Equipment Design

Equipment Design

Content:2 Heat Exchanger ( 1 & 2 )Cooler (E-100)Compressor (K-102)Trans-alkylation reaction

Shell and tube heat exchangerObjective : to cooled the stream out from reactor by exchange heat with benzene comes from benzene column.

Assumptions:Use shell and tube heat exchanger, one shell and two tube passes.

The value of the overall heat transfer coefficient was assumed to be 535 w/m2.s.

Assume the outer, the inner diameter and the length of the tube.

Main design procedure:

1-Heat load ,(kW)

Q = (m Cp ΔT)hot =(m Cp ΔT)cold

2- Tube side flow , (kg/hr)

cold

hotcold TCp

Qm

lmtm

lm

TFT

tT

ttS

tt

TTR

tTtT

tTtTT

11

12

12

21

12

21

1221

;

ln

3-Log mean Temperature, (˚C)

4-Provisional Area, (m2)

mo TU

QA

Number of tube:

Bundle and Shell Diameter

DensityPassArea

FlowRateuvelocity

areatoncrossPasstubespassArea

dareaSectioncross

sesAssumedPas

tubesPassTubes

ubeareaOfOneT

totalAreatubes

LdubeAreaOfOneT

t

i

o

*/

sec//

25.0

#/

#

2

10.12.Re

.,; 11

1

1

1

FigadingDD

PassesNofnKK

NdD

bs

nt

ob

Tube side Heat Transfer Coefficient

Shell side heat Transfer Coefficient

i

fi

ih

wh

pit

d

kNuh

d

LfjjNu

k

cdu

)(;PrRe

Pr;Re

14.033.0

e

fs

hw

h

pes

oto

e

ss

t

Bsots

d

kNuh

cutbufflefjjNu

k

cdu

dpd

d

A

FlowRateu

p

lDdpA

_Re,;PrRe

Pr;Re

917.01.1

14.033.0

22

Overall Coefficient

Tube Side pressure drop

Shell side Pressure Drop

ii

o

w

i

oo

oo hd

d

k

ddd

hU

1

2

ln11

25.28

2t

m

wifpt

u

d

LjNP

28

214.0

s

wBe

sfs

u

l

L

d

DjP

Thickness

cj

j

j

CPSE

t

Dr

6.0

Pr2

Equipment NameShell & tube heat exchanger

Objective to cooled the stream out from reactor by exchange heat with benzene comes from benzene column

Equipment Number E-105

Material of Construction

Carbon steel

Insulation Glass wool

Cost)$( 111672

Operating Condition

Shell Side

Inlet temperature (oC) 193Outlet temperature (oC) 265

Tube Side

Inlet temperature (oC)444Outlet temperature (oC)

361

Number of Tubes 838.754Shell Diameter (m) 1.264

Tube bundle Diameter (m) 1.189 LMTD (oC) 173.44

Q total (kw) 3.51e4 Heat Exchanger Area (m2)

385.76

U (W/m2. oC) 537.6

Assumptions:For second heat exchanger:Use shell and tube heat exchanger, one shell and two tube passes.



ResultsEquipment NameShell & tube heat exchanger

Objective to cooled the stream out from reactor by exchange heat with benzene comes from benzene column



Carbon steel


Cost)$( 58752

Operating ConditionShell Side

Inlet temperature (oC) 193Outlet temperature (oC) 260

Tube Side

Inlet temperature (oC)361Outlet temperature (oC)271

Number of Tubes 284.36Shell Diameter (m) .788

Tube bundle Diameter (m) .728 LMTD (oC) 89.005

Q total (kw) 6.29e3 Heat Exchanger Area (m2)

98.090

U (W/m2. oC) 801.54

Assumptions:For cooler:

Use shell and tube heat exchanger, one shell and two tube passes.



ResultsEquipment NameShell & tube heat exchanger

Objective to cooled the stream out from first bed reactor by using cold water



Carbon steel


Cost)$( 69000

Operating ConditionShell Side

Inlet temperature (oC) 701.88Outlet temperature (oC) 200

Tube Side

Inlet temperature (oC)25Outlet temperature (oC)80

Number of Tubes 211.48Shell Diameter (m) .788

Tube bundle Diameter (m) 1.135LMTD (oC) 352.4

Q total (kw) 15310Heat Exchanger Area (m2)

202.64

U (W/m2. oC) 222.96

Compressor (K-102)

Objective:

Compressor is a device in which a gas is compressed to increase its pressure.

Compressor (K-102) is employed to increase the pressure from Pin=(179.3psia) to (Pout=530.4psia)

Design procedure:

1.Calculate n from P1/P2 = ( T1/T2)^(n/n-1)

2. Calculate work doneBtu/lb-moleW = (n*R*(T1-T2))/(1-n)

R=Cp/Cv

3. Calculate horse power,ftlbf/lbmHp=( (Z1*R*T1)/Mw)*(n/n-1)*(Rc^(n-

1/n) – 1)

P1 T1

P2T2

where Rc = P2/P1

4. Calculate the efficiency from (n/n-1) = (K/K-1)*Ep ,

WhereK = (Mw*Cp)/(Mw*Cp – 1.986)Ep=efficiency of the compressorCp=heat capacity, Btu/lboF

Results:K-102

Inlet Temp.(oR)837.6

Outlet Temp.(oR)968.1

Inlet Pressure(Psia)179.3

Outlet Pressure(Psia)530.4

Efficiency%44.85%

Power(HP)332.848

Cost ($)= 251600

Type of compressor: reciprocating

Trans-alkylation reaction

Objective:

The aim from trans-alkylation reaction is to convert PEB to EB.

PEB EB

Main design procedure:

1) Design Equation:

2) Rate Law:

-rA = K CA

Arrhenius equation

3) Stoichiometry

4) Energy Balance

5) Dimensions of the Reactor Assuming L/D = 4

6) Height of reactor= L+D+(2*space)7) Weight of cat. = vol. of reactor (1- ϵ)* ρcat

8) Area of reactor= 2*(3.14)*r*H

9) t = (P r i / (S E-0.6P) ) + CcWhere:t: shell thickness(in)P: internal pressurer i (Rs): internal radius of shell (in)E: efficiency of jointS: working stress stain SteelCc: allowance for corrosion

Results:K = 37.6675 s-1

From Polymath the volume of reactor V = 13.3 m3

Dimensions of the ReactorD = 1.61764 m L = 6.470559 m

Material of Construction: 316 carbon steelCost : 154800 $

H(reactor)=21.23 ft W= 232.0318 kgcatA = 353.309 ft^2

t= 1.38e-1 m

Thank you

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Equipment Design