Material Balance
MATERIAL BALANANCE Preliminary Calculations: Basis: = = = = 100 metric tons /day of 99.5% pure Maleic Anhydride Oxidati
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MATERIAL BALANANCE Preliminary Calculations: Basis: = = = =
100 metric tons /day of 99.5% pure Maleic Anhydride Oxidation yield is 92 %wt based on benzene fed Selectivity of Maleic Anhydride is73 %wt Recovery and purification yield is 98 %wt
### Kg of MAN per hour
overall losses = 2% (assuming 1% loss in sucrubber and 1% in distillation co MAN to be produced 4228.75 Kg of MAN per hour Conversion in the reactor is 73 %wt Consider the main reaction C6H6 + 4.5 O2
C4H2O3 + 2CO2 +2H2
benzene produced
###
kg/hr
benzene actuallay required
###
kg/hr
For given process Benzene : Air 1 Air required for oxidation
Oxygen in Air Nitrogen in Air
24
### ###
kgmol/hr kg/hr
803.31
kg/hr
###
kg/hr
Assuming 65% air humidity at 30C From humidity chart 17.5 gm moisture / kg dry air Moisture in Air
1938
kg moisture / kg dry a
Stream 4 and 6 has Composition: compond
kg
%wt
NITROGEN
###
75.38
OXYGEN
###
22.89
WATER
1938
1.73
###
100
Mixer MIX-100
stream (3)
stream (6)
###
stream (7)
###
###
stream (7) has composition:
kg NITROGEN OXYGEN BENZENE WATER
Reactor PFR-100
### ### 4614.28 1938
%wt 72.41 21.99 3.95 1.66
###
100
In Reactor operating conditions are:
Temperature 350 – 400 oC Pressure 202.65kpa Oxidation yield 92 %wt MAN selectivity 73 %wt Of Benzene feed 73% is converted to MAN, 1.6% to Quinone and 17.4% is converted and CO (About 10% to CO2 and remaining to CO) while 8% Benzene feed leaves alon product stream as unconverted Benzene.
Chemical Reactions:
C6H6 + 4.5 O2 C6H6 + 7.5O2
C4H2O3 + 2CO2 +2H2 (Maleic Anhydride) 6CO2 +3H2O
C6H6 + 4.5 O2
6C0 + 3H2O
C6H6 + 1.5 O2
C6H4O2 + H2O (quinon)
Consider Reaction (R1) Benzene converted to MAN
### 43.12
MAN produced
43.12
oxygen required
194.06
CO2 produced
86.25
water produced
86.25
Consider Reaction (R2) benzene converted to CO2
461.43 5.91
oxygen required
44.31
CO2 produced
35.44
Water produced
17.72
Consider Reaction (R3) Benzene converted to CO
341.46 4.37
oxygen required
19.67
CO produced
26.23
Water produced
13.11
Consider Reaction (R4) Benzene converted to Quinon
73.83 0.95
Oxygen required
1.42
Quinone produced
0.95
Water produced
0.95
Total Oxygen consumed
259.45
Unreacted Oxygen
543.86
Total Water produced
118.03
Water in product stream
225.34
CO2 in product stream
121.69
Composition of stream (8) kg
%wt
Nitrogen
###
72.41
Oxygen
###
14.89
4056.1
3.47
Water
CO2
5354.48
4.58
MAN
4228.75
3.62
CO
734.41
0.63
Benzene
369.14
0.32
Quinone
102.17
0.09
###
100
Crude MAN separator:
Operating conditions:
Operating Pressure = 152kpa Operating temperature = 76.5oC Of stream (9) 41.17 %wt crude MAN is separated as stream (10) and rema Stream (10) contains: Maleic Anhydride
###
Water condensed
30.22
Quinone condensed
24.87
Composition of stream (10) kg MAN
%wt
1740.98
96.93
water
30.22
1.68
quinon
24.87
1.38
1796.07
100
Composition of stream (11) kg
%wt
Nitrogen
###
73.54
Oxygen
###
15.12
Water
4025.88
3.5
CO2
5354.48
4.65
MAN
2487.77
2.16
CO
734.41
0.64
Benzene
369.14
0.32
Quinone
77.3
0.07
Total
###
100
Scrubber T-100
Absorption is done in 40 %wt solution of Maleic Acid (MAC). Let 1% of the MAN produ is lost in vent stream. All the Benzene and 1% MAN leaves from the top with vent str while Quinone leaves with scrubbed liquid. MAN lost
42.29
kg/hr
MAN converted to MAC
### 24.94
kg/hr kgmol/hr
Operating Conditions: Operating Temperature: 50C Operating pressure: 152Kpa Assuming Liquid to vapor ratio in tower as 1.2 Stream (12)
G
###
kg/hr
Stream (15) will be L
###
kg of 40 % MAC soluti
Reaction taking place: C4H2O2 + H20
C4H4O4 (maleic acid)
As absorption is done in 40% solution of MAC stream (15) have composition: kg MAC water Total
%wt
55247.34 82871.01 ###
kgmole 40 60
475.98 4603.94 5079.93
MAC produced
24.94
kgmol/hr
Water consumed
24.94
kgmol/hr
500.92
kgmol/hr
4802.67
kgmol/hr
MAC leaving in stream (13) Water left in column
Total moles in vent stream excluding water: kg Nitrogen
kgmol ###
3023.07
Oxygen CO2 CO Benzene MAN Total
### ### 734.41 369.14 42.29 ###
543.86 121.69 26.23 4.73 0.43 3720.01
Assuming gases leaving in vent stream (14) saturated with water vapors Partial pressure of water vapors at 50 As at saturation condition partial pressure is equal to vapor pressure and pre same as molar ratio yH2O =
PH2O/P 0.08
And for rest of gases excluding water (O2, N2, CO, Benzene, 1% MA y rest Total moles in vent stream (14)
4056.72
Water in vent stream (14)
336.71
Water in scrubbed liquid (13)
4465.96
Composition of vent stream (14) kg Nitrogen Oxygen Water CO2 CO Benzene MAN Total
%wt
### ### 6060.74 5354.48 734.41 369.14 42.29 ###
73.86 15.18 5.29 4.67 0.64 0.32 0.04 100
Composition of scrubbed liquid stream (13): kg MAC water Quinon Total
%wt ### ### 77.3 ###
41.95 58 0.06 100
Mixer MIX-101
As stream (15) and (17) contains 40% solution of MAC. While (16) contains p ensure the composition of stream (15) and (17) at 40%wt of MAC.
MAC in stream (13)
###
40% solution will have the mass
###
So water added from stream (16)
6748.4
Stream (17)
7236.6
Water in stream (17)
###
MAC in stream (17)
###
Composition of stream (17)
MAC water Quinon Total
Dehydrator T-101:
kg 2894.63 4264.64 77.3 7236.58
%wt 40 58.93 1.07 100
In dehydrator Maleic Acid is converted back to Maleic Anhydride according to reaction: C4H4O4
C4H2O3 +
In addition to above reaction, some Maleic Acid may irreversibly convert to F according to the following reaction: C4H2O3 + H2O
C4H4O4 (maleic acid)
Assuming 0.5% MAC converts irreversibly to Fumeric Acid and rest 99.5% co Maleic Anhydride. And 95% of water is removed by azeotropic distillation fro dehydrator. Operating conditions: Top plate temperature = 110 C Bottom plate temperature = 148 C Reboiler temperature = 174 C Operating pressure = 15.2 kpa Azeotropic composition: Water = 77.5 %mole & O- xylene = MAC coming from stream (18)
###
0.5% converted to Fumaric Acid Fumaric Acid produced
14.47
MAC converted to MAN MAN produced
### 24.81 24.81
Water produced
24.81
Total water in Dehydrator O-xylene
261.74 75.99
As 95 % water is removed from the dehydrator so
Stream (19) contains Water O-xylene Composition of stream (19) kg water O-xylene Total
248.65 72.19
%wt
4475.73 7664.33 ###
36.87 63.13 100
Assuming stream (22) contains pure water and pure O-xylene stream (21) is to dehydrator. O-xylene in stream (26) 3.8 make up O-xylene required (23) Water in stream (22)
3.8 248.65
Composition of stream (26) kg water MAN Fumeric acid O-xylene quinone Total
235.56 2434.5 14.47 403.39 77.3 3165.23
%wt 7.44 76.91 0.46 12.74 2.44 100
Mixer MIX-102
Mixer MIX-102 mixes crude MAN from stream (10) with crude MAN obtained from Bot of dehydrating column stream (27) stream(27) + stream(10) ### 1796.07
= stream (28) ###
Composition of stream (28) kg water MAN Fumeric acid O-xylene quinone Totsal
265.78 4175.48 14.47 403.39 102.17 4961.29
%wt
kgmole
5.36 84.16 0.29 8.13 2.06 100
14.77 42.58 0.12 3.8 0.95 62.22
Distillation column T-102
Bottom product stream (36) contains 99.5 % pure MAN. 0.5% impurity will b Fumeric Acid (BP = 290oC) produced in Dehydrating column and remaing is Operating conditions
Top plate temperature = 120 C Bottom temperature = 145 C Operating pressure = 100Kpa MAN converted to Fumaric Acid 13.37 0 kg of MAN/hr 0.32 % of initial MAN produ MAN lost in distillation column 29.23 MAN in bottom product stream (36)
###
Bottom product of distillation column
###
Quinon in Bottom product
6.36
Composition of bottom product stream (36) kg MAN Fumeric acid quinone Total
4146.25 14.47 6.36 4167.08
%wt 99.5 0.35 0.15 100
Composition of overhead product stream (32) kg water MAN O-xylene quinone Total
265.78 29.23 403.39 95.81 794.21
%wt 33.47 3.68 50.79 12.06 100
aleic Anhydride enzene fed
nd 1% in distillation column + production of Fumeric acid)
C4H2O3 + 2CO2 +2H2O
ture / kg dry air
kg moisture / kg dry air
COMPOND
MOLECULAR WEIGHT
maleic anhydride benzene quinon maleic acid AIR water oxygen nitrogen carbon dioxide carbon monoxide O-xylene
98.06 78.11 108.10 116.07 28.95 18.06 32.00 28.01 44.00 28.00 106.17
kgmole
%mole
3021.99
76.84
803.31
20.43
107.67
2.74
3932.98
100
stream (7)
kgmole ### 803.31 59.07 107.31
%mole 75.71 20.12 1.48 2.69
###
100
0 – 400 oC
d 17.4% is converted to CO2 zene feed leaves along with
C4H2O3 + 2CO2 +2H2O (R1) Anhydride) 6CO2 +3H2O (R2)
6C0 + 3H2O
(R3)
C6H4O2 + H2O
(R4)
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr
kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kgmole
%mole
###
75.79
543.86
13.64
224.59
5.63
121.69
3.05
43.12
1.08
26.23
0.66
4.73
0.12
0.95
0.02
###
100
ssure = 152kpa perature = 76.5oC stream (10) and remaining MAN is sent along with gases in stream (11)
kg/hr kg/hr kg/hr
kgmole
%mole
17.75
90.29
1.68
8.54
0.23
1.17
19.66
100
kgmole
%mole
###
76.15
543.86
13.71
223.66
5.64
121.69
3.07
25.37
0.64
26.23
0.66
4.73
0.12
0.72
0.02
###
100
1% of the MAN produced m the top with vent stream
mperature: 50C ssure: 152Kpa
kg of 40 % MAC solution/hr
(maleic acid) composition: %mole 9.37 90.63
with water vapors of water vapors at 50 oC and 152 Kpa = 12.55 Kpa apor pressure and pressure ratio is
PH2O/P
CO, Benzene, 1% MAN CO2) y rest = 0.917 kgmol/hr
kgmole ### 543.86 336.71 121.69 26.23 4.73 0.43 ###
kgmole 500.92 ### 0.72 ###
%mole 74.52 13.41 8.3 3 0.65 0.12 0.01 100
%mole 10.08 89.9 0.01 100
While (16) contains pure water to %wt of MAC.
kg/hr kg/hr kg/hr kg/hr kg/hr kg/hr
kgmole 24.94 236.92 0.72 262.58
%mole 9.5 90.23 0.27 100
Anhydride according to the following
H20
reversibly convert to Fumaric Acid
C4H4O4 (fumeric acid)
cid and rest 99.5% converts back to eotropic distillation from the
perature = 110 C temperature = 148 C erature = 174 C ssure = 15.2 kpa
%mole & O- xylene = 22.5 %mole kg/hr
kg/hr kg/hr kgmol/hr kgmol/hr kgmol/hr
446.65
kgmol/hr
236.92
kgmol/hr
kgmol/hr kgmol/hr
kgmole 248.65 72.19 320.84
%mole 77.5 22.5 100
-xylene stream (21) is recycled back
kgmole 13.09 24.81 0.12 3.8 0.72 42.54
MAN obtained from Bottom
%mole 30.76 58.33 0.29 8.93 1.68 100
%mole 23.73 68.44 0.2 6.11 1.52 100
N. 0.5% impurity will be all the olumn and remaing is Quinon (BP = 180C)
kg of MAN/hr % of initial MAN produced
kg/hr
kg/hr
kgmole 42.28 0.12 5.21 47.62
kgmole 14.77 0.3 3.8 0.89 19.75
%mole 88.8 0.26 10.94 100
%mole 74.76 1.51 19.24 4.49 100
MOLECULAR WEIGHT
MATERIAL BALANANCE Preliminary Calculations: Basis: = = = =
100 metric tons /day of 99.5% pure Maleic Anhydride Oxidation yield is 92 %wt based on benzene fed Selectivity of Maleic Anhydride is73 %wt Recovery and purification yield is 98 %wt
2487.5 Kg of MAN per hour
overall losses = 2% (assuming 1% loss in sucrubber and 1% in distillation co MAN to be produced 2537.25 Kg of MAN per hour Conversion in the reactor is 73 %wt Consider the main reaction C6H6 + 4.5 O2
C4H2O3 + 2CO2 +2H2
benzene produced
###
kg/hr
benzene actuallay required
###
kg/hr
For given process Benzene : Air 1 Air required for oxidation
24
### ###
kgmol/hr kg/hr
Oxygen in Air
481.99
kg/hr
Nitrogen in Air
1813.2
kg/hr
Assuming 65% air humidity at 30C From humidity chart 17.5 gm moisture / kg dry air Moisture in Air
1162.8
kg moisture / kg dry a
Stream 4 and 6 has Composition: compond
kg
%wt
NITROGEN
###
75.38
OXYGEN
###
22.89
1162.8
1.73
###
100
WATER
Mixer MIX-100
stream (3)
stream (6)
###
stream (7)
###
###
stream (7) has composition:
kg NITROGEN OXYGEN BENZENE WATER
Reactor PFR-100
### ### 2768.57 1162.8
%wt 72.41 21.99 3.95 1.66
###
100
In Reactor operating conditions are:
Temperature 350 – 400 oC Pressure 202.65kpa Oxidation yield 92 %wt MAN selectivity 73 %wt Of Benzene feed 73% is converted to MAN, 1.6% to Quinone and 17.4% is converted and CO (About 10% to CO2 and remaining to CO) while 8% Benzene feed leaves alon product stream as unconverted Benzene.
Chemical Reactions:
C6H6 + 4.5 O2 C6H6 + 7.5O2
C4H2O3 + 2CO2 +2H2 (Maleic Anhydride) 6CO2 +3H2O
C6H6 + 4.5 O2
6C0 + 3H2O
C6H6 + 1.5 O2
C6H4O2 + H2O (quinon)
Consider Reaction (R1) Benzene converted to MAN
### 25.87
MAN produced
25.87
oxygen required
116.44
CO2 produced
51.75
water produced
51.75
Consider Reaction (R2) benzene converted to CO2
276.86 3.54
oxygen required
26.58
CO2 produced
21.27
Water produced
10.63
Consider Reaction (R3) Benzene converted to CO
oxygen required
204.87 2.62 11.8
CO produced
15.74
Water produced
7.87
Consider Reaction (R4) Benzene converted to Quinon
44.3 0.57
Oxygen required
0.85
Quinone produced
0.57
Water produced
0.57
Total Oxygen consumed
155.67
Unreacted Oxygen
326.32
Total Water produced
70.82
Water in product stream
135.2
CO2 in product stream
73.02
Composition of stream (8) kg
%wt
Nitrogen
###
72.41
Oxygen
###
14.89
2433.66
3.47
Water
CO2
3212.69
4.58
MAN
2537.25
3.62
CO
440.65
0.63
Benzene
221.49
0.32
Quinone
61.3
0.09
###
100
Crude MAN separator:
Operating conditions:
Operating Pressure = 152kpa Operating temperature = 76.5oC Of stream (9) 41.17 %wt crude MAN is separated as stream (10) and rema Stream (10) contains: Maleic Anhydride
###
Water condensed
30.22
Quinone condensed
24.87
Composition of stream (10) kg MAN
%wt
1044.59
94.99
water
30.22
2.75
quinon
24.87
2.26
1099.68
100
Composition of stream (11) kg
%wt
Nitrogen
###
73.57
Oxygen
###
15.13
Water
2403.44
3.48
CO2
3212.69
4.65
MAN
1492.66
2.16
CO
440.65
0.64
Benzene
221.49
0.32
Quinone
36.43
0.05
###
100
Total
Scrubber T-100
Absorption is done in 40 %wt solution of Maleic Acid (MAC). Let 1% of the MAN produ is lost in vent stream. All the Benzene and 1% MAN leaves from the top with vent str while Quinone leaves with scrubbed liquid. MAN lost
25.37
kg/hr
MAN converted to MAC
### 14.96
kg/hr kgmol/hr
Operating Conditions: Operating Temperature: 50C Operating pressure: 152Kpa Assuming Liquid to vapor ratio in tower as 1.2 Stream (12)
G
###
kg/hr
Stream (15) will be L
###
kg of 40 % MAC soluti
Reaction taking place: C4H2O2 + H20
C4H4O4 (maleic acid)
As absorption is done in 40% solution of MAC stream (15) have composition: kg MAC water Total
%wt
32861.68 49292.52 82154.2
kgmole 40 60
283.12 2738.47 3021.59
MAC produced
14.96
kgmol/hr
Water consumed
14.96
kgmol/hr
298.08
kgmol/hr
2857.03
kgmol/hr
MAC leaving in stream (13) Water left in column
Total moles in vent stream excluding water: kg Nitrogen
kgmol ###
1813.84
Oxygen CO2 CO Benzene MAN Total
### ### 440.65 221.49 25.37 ###
326.32 73.02 15.74 2.84 0.26 2232.01
Assuming gases leaving in vent stream (14) saturated with water vapors Partial pressure of water vapors at 50 As at saturation condition partial pressure is equal to vapor pressure and pre same as molar ratio yH2O =
PH2O/P 0.08
And for rest of gases excluding water (O2, N2, CO, Benzene, 1% MA y rest Total moles in vent stream (14)
2434.03
Water in vent stream (14)
202.02
Water in scrubbed liquid (13)
2655.01
Composition of vent stream (14) kg Nitrogen Oxygen Water CO2 CO Benzene MAN Total
%wt
### ### 3636.45 3212.69 440.65 221.49 25.37 ###
73.86 15.18 5.29 4.67 0.64 0.32 0.04 100
Composition of scrubbed liquid stream (13): kg MAC water Quinon Total
%wt ### ### 36.43 ###
41.98 57.98 0.04 100
Mixer MIX-101
As stream (15) and (17) contains 40% solution of MAC. While (16) contains p ensure the composition of stream (15) and (17) at 40%wt of MAC.
MAC in stream (13)
###
40% solution will have the mass
###
So water added from stream (16)
###
Stream (17)
4341.9
Water in stream (17)
###
MAC in stream (17)
###
Composition of stream (17)
MAC water Quinon Total
Dehydrator T-101:
kg 1736.78 2568.73 36.43 4341.95
%wt 40 59.16 0.84 100
In dehydrator Maleic Acid is converted back to Maleic Anhydride according to reaction: C4H4O4
C4H2O3 +
In addition to above reaction, some Maleic Acid may irreversibly convert to F according to the following reaction: C4H2O3 + H2O
C4H4O4 (maleic acid)
Assuming 0.5% MAC converts irreversibly to Fumeric Acid and rest 99.5% co Maleic Anhydride. And 95% of water is removed by azeotropic distillation fro dehydrator. Operating conditions: Top plate temperature = 110 C Bottom plate temperature = 148 C Reboiler temperature = 174 C Operating pressure = 15.2 kpa Azeotropic composition: Water = 77.5 %mole & O- xylene = MAC coming from stream (18)
###
0.5% converted to Fumaric Acid Fumaric Acid produced
8.68
MAC converted to MAN
1728.1 14.89 14.89
MAN produced Water produced
14.89
Total water in Dehydrator
157.6
O-xylene
45.75
As 95 % water is removed from the dehydrator so
Stream (19) contains Water O-xylene Composition of stream (19) kg water O-xylene Total
149.72 43.47
%wt
2694.89 4614.78 7309.67
36.87 63.13 100
Assuming stream (22) contains pure water and pure O-xylene stream (21) is to dehydrator. O-xylene in stream (26) 2.29 make up O-xylene required (23) Water in stream (22)
2.29 149.72
Composition of stream (26) kg water MAN Fumeric acid O-xylene quinone Total
141.84 1460.7 8.68 242.88 36.43 1890.54
%wt 7.5 77.26 0.46 12.85 1.93 100
Mixer MIX-102
Mixer MIX-102 mixes crude MAN from stream (10) with crude MAN obtained from Bot of dehydrating column stream (27) stream(27) + stream(10) ### 1099.68
= stream (28) ###
Composition of stream (28) kg water MAN Fumeric acid O-xylene quinone Totsal
172.06 2505.29 8.68 242.88 61.3 2990.21
%wt
kgmole
5.75 83.78 0.29 8.12 2.05 100
9.56 25.55 0.07 2.29 0.57 38.04
Distillation column T-102
Bottom product stream (36) contains 99.5 % pure MAN. 0.5% impurity will b Fumeric Acid (BP = 290oC) produced in Dehydrating column and remaing is Operating conditions
Top plate temperature = 120 C Bottom temperature = 145 C Operating pressure = 100Kpa MAN converted to Fumaric Acid 8.02 0 kg of MAN/hr 0.32 % of initial MAN produ MAN lost in distillation column 17.54 MAN in bottom product stream (36)
###
Bottom product of distillation column
###
Quinon in Bottom product
3.82
Composition of bottom product stream (36) kg MAN Fumeric acid quinone Total
2487.75 8.68 3.82 2500.25
%wt 99.5 0.35 0.15 100
Composition of overhead product stream (32) kg water MAN O-xylene quinone Total
172.06 17.54 242.88 57.49 489.96
%wt 35.12 3.58 49.57 11.73 100
aleic Anhydride enzene fed
nd 1% in distillation column + production of Fumeric acid)
C4H2O3 + 2CO2 +2H2O
ture / kg dry air
kg moisture / kg dry air
COMPOND
MOLECULAR WEIGHT
maleic anhydride benzene quinon maleic acid AIR water oxygen nitrogen carbon dioxide carbon monoxide O-xylene
98.06 78.11 108.10 116.07 28.95 18.06 32.00 28.01 44.00 28.00 106.17
kgmole
%mole
1813.20
76.84
481.99
20.43
64.60
2.74
2359.79
100
stream (7)
kgmole 1813.2 481.99 35.44 64.39
%mole 75.71 20.12 1.48 2.69
###
100
0 – 400 oC
d 17.4% is converted to CO2 zene feed leaves along with
C4H2O3 + 2CO2 +2H2O (R1) Anhydride) 6CO2 +3H2O (R2)
6C0 + 3H2O
(R3)
C6H4O2 + H2O
(R4)
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr
kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kg/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr kgmol/hr
kgmole
%mole
1813.2
75.79
326.32
13.64
134.75
5.63
73.02
3.05
25.87
1.08
15.74
0.66
2.84
0.12
0.57
0.02
2392.3
100
ssure = 152kpa perature = 76.5oC stream (10) and remaining MAN is sent along with gases in stream (11)
kg/hr kg/hr kg/hr
kgmole
%mole
10.65
84.8
1.68
13.37
0.23
1.83
12.56
100
kgmole
%mole
1813.2
76.18
326.32
13.71
133.52
5.61
73.02
3.07
15.22
0.64
15.74
0.66
2.84
0.12
0.34
0.01
###
100
1% of the MAN produced m the top with vent stream
mperature: 50C ssure: 152Kpa
kg of 40 % MAC solution/hr
(maleic acid) composition: %mole 9.37 90.63
with water vapors of water vapors at 50 oC and 152 Kpa = 12.55 Kpa apor pressure and pressure ratio is
PH2O/P
CO, Benzene, 1% MAN CO2) y rest = 0.917 kgmol/hr
kgmole ### 326.32 202.02 73.02 15.74 2.84 0.26 ###
kgmole 298.08 ### 0.34 ###
%mole 74.52 13.41 8.3 3 0.65 0.12 0.01 100
%mole 10.09 89.9 0.01 100
While (16) contains pure water to %wt of MAC.
kg/hr kg/hr kg/hr kg/hr kg/hr kg/hr
kgmole 14.96 142.71 0.34 158.01
%mole 9.47 90.32 0.21 100
Anhydride according to the following
H20
reversibly convert to Fumaric Acid
C4H4O4 (fumeric acid)
cid and rest 99.5% converts back to eotropic distillation from the
perature = 110 C temperature = 148 C erature = 174 C ssure = 15.2 kpa
%mole & O- xylene = 22.5 %mole kg/hr
kg/hr kg/hr kgmol/hr kgmol/hr kgmol/hr
267.99
kgmol/hr
142.71
kgmol/hr
kgmol/hr kgmol/hr
kgmole 149.72 43.47 193.18
%mole 77.5 22.5 100
-xylene stream (21) is recycled back
kgmole 7.88 14.89 0.07 2.29 0.34 25.47
MAN obtained from Bottom
%mole 30.94 58.46 0.29 8.98 1.32 100
%mole 25.13 67.17 0.2 6.01 1.49 100
N. 0.5% impurity will be all the olumn and remaing is Quinon (BP = 180C)
kg of MAN/hr % of initial MAN produced
kg/hr
kg/hr
kgmole 25.37 0.07 5.21 30.65
kgmole 9.56 0.18 2.29 0.53 12.56
%mole 82.77 0.24 16.99 100
%mole 76.12 1.42 18.22 4.24 100
MOLECULAR WEIGHT