Heat exchanger design

Submitted to:

Eng. Shadi Sawalha

Equipment design course (64444)

Prepared by:

Adel Hanin

Marwan Dwaikat

Nidal Marei

Department of Chemical Engineering

An-Najah National University

November 28, 2012

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ABSTRACT: ............................................................................................................................................................. 2

LIST OF TABLES: .............................................................................................................................................. 4

INTRODUCTION: .................................................................................................................................................... 5

THEORETICAL BACKGROUND: .............................................................................................................................. 21

SAMPLE OF CALCULATION OF OPTIMUM DIAMETER: .......................................................................................... 31

RESULTS: .............................................................................................................................................................. 38

DISCUSSION: ........................................................................................................................................................ 43

CONCLUSION: ...................................................................................................................................................... 47

APPENDIX: ........................................................................................................................................................... 48

WATER MSDS .................................................................................................................................................. 56

REFERENCES:........................................................................................................................................................ 67

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Abstract:

Heat exchangers are commonly used in practice in a wide range of applications, from heating

and air-conditioning systems in a household, to chemical processing and power production in

large plants.

This project aims to construct the most common type of heat exchangers; shell and tube heat

exchanger, it is desired to heat glycerin from 25°C to 50°C at a rate of 15 tons/hr using hot water

enters at 90°C and leaves at 60°C, with a flow rate of 7.38 tons/hr.

Different tube diameters ( ⁄ ⁄ ⁄

⁄ ,2) in, and lengths (6, 8, 12, 16) ft, were tested

in heat exchanger design with tow different type of pattern which triangle and square ; in order to

find the best layout according to (velocity of liquid inside tube, assumed and calculated value of

heat transfer coefficients, and finally the total capital operating and annual costs), the design of

heat exchangers was step by step procedure using Kerns method.

For triangle pattern, three tubes were in the range at ⁄ inch diameter with(8,12) ft length and

0.75 inch diameter with (16)ft length and this tube had the lower total annual cost with (44040

NIS).

On the other side, 4 different dimensions tubes had been obtained for square pattern, at ⁄ inch

with (6,8,12)ft length , and at 0.75 inch with 16 ft length which have the minmum total annual

cost in all acceptable tubes in the project with 43887 NIS.

0.75 inch diameter and 16 ft length was chosen as the optimum tube for the heat exchanger . in

this tube the velocity of water was calculated as 1.6 m/s . and for shell the velocity of glycerin

was calculated as 0.56 m/s with 446 baffles ..

The capital cost for our heat exchanger is 97743 NIS , and the annual operating cost 37370 NIS

with annual capital cost 6516 NIS and the total annual cost for this project 43887 NIS.

3 | P a g e 3

List of figures:

Figure (I.1): Double pipe heat exchanger with different flow types

Figure (I.2): Plate Heat Exchanger

Figure (I.3): Plate Fin Heat Exchanger

Figure (I.4): Shell and Tube Heat Exchanger

Figure (I.5): tube arrangement in heat exchanger

Figure (I.6): Double tube sheet

Figure (I.7): Inlet nozzle designs

Figure (I.8): Pass driver arrangement

Figure (I.9): Baffles

Figure (I.10) designing procedure using Kerns method

Figure (I.11) our heat exchanger diagram

Figure (R.1): Optimization curve by total annual cost

Figure (D1) Comparing according to total annual cost (NIS)

Figure (Ap.1): Correction factor figures

Figure (Ap.2): jh figure for tube side

Figure (Ap.3): jf figure for tube side

Figure (Ap.4): jh figure for shell side

Figure (Ap.5): jf figure for shell side

Figure (Ap.6): Shell bundle clearance calculation

Figure (Ap.7): jf calculation equation for tube side

Figure (Ap.8): jh calculation equation for shell side

Figure (Ap.9): jf calculation equation for shell side (for Re # from 0 to 300)

Figure (Ap.10): jf calculation equation for shell side (for Re # >300)

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List of tables:

Table (R.1): Determination of fluid place………

Table (R.2): Physical and chemical properties for water, glycerin and steel

Table (R.3): LMTD Results and Correction Factor

Table (R.4): Total annual cost for diameters and lengths that selected

Table (R.5): Final Result of Optimum Heat Exchanger

Table (Ap.1): Assumed U for shell and tube heat exchanger

Table (Ap.2): Fouling factor for several liquid and gases

Table (Ap.3): constants n , k

Table (Ap.4): MSDS for Water.

Table( Ap.5): viscosity of glycerin.

Table( Ap.6): density of glycerin.

Table (Ap.7): thermal conductivity of glycerin.

Table (Ap.8): Properties for Water.

Table (Ap.9) 14 BWG diameters

Table (Ap.10) Nomenclature

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Introduction:

Heat exchangers are devices that facilitate the exchange of heat between two fluids that are at

different temperatures while keeping them from mixing with each other. Heat exchangers are

commonly used in practice in a wide range of applications, from heating and air-conditioning

systems in a household, to chemical processing and power production in large plants. Heat

exchangers differ from mixing chambers in that they do not allow the two fluids involved to mix.

In a car radiator, for example, heat is transferred from the hot water flowing through the radiator

tubes to the air flowing through the closely spaced thin plates outside attached to the tubes.

Heat transfer in a heat exchanger usually involves convection in each fluid and conduction

through the wall separating the two fluids. In the analysis of heat exchangers, it is convenient to

work with an overall heat transfer coefficient U that accounts for the contribution of all these

effects on heat transfer. The rate of heat transfer between the two fluids at a location in a heat

exchanger depends on the magnitude of the temperature difference at that location, which varies

along the heat exchanger. {1}

There are two primary classifications of heat exchangers according to their flow arrangement. In

parallel-flow heat exchangers, the two fluids enter the exchanger at the same end, and travel in

parallel to one another to the other side. In counter-flow heat exchangers the fluids enter the

exchanger from opposite ends. The counter current design is most efficient, in that it can transfer

the most heat from the heat (transfer) medium. See countercurrent exchange. In a cross-flow heat

exchanger, the fluids travel roughly perpendicular to one another through the exchanger.

For efficiency, heat exchangers are designed to maximize the surface area of the wall between

the two fluids, while minimizing resistance to fluid flow through the exchanger. The exchanger's

performance can also be affected by the addition of fins or corrugations in one or both directions,

which increase surface area and may channel fluid flow or induce turbulence.

The driving temperature across the heat transfer surface varies with position, but an appropriate

means temperature can be defined. In most simple systems this is the "log mean temperature

difference" (LMTD).

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Types of heat exchangers:

Different heat transfer applications require different types of hardware and different

configurations of heat transfer equipment. The attempt to match the heat transfer hardware to the

heat transfer requirements within the specified constraints has resulted in numerous types of

innovative heat exchanger designs.

Double-pipe heat exchanger

The simplest type of heat exchanger consists of two concentric pipes of different diameters, as

shown in Figure 13–1, called the double-pipe heat exchanger. One fluid in a double-pipe heat

exchanger flows through the smaller pipe while the other fluid flows through the annular space

between the two pipes. Two types of flow arrangement are possible in a double-pipe heat

exchanger: in parallel flow, both the hot and cold fluids enter the heat exchanger at the same end

and move in the same direction. In counter flow, on the other hand, the hot and cold fluids enter

the heat exchanger at opposite ends and flow in opposite directions.

Figure (I.1): Double pipe heat exchanger with different flow types

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Plate heat exchanger

One is composed of multiple, thin, slightly-separated plates that have very large surface areas

and fluid flow passages for heat transfer. This stacked-plate arrangement can be more effective,

in a given space, than the shell and tube heat exchanger. Advances in gasket and brazing

technology have made the plate-type heat exchanger increasingly practical. In HVAC (Heating,

Ventilating, and Air Conditioning) applications, large heat exchangers of this type are called

plate-and-frame; when used in open loops, these heat exchangers are normally of the gasket type

to allow periodic disassembly, cleaning, and inspection. There are many types of permanently-

bonded plate heat exchangers, such as dip-brazed and vacuum-brazed plate varieties, and they

are often specified for closed-loop applications such as refrigeration. Plate heat exchangers also

differ in the types of plates that are used, and in the configurations of those plates. Some plates

may be stamped with "chevron" or other patterns, where others may have machined fins and/or

grooves.

Figure (I.2): Plate Heat Exchanger.

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Adiabatic wheel heat exchanger

A third type of heat exchanger uses an intermediate fluid or solid store to hold heat, which is

then moved to the other side of the heat exchanger to be released. Two examples of this are

adiabatic wheels, which consist of a large wheel with fine threads rotating through the hot and

cold fluids, and fluid heat exchangers.

Plate fin heat exchanger

This type of heat exchanger uses "sandwiched" passages containing fins to increase the

affectivity of the unit. The designs include cross flow and counter flow coupled with various fin

configurations such as straight fins, offset fins and wavy fins.

Plate and fin heat exchangers are usually made of aluminum alloys which provide higher heat

transfer efficiency. The material enables the system to operate at a lower temperature and reduce

the weight of the equipment. Plate and fin heat exchangers are mostly used for low temperature

services such as natural gas, helium and oxygen liquefaction plants, air separation plants and

transport industries such as motor and aircraft engines.

Pillow plate heat exchanger

A pillow plate exchanger is commonly used in the dairy industry for cooling milk in large direct-

expansion stainless steel bulk tanks. The pillow plate allows for cooling across nearly the entire

Figure (I.3): Plate Fin Heat Exchanger.

9 | P a g e 9

surface area of the tank, without gaps that would occur between pipes welded to the exterior of

the tank.

The pillow plate is constructed using a thin sheet of metal spot-welded to the surface of another

thicker sheet of metal. The thin plate is welded in a regular pattern of dots or with a serpentine

pattern of weld lines. After welding the enclosed space is pressurized with sufficient force to

cause the thin metal to bulge out around the welds, providing a space for heat exchanger liquids

to flow, and creating a characteristic appearance of a swelled pillow formed out of metal.

Fluid heat exchangers

This is a heat exchanger with a gas passing upwards through a shower of fluid (often water), and

the fluid is then taken elsewhere before being cooled. This is commonly used for cooling gases

whilst also removing certain impurities, thus solving two problems at once. It is widely used in

espresso machines as an energy-saving method of cooling super-heated water to be used in the

extraction of espresso.

Waste heat recovery units

A Waste Heat Recovery Unit (WHRU) is a heat exchanger that recovers heat from a hot gas

stream while transferring it to a working medium, typically water or oils. The hot gas stream can

be the exhaust gas from a gas turbine or a diesel engine or a waste gas from industry or refinery.

Dynamic scraped surface heat exchanger

Another type of heat exchanger is called "(dynamic) scraped surface heat exchanger". This is

mainly used for heating or cooling with high-viscosity products, crystallization processes,

evaporation and high-fouling applications. Long running times are achieved due to the

continuous scraping of the surface, thus avoiding fouling and achieving a sustainable heat

transfer rate during the process.

10 | P a g e 10

Phase-change heat exchangers

In addition to heating up or cooling down fluids in just a single phase, heat exchangers can be

used either to heat a liquid to evaporate (or boil) it or used as condensers to cool a vapor and

condense it to a liquid. In chemical plants and refineries, reboiler used to heat incoming feed for

distillation towers are often heat exchangers. {2}

Shell and tube heat exchangers

The most common type of heat exchanger in industrial application is the shell-and-tube heat

exchanger, shown in Figure (4). Shell-and-tube heat exchangers contain a large number of tubes

(sometimes several hundred) packed in a shell with their axes parallel to that of the shell. Heat

transfer takes place as one fluid flows inside the tubes while the other fluid flows outside the

tubes through the shell. Baffles are commonly placed in the shell to force the shell-side fluid to

flow across the shell to enhance heat transfer and to maintain uniform spacing between the tubes.

Despite their widespread use, shell and- tube heat exchangers are not suitable for use in

automotive and aircraft applications because of their relatively large size and weight. Note that

the tubes in a shell-and-tube heat exchanger open to some large flow areas called headers at both

ends of the shell, where the tube-side fluid accumulates before entering the tubes and after

leaving them.

Figure (I.4): Shell and Tube Heat Exchanger.

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Shell-and-tube heat exchangers are further classified according to the number of shell and tube

passes involved. Heat exchangers in which all the tubes make one U-turn in the shell, for

example, are called one-shell-pass and two tubes passes heat exchangers. Likewise, a heat

exchanger that involves two passes in the shell and four passes in the tubes is called a two-shell-

passes and four-tube-passes heat exchanger. {1}

Components of Shell and Tube Heat Exchangers:

1. Tubes: The tubes are the basic component of the shell and tube exchanger, providing

the heat transfer surface between one fluid flowing inside the tube and the other

fluid flowing across the outside of the tubes. The tubes may be seamless or welded

and most commonly made of copper or steel alloys. Other alloys of nickel, titanium, or

aluminum may also be required for specific applications. The tubes may be either bare or

with extended or enhanced surfaces on the outside. Typical tube will be extended

surface. Extended or enhanced surface tubes are used when one fluid has a

substantially lower heat transfer coefficient than the other fluid. Doubly enhanced

tubes that is, with enhancement both inside and outside are available that can reduce

the size and cost of the exchanger. Extended surfaces, (finned tubes) provide two to four

times as much heat transfer area on the outside as the corresponding bare tube, and

this area ratio helps to offset a lower outside heat transfer coefficient.

Figure (I.5): tube arrangement in heat exchanger

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2. Tube sheets: the tubes are held in space by being inserted into holes in the tube

sheet and there either expanded into grooves cut into the holes or welded to the tube sheet

where the tube protrudes from the surface The tube sheet is usually a single round plate of

metal that has been suitably drilled and grooved to take the tubes (in the desired pattern), the

gaskets, the spacer rods, and the bolt circle where it is fastened to the shell. However, where

mixing between the two fluids (in the event of leaks where the tube is sealed into the tube

sheet) must be avoided, a double tube sheet such as is shown in Fig. 1.36 may be provided. The

space between the tube sheets is open to the atmosphere so any leakage of either fluid

should be quickly detected. Triple tube sheets (to allow each fluid to leak separately to the

atmosphere without mixing) and even more exotic designs with inert gas shrouds and/or

leakage recycling systems are used in cases of extreme hazard or high value of the fluid. The

tube sheet, in addition to its mechanical requirements, must withstand corrosive attack by both

fluids in the heat exchanger and must be electrochemically compatible with the tube and all

tube-side material. Tube sheets are sometimes made from low carbon steel with a thin layer

of corrosion-resisting alloy metallurgic ally bonded to onside.

Figure (I.6): Double tube sheet

3. Shell and Shell-Side Nozzles. The shell is simply the container for the shell-side fluid,

and the nozzles are the inlet and exit ports. The shell normally has a circular cross section

and is commonly made by rolling a metal plate of the appropriate dimensions into a

13 | P a g e 13

cylinder and welding the longitudinal joint ("rolled shells"). Small diameter shells (up to

around 24 inches in diameter) can be made by cutting pipe of the desired diameter to the

correct length ("pipe shells"). The roundness of the shell is important in fixing the

maximum diameter of the baffles that can be inserted and therefore the effect of shell-to-

baffle leakage. Pipe shells are more nearly round than rolled shells unless particular

care is taken in rolling, In order to minimize out-of-roundness, small shells are

occasionally expanded over a mandrel; in extreme cases, the shell is cast and then bored out

on a boring mill. In large exchangers, the shell is made out of low carbon steel wherever

possible for reasons of economy, though other alloys can be and are used when

corrosion or high temperature strength demands must be met. The inlet nozzle often has

an impingement plate set just below to divert the incoming fluid jet from impacting

directly at high velocity on the top row of tubes. Such impact can cause erosion,

cavitations.

Figure (I.7): Inlet nozzle designs

In order to put the impingement plate in and still leave enough flow area between the shell

and plate for the flow to discharge without excessive pressure loss, it may be necessary to

omit some tubes from the full circle pattern. Other more complex arrangements to distribute

the entering flow, such as slotted distributor plate and an enlarged annular distributor

section are occasionally employed.

14 | P a g e 14

4. Tube-Side Channels and Nozzles: Tube-side channels and nozzles simply control the

flow of the tube-side fluid into and out of the tubes of the exchanger. Since the tube-side

fluid is generally the more corrosive, these channels and nozzles will be often made out

of alloy material (compatible with the tubes and tube sheets, of course). They may be

clad instead of solid alloy.

5. Channel Covers: The channel covers are round plates that bolt to the channel flanges

and can be removed for tube inspection without disturbing the tube-side piping. In

smaller heat exchangers, bonnets with flanged nozzles or threaded connections for the

tube-side piping are often used instead of channels and channel covers.

6. Pass Divider: A pass divider is needed in one channel or bonnet for an exchanger

having two tube-side passes, and they are needed in both channels and bonnets for an

exchanger having more than two passes. If the channels or bonnets are cast, the dividers

are integrally cast and then faced to give a smooth bearing surface on the gasket

between the divider and the tube sheet. If the channels are rolled from plate or built up

from pipe, the dividers are welded in place. The arrangement of the dividers in

multiple-pass exchangers is somewhat arbitrary, the usual intent being to provide nearly

the same number of tubes in each pass, to minimize the number of tubes lost from the

tube count, to minimize the pressure difference across any one pass divider (to

minimize leakage and therefore the violation of the MTD derivation), to provide

adequate bearing surface for the gasket and to minimize fabrication complexity and cost.

15 | P a g e 15

Figure (I.8): Pass driver arrangement

7. Baffles: Baffles serve two functions: Most importantly, they support the tubes in the

proper position during assembly and operation and prevent vibration of the tubes caused

by flow-induced eddies, and secondly, they guide the shell-side flow back and forth

across the tube field, increasing the velocity and the heat transfer coefficient. The most

common baffle shape is the single segmental .The segment sheared off must be less

than half of the diameter in order to insure that adjacent baffles overlap at least one full

tube row. For liquid flows on the shell side, a baffle cut of 20 to 25 percent of the

diameter is common; for low pressure gas flows, 40 to 45 percent (i.e., close to the

maximum allowable cut) is more common, in order to minimize pressure drop. The

baffle spacing should be correspondingly chosen to make the free flow areas through

the "window" (the area between the baffle edge and shell) and across the tube bank

roughly equal. For many high velocity gas flows, the single segmental baffle

configuration results in an undesirably high shell-side pressure drop.{3}

16 | P a g e 16

Figure (I.9): Baffles.

the proper selection of optimum heat exchanger depends on many factors:

1. Heat Transfer Rate: This is the most important quantity in the selection of a heat

exchanger. A heat exchanger should be capable of transferring heat at the specified rate

in order to achieve the desired temperature change of the fluid at the specified mass flow

rate.

2. Cost: Budgetary limitations usually play an important role in the selection of heat

exchangers, except for some specialized cases where “money is no object.” An off-the-

shelf heat exchanger has a definite cost advantage over those made to order. However, in

some cases, none of the existing heat exchangers will do, and it may be necessary to

undertake the expensive and time-consuming task of designing and manufacturing a heat

exchanger from scratch to suit the needs. This is often the case when the heat exchanger

is an integral part of the overall device to be manufactured. The operation and

maintenance costs of the heat exchanger are also important considerations in assessing

the overall cost.

3. Pumping Power: In a heat exchanger, both fluids are usually forced to flow by pumps or

fans that consume electrical power. Minimizing the pressure drop and the mass flow rate

of the fluids will minimize the operating cost of the heat exchanger, but it will maximize

the size of the heat exchanger and thus the initial cost. As a rule of thumb, doubling the

17 | P a g e 17

mass flow rate will reduce the initial cost by half but will increase the pumping power

requirements by a factor of roughly eight. Typically, fluid velocities encountered in heat

exchangers range between 0.7 and 7 m/s for liquids and between 3 and 30 m/s for gases.

Low velocities are helpful in avoiding erosion, tube vibrations, and noise as well as

pressure drop.

4. Size and Weight: Normally, the smaller and the lighter the heat exchanger, the better it

is. This is especially the case in the automotive and aerospace industries, where size and

weight requirements are most stringent. Also, a larger heat exchanger normally carries a

higher price tag. The space available for the heat exchanger in some cases limits the

length of the tubes that can be used.

5. Type: The type of heat exchanger to be selected depends primarily on the type of fluids

involved, the size and weight limitations, and the presence of any phase change

processes. For example, a heat exchanger is suitable to cool a liquid by a gas if the

surface area on the gas side is many times that on the liquid side. On the other hand, a

plate or shell-and-tube heat exchanger is very suitable for cooling a liquid by another

liquid.

6. Materials: The materials used in the construction of the heat exchanger may be an

important consideration in the selection of heat exchangers. For example, the thermal and

structural stress effects need not be considered at pressures below 15 atm or temperatures

below 150°C. But these effects are major considerations above 70 atm or 550°C and

seriously limit the acceptable materials of the heat exchanger. A temperature difference

of 50°C or more between the tubes and the shell will probably pose differential thermal

expansion problems and needs to be considered. In the case of corrosive fluids, we may

have to select expensive corrosion-resistant materials such as stainless steel or even

titanium if we are not willing to replace low-cost heat exchangers frequently.

7. Other Considerations: There are other considerations in the selection of heat

exchangers that may or may not be important, depending on the application. For example,

being leak-tight is an important consideration when toxic or expensive fluids are

involved. Ease of servicing, low maintenance cost, and safety and reliability are some

other important considerations in the selection process. Quietness is one of the primary

18 | P a g e 18

considerations in the selection of liquid-to-air heat exchangers used in heating and air

conditioning applications.{1}

Procedure of design (Kerns method):

Figure (I.10) designing procedure using Kerns method.

19 | P a g e 19

Figure (I.10)>continued>designing procedure using Kerns method.

20 | P a g e 20

In our heat exchanger, shell and tube exchanger was designed to heat glycerin from 25°C to

50°C at a rate of 15 tons/hr by using hot water enters at 90°C and leaves at 60°C.

Figure (I.11) our heat exchanger diagram.

21 | P a g e 21

Theoretical Background:

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22 | P a g e 22

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23 | P a g e 23

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24 | P a g e 24

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25 | P a g e 25

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26 | P a g e 26

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27 | P a g e 27

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hd

d

Kw

d

dd

hhU

where

unofcalculatio

%150

)26..(..............................%.........100%

:*

.)(:

.)(:

)../(:

)../(:

)../(:

)../(:

)../(:

;

0

2

2

0

2

2

0

2

0

U

U

UUUinerror

UinError

mdiameterinsided

mdiameteroutsided

CmWtcoefficientransferheatdirtinsideh

CmWtcoefficientransferheatdirtoutsideh

CmWtcoefficientransferheatinsideh

CmWtcoefficientransferheatoutsideh

CmWtcoefficientransferheatoveralloutsideU

where

assumed

assumedcalculated

i

id

d

i

28 | P a g e 28

Calculation of Shell side:

)29.....(........................................785.027.1

:

:)(

)28.....(........................................

:

5

).(

).(

25.1)(

;

)27......(........................................

:)(

'

2

0

2

0

..

0

0

0

dPd

d

typeSquarefor

diameterhydrolicdiameterequivalentsideShell

A

m

A

QU

velocitymasssideShell

DspacingbaffleL

mmdiameterinsideshellD

mmdiameteroutsidetubed

dmmpitchtubeP

where

P

LDdPA

AflowcrossofArea

rocedurePMethodsKern

te

S

S

S

S

SB

S

t

t

BStS

S

)32.....(..............................PrRe

)31.........(........................................Re

)30..(..............................917.01.1

:

14.0

33.0

2

0

2

0

w

h

f

es

eS

te

jk

dhNu

dU

dPd

d

trianglealequilaternfor

29 | P a g e 29

)34....(........................................

:

)33..(....................2

8

.

14.02

S

shell

w

S

Be

S

fS

PmP

sideshellforpowerPump

U

L

L

d

DjP

3.3) Cost calculation:

)35.......(....................Kwatt.hr

(NIS)Cost )(P(NIS) A.O.C rsworkinghouKwatt

6)........(3....................)......... areafer Heat trans88(10000($)cost Capital

)37.........(......................................................................lifeProject

(NIS)cost CapitalA.C.C

:A.C.Ccost capital annual

)38...(..................................................A.O.C)) A.O.C(..T.A.C

:(NIS) (T.A.C)Cost Annual Total

shelltubes

CCA

Correction factor calculation:

F1-2 =

*√

+ (

)

( √

√ )

(used for 1 shell pass) ………………...(39)

F2-4 =

*√

+ (

)

( √

√ )

(used for 2-4 shell pass) ………………...(40)

30 | P a g e 30

√

Where, T1: temperature of fluid inside shell.

T2: temperature of fluid outside shell.

t1: temperature of fluid inside tube.

t2: temperature of fluid outside tube.

31 | P a g e 31

Sample of calculation of optimum diameter:

Tube calculation

QC= QH

QC=

I = 258.17 KW

From figure Ft= 0.92

(

)

32 | P a g e 32

= 0.92 x37.44= 34.44

lmTUAFQ

Assume U =590 W/m².C

A = 12.92 m2

Find Number of tubes:

OSOt AAN /

ASO = 0.000172 m2

200134.0.88.4.*01905.0* mDLAo

tubesN t 47860.46000172.0

6858.13

Number of tubes per Pass:

8810.76

860.46

......

passesofNumber

NpasspertubesofNumber t

Cross Sectional area (Ac):

Dout=0.75inch=0.75 inch*(0.0254 m/inch)=0.01905m

Thick=0.083inch*(0.021184m/inch)=0.0021m

Dinsid=Dout - (2*thick) =0.584-(0.0021*2) =0.014834m

2)(*4

DinsidAC

For one tube

Total flow area= CA (one tube)*Number of tubes per pass

22 000172.0)014834.0(*4

mAC

33 | P a g e 33

=0.000172*3246.860=0.001349 m²

Velocity for one tube

areaflowTotal

rateflowVolumetubeofVelocity

..

....

smDensity

rateflowmassrateflowVolume /0021045.0

86.974

051637.2.... 3

areaflowTotal

rateflowVolumetubeofVelocity

..

....

=0.0021045/0.00134=1.55925 m/s

hi= (4200*(1.35+0.02*75)*(1.55925)0.8

)/ (14.834)0.2

=9027.07 (W/m2. °C)

Reynolds Number for tube:

32.593520003799.0

584.0*55925.1*86.974.Re

idNumber

34 | P a g e 34

WPm

P

PaP

f

f

where

Nd

NLfUP

ttube

t

i

i

P

i

Pitt

26886.9746.0

725.76447051637.2

725.7644764014834.0

688.4003135.04

2

55925.1*86.974

003135.0.028.3)32.59352ln(58.1

28.3Re)ln(58.1

;

44

2

2

2

2

2

Shell side calculation (Glycerin calculation):

Diameter of Bundle:

ntob

k

NdD

1

)(

For equilateral pattern & 8 pass:

k=0.402

n=2.617

617..2

1

)402.0

860.46(01905.0bD

mDb 01905.0

Pt & clearance between tubes:

35 | P a g e 35

mdP ot 0238125.001905.0*25.1*25.1

Clearance between tubes= ((Db*10) + 8) /1000 = 0.008195 m.

Clearance between tubes= ((0.01905*10) + 8) /1000 = 0.008195 m.

Shell Diameter

clearanceDD bS

mDS 0272405.0008195.001905.0

Baffle Spacing

mDL sB 1078.05/0272405.05/

Number of Baffles

)1(.. BL

LBaffflesofNumber

= 862.4461)0108962.0

88.4( Baffles

Area of cross flow in 2 shell:

2

)(

t

BSot

S

p

LDdp

A

2

0238125.0

01089.0*02724.0*)01905.002381.0(

SA 0.56151 m²

Velocity for Shell:

s

SA

rateFlowU

.= sm /56.0

56151.005810.01250

1666.4

Hydraulic Diameter (de)

36 | P a g e 36

= (1.1/0.01905)*((0.023812)2- (0.917*0.01905

2)) = 0.01352 m

2

Reynolds number

eS dUnumber .Re

08261.26364.0

1250*01352.0*8992.701.Re number

For two Shell

14.0

2

)(2

)2

)((8w

S

Be

Sf

U

L

L

d

DjP

Jf=

Jf= 0.2269*0.102557^(-0.164) = 0.93912

243.13353252

)56.0(*1250()

0108962.0

88.4*2(*)

01352.0

02724.0(*93912.0*8

2

P

kpaP 325.1335

WKWPm

P ttube 35.741841847.7

12506.0

325.13351666.4

U theoretical

ii

o

idi

o

w

i

o

o

odoO hd

d

hd

d

k

d

dd

hhU

1.

1.

2

)ln(111

Where: ho = h S = 827.2610(W/m2. °C)

)917.0(1.1 22

ot

o

e dPd

d

37 | P a g e 37

h od = 5000 (W/m2. °C)

h id = 4000 (W/m2. °C)

hi= 9027.07(W/m2. °C)

d o =0.01405 m

di =0.014834 m

Kw= 60 (W/m2. °C)

Then U Calculated

= 523 W/m².C

% of error = %100*Calculated

assumedCalculated

U

UU

%16.5523

550523.%

errorof

Capital Cost

Cost of H.E ($) =24000+46*(13.6858^1.2)= 97743.33

Annual capital Cost =15

tCapitalCos

NIStcapitalAnnual 222.651615

33.97743cos..

Annual Operating Cost =Power of pump * operating hour per year (24*365)*Cost

of electrical energy (0.7NIS/ KW. hr)

Assume: 1 $ =3.9 NIS

Total annual Operating Cost = 2751* 24* 365* 0.925* 0.7 = 37370.81 NIS

Annual Total Cost =Annual Capital Cost +Annual Operating Cost

Annual total Cost = 6516.222+ 37370.81= 43887.03 NIS

38 | P a g e 38

Results:

Table (R.1): Determination of fluid place.

Properties Limitation Fluid

Corrosion The more corrosive fluid should be

allocated in tube side

Water

Fouling The fluid that has greatest

tendency to foul the heat

exchanger surfaces should be

placed in tube side

Water

Fluid Temp. The higher temp. Fluid should be

placed in tubes and that will

reduce the overall cost

Water

Operating Pressure The higher pressure stream should

be allocated to the tube side

Water

Pressure Drop The fluid with the lowest

allowable pressure drop should be

allocated to the tube side

water

Viscosity The viscous fluid should be

allocated to the shell side

Glycerin

Stream Flow rates To achieve the most economical

design, the fluid with the lowest

flow rates should be allocated to

the shell side

Glycerin

From this figure the points that support the allocation of water in tubes is more than the glycerin ,

so water put in tube side and glycerin in shell side.

39 | P a g e 39

Table (R.2): Physical and chemical properties for water, glycerin and steel.

Water Glycerin

Temp (oC) 75 37.5

Temp (K) 348 310.65

Density (Kg/m3) 974.86 1250.919

Viscosity (Pa.s) 3.799E-04 0.364

Specific Heat (J/Kg.K) 4194.653 2478

Thermal Conductivity

(W/m.K)

0.661 0. 286

Dirt factor (w/m2.k) 4000 5000

Prandtl # 2.41 3154

Metal of construction Carbon Steel

Thermal Conductivity

(W/m.K)

45

The above physical and chemical properties was determined by using both references and

correlations , were the properties that used in calculation such as Prandtl # are calculated

at average temperature.

The calculation for them is in the sample of calculation.

40 | P a g e 40

Table (R.3): LMTD Results and Correction Factor.

Tubes Shell

Flow Rate (kg/s) 2.05 4.167

Heat Duty (W) 258177

Inlet Temp (oC) 90 25

Outlet Temp (oC) 60 50

R 0.833

S 0.4615

Correction Factor F 0.92

∆Tlm 37.44

LMTD 34.44

Table (R.4): Total annual cost for diameters and lengths that selected in range of work for

triangular(t) and square (s) shape..

Diameters

(in)

Lengths (ft)

6 8 12 16

0.5 t ---- 78061.57

115935.9

----

Cost

(NIS)

0.75 t ---- ---- ---- 44040.81

0. 5 s 59974.84

78061.57

115935.9

----

0.75 s ---- ---- ---- 44040.81

41 | P a g e 41

Figure (R.1): Optimization curve by total annual cost.

From this figure, the minimum total annual cost is for (s 0.75\16) 0.75 in diameter with 16 ft tube

length.

0

20000

40000

60000

80000

100000

120000

140000

t 0.5\12 t 0.5\8 t 0.75\16 s 0.5\6 s 0.5\8 s 0.5\12 s 0.75\16

T.A

.C (

$)

diameter (in)\length (ft) (t: triangle , s: square)

42 | P a g e 42

Table (R.5): Final Result of Optimum Heat Exchanger.

Arrangement of tubes Equilateral Triangle

Tube diameter (in) 0.75

Tube length (ft) 16

U (W/m2.0C) 560

Heat Transfer Area (m2)

13.68

Tube Velocity (m/s) 1..55

Shell Velocity (m/s) 0.56

# of Tubes 105

# of Tube Passes 6

# of Shell Passes 1

Shell Diameter (m) 0.0272405

Tube Pitch (m) 0.024

# of Baffles 447

∆P for Tube (kPa) 76.447

∆P for Shell (kPa) 1335.325

Power for tubes pump (W) 268

Power for shell pump (W) 7418

Inside Heat Transfer Coefficient hi

(W/m2.oC)

9958

Outside Heat Transfer Coefficient hs

(W/m2.oC)

1003.82

Annual Operating Cost (NIS) 37370

Annual Capital Cost (NIS) 6516

Total Annual Cost (NIS) 43887

43 | P a g e 43

Discussion:

The main objective of this experiment was to design a heat exchanger that achieves 258.177 KW

heat duty, to heat glycerin from 25 °C to 50 °C using water which enters the heat exchanger at 90

°C and leaves at 60 °C. First step was locating the fluids in shell / tube side, water was allocating

in the tube side, because it is more corrosive this give an easy replacement for the fouled tubes.,

has more tendency to fouling, has higher temperature and higher temperature fluid should be

placed in tubes – temperature has a little effect in allocating fluids- and that will reduce the

overall cost, water also has higher pressure stream, has lower allowable pressure drop. But

glycerin has higher viscosity, and higher flow stream, and fluid with higher viscosity and higher

flow rate, should be located in the tube side. But water has more suitable properties than

glycerin, and it was allocated in the tube side. Table (N.1) shows allocation properties and

comparing between them.

To determine number of shells and tubes wanted, a correction factor f was calculated, it should

be greater than or equal 0.75, it was obtained from figure (Ap.1) or using equation (44). To

obtain correction factor Fm which value was 0.92.

First assumption of overall heat transfer coefficient was 590 (W/m2. °C), this is the average

value assumed from table (Ap.1) between water and organic solution.

Carbon steel was chosen for both tube and shell side due to its withstand high temperature of

fluids, has no oxidation with water or glycerin, its resistance to pressure and corrosion is high, it

is available and cheaper than other alternatives.

Different diameters and lengths were taken in design calculations, smaller diameters ( ⁄ – 1) in

are preferred because for most duties, they will give more compact and cheaper, although the

larger diameter are easier to clean by mechanical methods, but they would be selected for heavily

fouling fluids. Thickness was selected to withstand the internal pressure and give an adequate

corrosion allowance (14 BWG: Birmingham Wire Gauge), for a given surface area the use of

longer tubes will reduce the shell diameter, which will result in a lower cost exchanger.

44 | P a g e 44

Tubes arrangements have many shapes, like; equilateral triangle, square, and rotated square.

For rotated square it have high heat transfer area which is good, but it’s disadvantage is its high

pressure drop, triangle and rotated square patterns have higher heat transfer rates, but at the

expense of higher pressure drop than square pattern. In this project optimization done between

triangle and square patterns to find the optimum diameter and length for each one .

A certain distance between tube centers should be taken, which is called pitch distance and

equals 1.25 times the outside diameter of the tubes, for the tube side passes, passes are used to

increase the length of the flow path, although increasing the length of tubes can give the same

goal, but passes decrease the total length -and so decrease the area- of the heat exchanger. Passes

also used to give the required tube side design velocity, the fluid inside tube velocity preferred to

be in range of 1.5 to 3 m/s, because it will increase the pressure drop and so the power needed

and the total cost.

According to the velocity range allowable, and percent of error in heat transfer coefficient, these

values were obtained to be good diameters and lengths. For triangle pattern at diameter of ⁄

inch, and lengths of (8, 12) ft, diameter of inch and lengths of (16) ft, and for square

pattern diameter of inch and lengths of (6,8,12) ft and diameter of inch and lengths of (16)

ft. Other diameters obtained velocities or/and error in U, not recommended, at large diameters,

the velocity will decrease which decreases Reynolds number and cause increasing in the heat

transfer rate coefficient and U will increase. For diameters of (1, 1 ⁄ , 1

⁄ ) in, there were no

obtained values, because we have constant flow rate, so as we increase the diameter, as the

velocity decreases.

Seven values were obtained, we depend on the final steps of optimization on the total annual cost

and 0.75 inch diameter with 16 ft length had been chosen as the optimum diameter with 43887

NIS.

45 | P a g e 45

Figure (D1) Comparing according to total annual cost (NIS).

As it is shown, the minimum total annual cost was 43887.03 (NIS), and the closest cost is for the

same diameter and length but with square patterns with 44040 (NIS.

Heat transfer coefficient in the tube side was greater, because diameter is less than the shell

diameter, and Reynolds number is greater than shell side, in the other hand, pressure drop in the

shell side is greater than the tube side because it has greater length, and diameter.

to Increase Recommended Velocity

It was found from the figures and the trials for each diameter and length that the

recommended velocity can be reached by different variables.

1. Increase flow rate

2. Decrease diameter

3. Decrease number of tubes

4. Increase number of passes

t 0.5\12 t 0.5\8t

0.75\16s 0.5\6 s 0.5\8 s 0.5\12

s0.75\16

Cost (NIS) 115935.9 78061.57 44040.81 59974.84 78061.57 115935.9 43887.03

0

20000

40000

60000

80000

100000

120000

140000

T.A

.C (

$)

diameter (in)\length (ft) (t: triangle , s: square)

46 | P a g e 46

Sources of error:

Errors can be result from many sources, personal error by calculation, uses of assumptions that

were taken in this project, for example number of tube passes was taken 6 passes, while it can be

less than this like 4 or more like 8 , and another source of error was using figures and

approximation of some terms like the correction viscosity

w

It was assumed that there was no heat loss from shell to surrounding, so insulation is needed in

this case to avoid the heat loss that affects on the heat transfer between the two fluids decrees

the efficiency.

All these factors can be affected on the result.

47 | P a g e 47

Conclusion:

In the designing of the shell and tube heat exchanger, square arrangement was selected.

For the optimum heat exchanger:

1. The length of the tube equal to (16) ft.

2. The outside diameter of the tube is equal to (0.75) inch.

3. The number of tubes needed is equal to (47) tubes.

4. The number of tube passes is equal to (6 passes).

5. The number of shell passes is equal to (1 passes).

6. The number of baffles needed is equal to (446) baffle.

7. Heat transfer area is equal to (12.744) m2

8. Inside Heat Transfer Coefficient hi is equal to (9027 W/m2.oC).

9. Outside Heat Transfer Coefficient hs is equal to 827 W/m2.oC).

10. The pumping power in the tube side is equal to 7419 watt.

11. Total annual capital cost is equal to (43887) NIS .

12. The annual operating cost is equal to (37370) NIS.

13. The annual capital cost (6516) NIS.

48 | P a g e 48

Appendix:

Figure (Ap.1): Correction factor figures.

49 | P a g e 49

Figure (Ap.2): jh figure for tube side.

Figure (Ap.3): jf figure for tube side.

50 | P a g e 50

Figure (Ap.4): jh figure for shell side.

Figure (Ap.5): jf figure for shell side.

51 | P a g e 51

Figure (Ap.6): Shell bundle clearance calculation.

52 | P a g e 52

Figure (Ap.7): jf calculation equation for tube side.

Figure (Ap.8): jh calculation equation for shell side.

y = 0.0517x-0.255 R² = 0.9988

0

0.001

0.002

0.003

0.004

0.005

0.006

0.007

0.008

0.009

0.01

0 20000 40000 60000 80000 100000 120000

jf

Re #

y = 0.4907x-0.48 R² = 0.9981

0

0.02

0.04

0.06

0.08

0.1

0.12

0.14

0.16

0.18

0.2

0 10000 20000 30000 40000 50000 60000

jh

Re #

53 | P a g e 53

Figure (Ap.9): jf calculation equation for shell side (for Re # from 0 to 300).

Figure (Ap.10): jf calculation equation for shell side (for Re # >300).

0

0.5

1

1.5

2

2.5

3

0 50 100 150 200 250 300 350

jf

Re #

0

0.01

0.02

0.03

0.04

0.05

0.06

0.07

0.08

0.09

0.1

0 1000 2000 3000 4000 5000 6000 7000

jf

Re #

54 | P a g e 54

Table (Ap.1): Assumed U for shell and tube heat exchanger.

55 | P a g e 55

Table (Ap.2): Fouling factor for several liquid and gases.

Table (Ap.3): Constants used n,k.

56 | P a g e 56

Table (Ap.4): MSDS for Water.

Water MSDS

1. Product Identification

Synonyms: Hydrogen oxide; Dihydrogen oxide; Distilled water

CAS No.: 7732-18-5

Molecular Weight: 18.02

Chemical Formula: H2O

Product Codes: J.T. Baker: 4022, 4201, 4212, 4216, 4218, 4219, 4221, 6906, 9823, 9831, XL-317

Mallinckrodt: 6795, H453, V564

2. Composition/Information on Ingredients

Ingredient CAS No Percent

Hazardous

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

------

Water 7732-18-5 100%

No

3. Hazards Identification

Emergency Overview --------------------------

Not applicable.

SAF-T-DATA(tm)

Ratings (Provided here for your convenience)

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

Health Rating: 0 - None

Flammability Rating: 0 - None

Reactivity Rating: 1 - Slight

Contact Rating: 0 - None

Lab Protective Equip: GOGGLES; LAB COAT

Storage Color Code: Green (General Storage)

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

57 | P a g e 57

Potential Health Effects ----------------------------------

Water is non-hazardous.

Inhalation: Not applicable.

Ingestion: Not applicable.

Skin Contact: Not applicable.

Eye Contact: Not applicable.

Chronic Exposure: Not applicable.

Aggravation of Pre-existing Conditions: Not applicable.

4. First Aid Measures

Inhalation: Not applicable.

Ingestion: Not applicable.

Skin Contact: Not applicable.

Eye Contact: Not applicable.

5. Fire Fighting Measures

Fire: Not applicable.

Explosion: Not applicable.

Fire Extinguishing Media: Use extinguishing media appropriate for surrounding fire.

Special Information: In the event of a fire, wear full protective clothing and NIOSH-approved self-contained breathing

apparatus with full face piece operated in the pressure demand or other positive pressure mode.

58 | P a g e 58

6. Accidental Release Measures

Non-hazardous material. Clean up of spills requires no special equipment or procedures.

7. Handling and Storage

Keep container tightly closed. Suitable for any general chemical storage area. Protect from

freezing. Water is considered a non-regulated product, but may react vigorously with some

specific materials. Avoid contact with all materials until investigation shows substance is

compatible.

8. Exposure Controls/Personal Protection

Airborne Exposure Limits: Not applicable.

Ventilation System: Not applicable.

Personal Respirators (NIOSH Approved): Not applicable.

Skin Protection: None required.

Eye Protection: None required.

9. Physical and Chemical Properties

Appearance: Clear, colorless liquid.

Odor: Odorless.

Solubility: Complete (100%)

Specific Gravity: 1.00

pH: 7.0

% Volatiles by volume @ 21C (70F): 100

59 | P a g e 59

Boiling Point: 100C (212F)

Melting Point: 0C (32F)

Vapor Density (Air=1): Not applicable.

Vapor Pressure (mm Hg): 17.5 @ 20C (68F)

Evaporation Rate (BuAc=1): No information found.

10. Stability and Reactivity

Stability: Stable under ordinary conditions of use and storage.

Hazardous Decomposition Products: Not applicable.

Hazardous Polymerization: Will not occur.

Incompatibilities: Strong reducing agents, acid chlorides, phosphorus dichloride, phosphorus pentachloride,

phosphorus oxychloride.

Conditions to Avoid: No information found.

11. Toxicological Information

For Water: LD50 Oral Rat: >90 ml/Kg. Investigated as a mutagen.

--------\Cancer Lists\-----------------------------------------------------

-

---NTP Carcinogen---

Ingredient Known Anticipated IARC

Category

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

-

Water (7732-18-5) No No None

12. Ecological Information

Environmental Fate: Not applicable.

60 | P a g e 60

Environmental Toxicity: Not applicable.

13. Disposal Considerations

Whatever cannot be saved for recovery or recycling should be flushed to sewer. If material

becomes contaminated during use, dispose of accordingly. Dispose of container and unused

contents in accordance with federal, state and local requirements.

14. Transport Information

Not regulated.

15. Regulatory Information

--------\Chemical Inventory Status - Part 1\---------------------------------

Ingredient TSCA EC Japan Australia

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

Water (7732-18-5) Yes Yes Yes Yes

--------\Chemical Inventory Status - Part 2\---------------------------------

--Canada--

Ingredient Korea DSL NDSL Phil.

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

Water (7732-18-5) Yes Yes No Yes

--------\Federal, State & International Regulations - Part 1\----------------

-SARA 302- ------SARA 313------

Ingredient RQ TPQ List Chemical Catg.

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

Water (7732-18-5) No No No No

--------\Federal, State & International Regulations - Part 2\----------------

-RCRA- -TSCA-

Ingredient CERCLA 261.33 8(d)

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

Water (7732-18-5) No No No

Chemical Weapons Convention: No TSCA 12(b): No CDTA: No

SARA 311/312: Acute: No Chronic: No Fire: No Pressure: No

Reactivity: No (Pure / Liquid)

Australian Hazchem Code: None allocated.

Poison Schedule: None allocated.

WHMIS: This MSDS has been prepared according to the hazard criteria of the Controlled Products

61 | P a g e 61

Regulations (CPR) and the MSDS contains all of the information required by the CPR.

16. Other Information

NFPA Ratings: Health: 0 Flammability: 0 Reactivity: 0

Label Hazard Warning: Not applicable.

Label Precautions: Keep in tightly closed container.

Label First Aid: Not applicable.

Product Use: Laboratory Reagent.

Revision Information: No Changes.

Disclaimer: ******************************************************************************

******************

Mallinckrodt Baker, Inc. provides the information contained herein in good faith but

makes no representation as to its comprehensiveness or accuracy. This document is

intended only as a guide to the appropriate precautionary handling of the material by a

properly trained person using this product. Individuals receiving the information must

exercise their independent judgment in determining its appropriateness for a particular

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62 | P a g e 62

Table( Ap.5): viscosity of glycerin.

Table( Ap.6): density of glycerin.

63 | P a g e 63

Table( Ap.7): thermal conductivity of glycerin.

Table (Ap.8): Properties for Water.

Temperature

- t -

Absolute

pressure

- p -

Density

- ρ -

Specific

volume

- v -

Specific Heat

- cp -

Specific

entropy

- e -

(oC) (kN/m

2) (kg/m

3) 10

-3 (m

3/kg) (kJ/Kg.K) (kJ/Kg.K)

0.01 0.6 999.8 1.00 4.210 0

4

(maximum

density)

0.9 1000.0

5 0.9 1000.0 1.00 4.204 0.075

64 | P a g e 64

10 1.2 999.8 1.00 4.193 0.150

15 1.7 999.2 1.00 4.186 0.223

20 2.3 998.3 1.00 4.183 0.296

25 3.2 997.1 1.00 4.181 0.367

30 4.3 995.7 1.00 4.179 0.438

35 5.6 994.1 1.01 4.178 0.505

40 7.7 992.3 1.01 4.179 0.581

45 9.6 990.2 1.01 4.181 0.637

50 12.5 988 1.01 4.182 0.707

55 15.7 986 1.01 4.183 0.767

60 20.0 983 1.02 4.185 0.832

65 25.0 980 1.02 4.188 0.893

70 31.3 978 1.02 4.191 0.966

75 38.6 975 1.03 4.194 1.016

Table (Ap.9) 14 BWG diameters

Tube OD (in) Thickness (in) Tube ID (in)

1/2" 0.083 0.334

3/4" 0.083 0.584

1" 0.083 0.834

1 1/4" 0.083 1.084

1 1/2" 0.083 1.334

65 | P a g e 65

Table (Ap.10) Nomenclature

Symbol unit

Q heat Transfer Rate W

m Mass Transfer kg/s

PC Specific Heat Capacity J/Kg.°C

LMT logarithmic mean temperature difference oC

1T Temperature of liquid enter the shell oC

2T Temperature of liquid exit from the Shell oC

1t Temperature enter the tube oC

2t Temperature exit from Tube oC

U Overall Heat Transfer Coefficient W/m².oC

SA Surface area of heat Transfer m²

A , B &C Regression coefficient for chemical compound -

F Correction Factor -

Nt Number of tubes -

Ac Cross sectional area m²

Pt Tube pitch m

Db Diameter of bundle of tube m

Ds Diameter of Shell m

Ken Constants depends on arrangements of tube and

number of passes

-

L B Baffle spacing m

Us Mass velocity m/s

de Equivalent Diameter m

Re Reynolds Number -

Nu Nusselt number -

Pr Prandtl Number -

µ Viscosity Pa.s

ρ Density Kg/m³

k f Thermal conductivity of fluid W/m.oC

Kw Thermal Conductivity of tube wall material W/m.oC

h o Outside fluid film coefficient W/m².oC

h i Inside fluid film coefficient W/m².oC

h od Outside dirt coefficient W/m².oC

h id Inside dirt coefficient W/m².oC

j Heat transfer factor -

ΔP Pressure Drop pa

Ws Fluid flow rate on the Shell side Kg/s

Np number of tube side passes -

66 | P a g e 66

L Length of one tube m

do Tube outside diameter m

di Tube inside diameter m

Efficiency -

67 | P a g e 67

References:

{1}: Cengel, Y. A. 2003. Heat Transfer: a practical Approach. 2nd

edition. The McGraw-Hill

companies.

{2}: http://en.wikipedia.org/wiki/Heat_exchanger. Retrieved 2012-11-15

{3}: http://www.wlv.com/products/databook/ch1_4.pdf. Retrieved 2012-11-10

{4}: http://www.aapsj.org/view.asp?art=ps040445. Retrieved 2012-11-11

{5}:http://www.eng.uwo.ca/people/aray/CBE322%20Heat%20Transfer/Shell%20and%20tube%

20heat%20exchanger%20design%20procedure.pdf. Retrieved 2012-11-11

{6}:http://www-unix.ecs.umass.edu/~rlaurenc/Courses/che333/Reference/exchanger.pdf

Retrieved 2012-11-11

{7}: Coulson & Richardson’s, Chemical Engineering, Volume 6,Fourth Edition, Chemical

Engineering Design R. K. Sinnott