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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