH: 25

FC: 10

FH: 25

FC: 10

FH: 25

Actual Flow, USGPM FC: 10.0

FH: 25.1

FC: 11.1

FH: 25.1

FC: 11.2

FH: 25.2

Temperature, ͦC/F, inlet Tl3:T1: 40.1

Tl1:t1: 72.4

Tl3:T1: 41.0

Tl1:t1: 70.1

Tl3:T1: 42.9

Tl1:t1: 65.1

Temperature, ͦC/F, outlet

TL4:T2: 66.8

Tl2:t2: 65.1

TL4:T2: 64.4

Tl2:t2: 63.0

TL4:T2: 62.8

Tl2:t2: 60.9

Pressure, psig, inlet PG-C: 8.5

PG-H: 12.6

PG-C: 8.5

PG-H: 12.6

PG-C: 8.5

PG-H: 12.6

Pressure Drop, mmH2O DP: 872

DP: 4333

DP: 873

DP: 4347

DP: 875

DP: 4347

shell tube shell tube shell tube

RUN 2



FH: 20

FC: 10

FH: 20

FC: 10

FH: 20


FH: 19.9

FC: 10.3

FH: 19.8

FC: 11.2

FH: 19.8

Temperature, ͦC/F, inlet Tl3:T1: Tl1:t1: Tl3:T1: Tl1:t1: Tl3:T1: Tl1:t1:

38.1 69.5 38.5 61.7 41.4 57.5Temperature, ͦC/F, outlet

TL4:T2: 64.8

Tl2:t2: 61.1

TL4:T2: 53.7

Tl2:t2: 54.5

TL4:T2: 51.1

Tl2:t2: 52.0


PG-H: 8.0

PG-C: 10.0

PG-H: 8.0

PG-C: 8.5

PG-H: 8.0


DP: 2723

DP: 767

DP: 2726

DP: 880

DP: 2740

shell tube shell tube shell tubeRUN 3



FH: 15

FC: 10

FH: 15

FC: 10

FH: 15


FH: 15

FC: 9.4

FH: 15

FC: 10

FH: 15


Tl1:t1: 65.0

Tl3:T1: 37.9

Tl1:t1: 57.9

Tl3:T1: 39.1

Tl1:t1: 55.5


TL4:T2: 56.5

Tl2:t2: 55.6

TL4:T2: 50.1

Tl2:t2: 50.7

TL4:T2: 48.6

Tl2:t2: 49.4


PG-H: 4.9

PG-C: 10.0

PG-H: 4.9

PG-C: 11.0

PG-H: 4.9


DP: 1586

DP: 660

DP: 1585

DP: 720

DP: 1587


RUN 4



FH: 10

FC: 10

FH: 10

FC: 10

FH: 10


FH: 10.3

FC: 10.1

FH: 10.4

FC: 8.6

FH: 10.4


Tl1:t1: 63.8

Tl3:T1: 38.5

Tl1:t1: 60.2

Tl3:T1: 38.1

Tl1:t1: 57.9


TL4:T2: 52.1

Tl2:t2: 52.4

TL4:T2: 49.4

Tl2:t2: 50.0

TL4:T2: 48.8

Tl2:t2: 49.3


PG-H: 2.2

PG-C: 7.7

PG-H: 2.2

PG-C: 10.0

PG-H: 2.3


DP: 740

DP: 717

DP: 747

DP: 584

DP: 736


RUN 5



FH: 10

FC: 6

FH: 10

FC: 6

FH: 10


FH: 10.2

FC: 5.0

FH: 10.2

FC: 5.1

FH: 10.2


Tl1:t1: 69.7

Tl3:T1: 37.8

Tl1:t1: 65.6

Tl3:T1: 38.0

Tl1:t1: 64.3


TL4:T2: 60.1

Tl2:t2: 58.3

TL4:T2: 57.0

Tl2:t2: 56.4

TL4:T2: 56.5

Tl2:t2: 55.5


PG-H: 2.0

PG-C: 7.7

PG-H: 2.0

PG-C: 7.72

PG-H: 2.1


DP: 712

DP: 279

DP: 703

DP: 287

DP: 706


CALCULATED DATA

RUN 1


Temperature Change, ͦC T2-T1: 26.70

t1-t2: 7.30

T2-T1: 23.40

t1-t2: 7.10

T2-T1: 19.90

t1-t2: 4.20

Average Temperature, ͦC (T2+T1)/2: 53.45

(t1+t2)/2: 68.75

(T2+T1)/2: 52.70

(t1+t2)/2: 66.55

(T2+T1)/2: 52.85

(t1+t2)/2: 63.00

Q, Head Load, BTU/HR QC: 240804.63

QH: 165253.30

QC:243267.00

QH: 160725.82

QC:201013.24

QH:95456.04

Ratio QC/QH 1.46 1.51 2.11Selection Selected Not selected Not selected0.5 (QC + QH) 203028.97 - -LMTD, ͦC 12.967

Actual LMTD : 9.73- -

U, BTU/HR ft2°F 130.17 - -Reynolds’s Number, Re Shell: 215.63

Tube: 23870.68- -

RUN2



t1-t2: 8.40

T2-T1: 15.20

t1-t2: 7.20

T2-T1: 9.70

t1-t2: 5.50


(t1+t2)/2: 65.30

(T2+T1)/2: 46.10

(t1+t2)/2: 58.10

(T2+T1)/2: 46.25

(t1+t2)/2: 54.75

Q, Head Load, BTU/HR QC:262477.29

QH:150760.01

QC:141200.04

QH:128573.44

QC:97981.33

QH:98215.82

Ratio QC/QH 1.74 1.09 1.00Selection Not selected Not selected Selected0.5 (QC + QH) - - 98098.58LMTD, ͦC - - 8.32

Actual LMTD: 6.99U, BTU/HR ft2°F - - 69.85Reynolds’s Number, Re - - Shell: 216.27

Tube: 16173.23RUN 3



t1-t2: 9.40

T2-T1: 12.20

t1-t2: 7.20

T2-T1: 9.50

t1-t2: 6.10


(t1+t2)/2: 60.30

(T2+T1)/2: 44.00

(t1+t2)/2: 54.30

(T2+T1)/2: 43.85

(t1+t2)/2: 52.45


QH:127166.49

QC:103428.75

QH:97404.12

QC:85679.55

QH:82522.94

Ratio QC/QH 1.29 1.06 1.04Selection Not selected Not selected Selected0.5 (QC + QH) - - 84101.25LMTD, ͦC - - 8.49


Tube: 11347.44

RUN 4



t1-t2: 11.40

T2-T1: 10.90

t1-t2: 10.20

T2-T1: 10.70

t1-t2: 8.60


(t1+t2)/2: 58.10

(T2+T1)/2: 43.95

(t1+t2)/2: 55.10

(T2+T1)/2: 43.45

(t1+t2)/2: 53.60


QH:105900.26

QC:99289.17

QH:95672.49

QC:82991.92

QH:80665.04

Ratio QC/QH 1.08 1.04 1.03Selection Not selected Not selected Selected

0.5 (QC + QH) - - 81828.48LMTD, ͦC - - 10.11


Tube: 7867.56

RUN 5



t1-t2: 11.40

T2-T1: 19.20

t1-t2: 9.20

T2-T1: 18.50

t1-t2: 8.80


(t1+t2)/2: 64.00

(T2+T1)/2: 47.40

(t1+t2)/2: 61.00

(T2+T1)/2: 47.25

(t1+t2)/2: 59.90


QH:104871.77

QC:86581.44

QH:84633.36

QC:85093.49

QH:80953.65

Ratio QC/QH 1.14 1.02 1.05Selection Not selected Selected Not selected0.5 (QC + QH) - 85607.4 -LMTD, ͦC - 12.96

Actual LMTD: 9.85-

U, BTU/HR ft2°F - 275.91 -Reynolds’s Number, Re - Shell: 96.55

Tube: 8993.78-

Sample Calculations

RUN 1

i) Heat Load

FC= 10 USPGM

FC= 10 USGPM x m 3 /Hr x 1000 Kg x 2.20462 Ibm 4.4 USGPM m3 Kg

FC= 5010.5 Ibm/hr

CP= 1 Btu/Ibm oF

QC = FC X CP X (T2-T1)

= 5010.5 Ibm/hr x 1 Btu/Ibm oF x (152.24 – 104.18) oF

= 240804.63 Btu/hr

FH = 25.1 USPGM

FH = 25.1 USGPM x m 3 /Hr x 1000 Kg x 2.20462 Ibm 4.4 USGPM m3 Kg

FH = 12576.355 Ibm/hr

CP= 1 Btu/Ibm oF

QH = FH X CP X (t1 - t2)

= 12576.355 Ibm/hr x 1 Btu/Ibm oF x (162.32-149.18) oF

= 165253.30 Btu/hr

ii) LMTD

LMTD=( t1−T 2 )−( t2−T1 )

ln( t1−T 2)( t2−T 1)

= (72.4-66.8)-(65.1-40.1)ln (72.4-66.8)

(65.1-40.1)

= 5.6 – 25.0 ln 5.6 25

= 12.967 ͦC

R = - (40.1-66.8) - (65.1-72.4)

= 3.65

S = - (65.1-72.4) - (40.1-72.4)

= 0.23

.:. From graph, FT= 0.75

Actual LMTD = 12.967 ͦC X 0.75 = 9.73 ͦC = 49.514 ͦF

iii) Overall Heat Transfer Coefficient

U= QA×LMTD×FT

= 203028.97 BTU/HR 31.50 ft2 X 49.514 ͦF = 130.17 BTU/HR ft2°F

iv) Reynolds’s Number

Shell-side Re( s )for CW

Re( s )=De .Gsμ

Where:

De=de12

de=4 (1/2PT×0 .86 PT−1 /2 π .

do4

2

)

1/2π .do

de = 4(1/2 (0.0675) X 0.86(0.0675)- ½ π(0.0619 2 /4)) ½ π (0.0619)

= 0.0187

De = 0.018712

= 1.56 X 10-3

Re(s) = 1.56 X 10 -3 ( 5010.5 /0.029) (516.7 X 10-6) X 2419.1 = 215.63

Tube-side Re( t ) for HW

Re( t )=D .Gtμ

= 0.04125( 12576.355/0.02139) (420 X 10-6) X 2419.1

= 23870.68

v) Pressure Drop

The pressure drops are already obtained during the experiment. The shell and tube-side

pressure drop (DP) are measured using the differential pressure transmitter (DPT) and then

indicated digitally at the panel DP (DPI*). A selector switch with a set of 5 solenoid valves allows

both the shell and tube-sides pressure drop i.e. DP (shell), DP (tube), to be measured one at a

time.

Discussion

In this experiment, the objectives are to evaluate and study the heat load and head

balance, LMTD and overall heat transfer coefficient, to calculate the Reynolds numbers at the

shell and tubes sides and to measure and determine the shell and tube sides pressure drop. At

the end of the experiments, all objectives are met although maybe there are some errors.

It is found that the calculated values of QH and QC are not really satisfied the theory

since supposedly, the ratio of QC/QH is unity means the ideal condition is the value of QC

should be closed to the value of QH. But in the calculated results, it is found that there are

some deviations in the value but it is normal because it is impossible to have an ideal system in

real life. The most irrelevant data for QC/QH is in run 1, set 3 where the ratio is 2.11. The

margin is big when compare to the ideal condition where QC/QH = 1.0. The irrelevant value of

this ratio is maybe caused by the unstable conditions of shell and tube heat exchanger where

this phenomenon occurs at the beginning of the experiment.

For LMTD, the calculations consist of the use of graph which called as correction factor

graph. This graph is used to obtain a more accurate LMTD as the calculated LMTD values may

deviated from the actual one. The correction factor, FT is obtained from the graph by finding

the values of R and S.

The overall heat transfer coefficients are also calculated in this experiment to determine

the total thermal resistance to heat transfer between two fluids. The resistance can be reduced

by increasing the surface area, which will lead to a more efficient heat exchanger

The calculated Reynolds Number is to determine whether the flow of water in shell and

tube heat exchanger is turbulent flow or laminar flow. After the Reynolds Number are obtained,

we can determine whether the flow is turbulent or laminar as for Re<2100, the flow is laminar

flow and for Re>4200, the flow is turbulent flow. For this experiment, based on the calculated

results, the water flow is turbulent at the tube sides of heat exchanger as Reynolds Number

that we obtained all exceeded 4200.

.

Conclusion

In conclusion, every objectives of this experiment had been achieved. Although there

might be errors, students still can achieve the objectives of this experiment. At the end of the

experiment, students are able to evaluate and study the heat load and head balance, LMTD and

overall heat transfer coefficient, as well as to calculate the Reynolds numbers at the shell and

tubes sides and also to measure and determine the shell and tube sides pressure drop.

Students also are able to learn the fundamentals of shell and tube heat exchanger, as well as

the applications and advantages of it. All the calculated data for this experiment can be referred

to the table in calculation section.

Recommendations

Follow safety regulations such as wearing a goggle, appropriate clothes, and gloves to

avoid any over-exposure to the substances which can be harmful.

All the temperature and flowrate readings are taken simultaneously as CW inlet

temperature is increasing gradually and CW outlet temperature varies together with the

HW inlet/outlet temperature.

The last set of temperature readings should be taken when all the temperatures are

fairly steady.

Whenever the annunciator TAH3 is activated during the course of the experiment, press

the red acknowledge button to silence the buzzer.

The first set of data must be taken right away after the process is started.

References

1. Coulson and Richardson; Chemical Engineering; Volume 1, 6th edition. 2. Max S. Peter & Klaus D. Timmerhaus; Plant Design and Economic for Chemical

Engineering; 4th edition; Page 576.3. Rase, Howard F; Chemical Reactor Design and for Process and plants; Volume 1; 1 st

edition.4. G.C DRYDEN; The Efficient Use of Energy; 1st edition.5. Frank P. Incropera, David P. DeWitt, 2002, Fundamental of Heat and Mass Transfer,

United State of America, 5th Edition, John Wiley & Sons, Inc.

Appendices

UNIVERSITI TEKNOLOGI MARA FAKULTI KEJURUTERAAN KIMIA

ENGINEERING CHEMISTRY LABORATORY (CHE 523)

No. Title Allocated Marks (%) Marks

1 Abstract/Summary 5 2 Introduction 5 3 Aims 5 4 Theory 5 5 Apparatus 5 6 Methodology/Procedure 10 7 Results 10 8 Calculations 10 9 Discussion 20 10 Conclusion 5 11 Recommendations 5 12 Reference / Appendix 5

NAME : NURFARAHIMA BINTI IBRAHIM MATRIC NO. : 2010389697GROUP : GROUP 2/EH2203AEXPERIMENT : EXPERIMENT 3 (SHELL AND TUBE HEAT EXCHANGER)DATE PERFORMED : 20 MARCH 2012SEMESTER : 3PROGRAMME / CODE :EH220SUBMIT TO :MADAM RABIATUL ADAWIYAH BT. ABDU AZIZ

13 Supervisor’s grading 10 TOTAL MARKS 100

Remarks:

Checked by:

---------------------------

Date:

UNIVERSITI TEKNOLOGI MARA FAKULTI KEJURUTERAAN KIMIA

ENGINEERING CHEMISTRY LABORATORY (CHE 523)

No. Title Allocated Marks (%) Marks

1 Abstract/Summary 5 2 Introduction 5 3 Aims 5 4 Theory 5 5 Apparatus 5 6 Methodology/Procedure 10 7 Results 10 8 Calculations 10 9 Discussion 20 10 Conclusion 5 11 Recommendations 5

NAME : NORSOLEHAH BINTI HANAFIAH MATRIC NO. : 2010305937GROUP : GROUP 2/EH2203AEXPERIMENT : EXPERIMENT 3 (SHELL AND TUBE HEAT EXCHANGER)DATE PERFORMED : 20 MARCH 2012SEMESTER : 3PROGRAMME / CODE :EH220SUBMIT TO :MADAM RABIATUL ADAWIYAH BT. ABDU AZIZ

12 Reference / Appendix 5 13 Supervisor’s grading 10

TOTAL MARKS 100

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Shell and Tube Heat Exchanger

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