The document describes the production of acrylonitrile via the ammoxidation of propylene. It involves three main steps:
1) The ammoxidation reaction of propylene, ammonia, and oxygen over a bismuth phosphomolybdate catalyst to produce acrylonitrile, water, and other byproducts.
2) Further processing of the reaction products using various separation techniques like distillation columns and absorbers to purify the acrylonitrile.
3) Material and energy balance calculations to determine the inputs, outputs, heat of reactions, and energy requirements of the process. A fluidized bed reactor design is also proposed for the ammoxidation reaction.
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Production of Acrylonitrile by Ammoxidation of Propylene
1. Production of Acrylonitrile by
Ammoxidation of Propylene
Aditya Kotecha(16CH022)
Ashish Pal(16CH039)
Guide :Dr. K R Jethani
All India Shri Shivaji Memorial Society’s
College of Engineering-Pune
1
2. Introduction
• It was first prepared in 1893 by the french
chemist Charles
• Chemical formula:C3H3N
• it consists of a vinyl group linked to a nitrile
• This is pungent-smelling colorless liquid
• It is monomer for the manufacturing of plastic
• It produces toxic combustion product
2
6. • Heat from exothermic main, side and secondary
reactions evolved, via fluidized bed and heat
exchanger utilize in steam generation.
• Reaction
H2C=CHCH3 +NH3+ 1.5 O2 H2C=CHCN+ 3H2O
[Catalyst = bismuth phosphomolybate]
6
31. Energy –Energy + Energy + Energy = Energy
In Out Generated Consumed Accumulated
Reactions
1)ACN
C3H6+NH3+3/2 O2 C3H3N+3H20
2)HCN
C3H6+3NH3+3O2 3HCN+6H2O
3) AcetoN
C3H6+1.5NH3+1.5O2 1.5CH3CN+3H2O
Cp=A+BT+CT2+DT3+ET4 (J/mol K)
31
33. Reactor
Component Heat Input (J/hr) Heat Output (J/hr)
Feed Stream 73202094.07 -
Output Stream - 173709556248
Heat of reaction (Exothermic
reaction)
- -101108122182
Heat added (Molten salt solution) 0 0
Total 73202094.07 73202094.07
Reactor
Reaction
temp=
723 K
33
34. Gas Cooler
Component Heat Input (J/hr) Heat Output (J/hr)
Feed Stream 173709556248 -
Output Stream - 75911307691
Heat of reaction - -
Heat removed by water 97798248557 -
Total 75911307691 75911307691
Gas
Cooler
T= 723 K T=503 K
34
35. Quench Column
Component Heat Input (J/hr) Heat Output (J/hr)
Feed Stream 76493783455 -
Output Stream - 73327924815
Heat of reaction (Exothermic
reaction)
- 99389031382
Heat added for quenching 121127763400
Heat removed by water 51589192816 -
Total 172716956200 172716956200
Quench
Column
T=503 K
T= 358 K
Top product
H2O in
H2SO4 in
Ammonium Sulphate
35
36. Absorber
Component Heat Input (J/hr) Heat Output (J/hr)
Feed Stream 99389031382 -
Output (off gases) - 7491270847
Output (bottom product) - 2974549067
Heat removed by water 0 0
Total 99389031382 99389031382
Absorber
Column
Feed
T= 385 K
Off gases
Product
T=313 K
36
37. Product Splitter
37
Component Heat Input (KJ/Day) Heat Output (KJ/Day)
Feed stream 6119900245 -
Distillate - 1188294817
Bottoms - 369955315.6
Heat load of condensor - 44318569073
Heat load of reboiler 40006930970 -
Total 4.6*1010 4.6*1010
350 K
350 K
358 K
38. HCN Column
38
38
329 K
350 K
329 K
Component Heat Input (KJ/Day) Heat Output (KJ/Day)
Feed stream 244815032.5
Distillate - 59434085.75
Bottoms - 3105588628
Heat load of condensor - 3603604975
Heat load of reboiler 6523812657 -
Total 6768627690 6768627689
39. Aceto column
39
39
39
355 K
355 K
Component Heat Input (KJ/Day) Heat Output (KJ/Day)
Feed stream 369955315.6
Distillate - 288087119.3
Bottoms - 76252620.67
Heat load of condensor - 4100160981
Heat load of reboiler 4094545406 -
Total 4464500722 4464500722
350 K
40. ACN Column
40
Heavy Ends
Feed
ACN
Component Heat Input (KJ/Day) Heat Output (KJ/Day)
Feed stream 3105588628
Distillate - 3034235835
Bottoms - 71352793.09
Heat load of condensor - 39776260460
Heat load of reboiler 39778114321 -
Total 4.28*10^10 4.28*10^10
41. Reactor Design
• A fluidized bed reactor is a type
of reactor device that can be
used to carry out a variety of
multiphase chemical reactions.
In this type of reactor, a fluid is
passed through a solid granular
material at high enough
velocities to suspend the solid
and cause it to behave as
though it were a fluid.
41
42. Procedure
Catalyst bed data:
Catalyst: C-49 (Ferobysmuth-molybdate)
Density: 1500 kg/m3
Avg diameter of catalyst: 50um
Shape factor: 0.7
Average density: PM/RT=0.86kg/m3
G=233682.534 kg/hr=64.91 kg/sec
Weight of catalyst(using WHSV):324.55 Kg
42
43. Procedure
• Assuming L/D=3
• Crossectional area= π/4D2
• Surface area of reactor= πDL=3 πD2
• Using Leva’s Equation:
Gmf: 0.150 Kg/m2s
Gmf(actual)= 15*Gmf=2.25 Kg/m2s
G(actual)=mass flow rate/C.S.A of reactor
• C.S.A of reactor= 28.8 m2
43
45. Mechanical Design
• Thickness of reactor
J=0.85
t= pDo/(2fJ+p)
= 2.82 mm
Taking corrosion allowance = 3 mm
Taking standard value = t= 6 mm
• Tower Height for various external and internal loads
Height of reactor= 20.17 m
MOC : Carbon Steel
Specific Gravity = 7.7
1)Axial stress Due to Pressure
Fap=413.41 Kgf/cm2
45
46. 2) Stress Due to Dead loads
a) Compressive stress due to weight of shell up
to distance ‘x’
fds= ρs(x)=7.7*10-3(x) kgf/cm2
b) Compressive stress due to weight of
insulation upto distance ‘x’
fdins= (tinsρinsx)/(ts-c)
=0.0564(x) kgf/cm2
46
47. C) Compressive stress due to attachments
Weight of standard dished head
=π/4(D-1.2)2*t*ρs
= 1928.45 kg
Fdatt=324.55+1928.45/(D(ts-c)= 3.52 Kgf/cm2
Total compressive stresses,
Fds=fds+fdins+fdatt=0.0641(x)+3.52
47
48. Conclusion
• We have Studied literatue survey for the given
process
• We have selected SOHIO process based on
various parameters.
• We have tested thermodynamic feasibility for
the given process which is spontaneous.
• We have done mass balance and energy
balance for the Sohio process.
48