Material Balance

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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

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