AIM:

Assuming loses 1) Reactor 0.5 % of COS carbonyl sulfide

2) Absorber 1 % of COS carbonyl sulfide

3) Stripper 1 % of CS2 carbon disulfide

Molecular weight of compounds used in the process:

1 Carbon monoxide CO 28.01 kg/kmol

2 Carbon dioxide CO2 44.01 kg/kmol

3 Sulphur Dioxide SO2 64.066 kg/kmol

4 Carbon disulfide CS2 76.139 kg/kmol

5 Carbonyl sulfide COS 60.075 kg/kmol

Unit 1: shell and tube reactor

Reaction:

Feed:

CO 373.0715779 kmol/hr

10449.7349 kg/hr

SO2 124.3571926 kmol/hr

7967.067902 kg/hr CO COS

Product: CO2

COS 118.139333 kmol/hr

7097.220429 kg/hr SO2

CO2 236.278666 kmol/hr

10398.62409 kg/hr

235.0973 kmol/hr

10346.63 kg/hr

COS output after loss 117.5486 kmol/hr

7061.734 kg/hr

To design carbon disulfide plant of 100 TPD

3CO + SO2 COS + 2CO2

CO2 output after loss

Conversion rate = 95 %

Shell and tube reactor

Second unit: Reactor cum absorber:

Reaction:

Feed: 1) CO2 235.0973 kmol/hr

10346.63 kg/hr

2) COS 117.5486 kmol/hr

7061.734 kg/hr

Note: Conv 95% factor(Mole ): 0.5

Product 1) CS2 55.8356 kmol/hr

4251.267 kg/hr

2) CO2 55.8356 kmol/hr

2457.325 kg/hr

Product after loss 1) Carbon disulfide 55.27724623 kmol/hr

4208.754251 kg/hr

Third Unit: Stripping section()

Feed: Carbon Monoxide CO 5% more then required in first reactor

391.7252 kmol/hr

10972.22 kg/hr

carbon disulfide CS2 55.27725 kmol/hr

4208.754 kg/hr

Final CS2 After Losses CS2 54.72447 kmol/hr

4166.667 kg/hr

2COS CS2 + CO2

Stripping Section(No reaction takes place here)

Considering plant operation of 24 HR 24 hr

Total production of CS2 1313.38737 kmol/day

100000.001 kg/day

100.000001 TPD

1) Temperature of reactor 200 Celsius 473.15 Kelvin

2) log Kp 22.58819

1 CO -110.53 KJ/mol

2 CO2 -393.5 KJ/mol

3 COS -141.5 KJ/mol

4 CS2 -116.9 KJ/mol

5 SO2 -296.81 KJ/mol

1 CO

2 CO2

3 COS

4 CS2

5 SO2

6 Ethylene

3)

m(CO) 373.0716 Kmol/hr Cp(CO) 0.0292 KJ/Kmol C 29.2 KJ/kmol C

m(SO2) 124.3572 Kmol/hr CP(SO2) 0.042 KJ/Kmol C 42 KJ/kmol C

temp T1 25 C 298.15 K

T2 200 C 473.15 K

Heat required m*Cp*ΔT

Heat Capacity datas at constant pressure Cp

Energy require to take CO and SO2 from 25 C to 200C

Energy Balance Across UNIT 1: Shell and tube Reactor.

Heat of formation at 25 Degree

19.10)1

(15509log T

Kp

2820421 KJ/hr

67690107 KJ/day

4) Heat of reaction for first reaction in catalytic reactor:

Reaction:

ΔHr -48.1 KJ/mol -48100 KJ/Kmol -5682501.92 KJ/hr

-5654.08941 KJ/hr -136380046 KJ/day

-135698.146 KJ/day

4.1) Heat removed to get 100C

T1 200 energy needed 1776512.541 KJ/hr

T2 100

Cp(CO2) 39.94

Cp(COS) 71.25

If we use ethylene glycol in our HE Cp(Ethylen gylcol) 150.6

flowrate 235.9246

Inlet temp 0

Outlet Temp 50

Energy 1776513

5) Reaction:

ΔHr -227.4 KJ/mol -227400 KJ/Kmol

-12570.0458 KJ/hr

-301681.099 KJ/day

5.1) Energy to heat the CO from 25 to 100

T1 25

T2 100

energy required 857878.1

Taking ethylene glycol as a cooling agent in HE flowrate 113.928 Kmol/hr

T1 0 C

3CO + SO2 COS + 2CO2

2COS CS2 + CO2

T2 50 C

857878

6)

T2 25 C Cp(CS2) 76.01

T1 100 C Cp(CO) 29.2

heat 1173000 KJ/hr

150.6 KJ/Kmol C

flowrate required to achieve cooling 155.7769

inlet temp 0

outlet temp 50

1173000

Total Energy requirement -214249 KJ/hr

Taking ethylene gycol in heat exchanger Cp(ethylene glycol)

Temperature required

Heat balance around the condensor

CS2 + CO2

Solvent back to absrober

CO (For stripping)

COS absorbed in Solvent

Stripper

CO2

Dissolved COS to stripper

COS + CO2

5% more then required in first reactor

Solvent(From Stripper)

Reactor cum absorber

CO 373.0716 kmol/hr

COS 118.1393 kmol/hr

CO2 236.2787 kmol/hr

SO2 124.3572 kmol/hr

KJ/kmol C

kmol/hr

C

C

KJ/Kmol C

KJ/Kmol C

kmol/hr

C

C

KJ/hr