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Production Of Di-Ethyl Ether By Vapor Phase Dehydration Of Ethanol Project Supervisor : Miss Sidra Jabeen Co-Adviser : Muhammad Usman

Production Of Di-Ethyl Ether By Vapor Phase Dehydration Of Ethanol Project Supervisor : Miss Sidra Jabeen Co-Adviser: Muhammad Usman

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Production Of Di-Ethyl Ether By Vapor Phase Dehydration Of Ethanol

Project Supervisor : Miss Sidra JabeenCo-Adviser : Muhammad Usman

The Team

•2010-Ch-08 Ruqia Mustafa•2010-Ch-32 Kamran Mohy-ud-Din(Group Leader)•2010-Ch-36 Ismail Zaidi•2010-Ch-76 Abbas Raza•2010-Ch-108 Irtiza Ali Butt•2010-Ch-120 Arslan Khan

Contents• Introduction to DEE• Uses Of DEE• Production Of DEE• Methods to Prepare DEE• Selection Of Process• Capacity Selection• Process Description• Material Balance• Energy Balance

Introduction to DEE

• Diethyl ether is an organic compound in the ether class with the formula C2H5—O—C2H5

Properties• It is a colorless• Highly volatile flammable liquid• It is commonly used as a solvent • Used as a general anesthetic. It has narcotic properties • It has a burning sweet taste• Its boiling point is 34.6 C at 1 atm

Uses Of DEE• As a Fuel• Laboratory uses• Medical use• Recreational use• Metabolism

Companies producing DEECompanies Country Production in Metric

Tons/Year

Henan Golden Yangtze River Industry Co. Ltd.

China 10,800

Anhui Jin’ao Chemical Co. Ltd

China 5,000

Royal Exim India 2,000

Chemical Point UG Germany 7,000

SOHEUNG Chem Co. Ltd. South Korea 7200

Contd…• Diethyl ether Imports by Countries in US Dollars

Contd..

• Consumption in Pakistan

Pakistan Yearly Imports in US Dollars - Diethyl ether

Capacity Selection

•5000 Metric Ton per year

Methods To Prepare DEEDEE is prepared from the following processes

• Vapor-phase Dehydration Of Ethanol• Acid ether synthesis • Williamson ether synthesis

Selection Of Process

Process Yield(%) Per Pass Conversion

(%)

Catalyst Purity (%)

Vapor-phase dehydration of

Ethanol

95 80 Al2O3(Alumina)

99.5

Acid Ether Synthesis

75 70 H2SO4(sulphuric acid)

95

Williamson Ether Synthesis

55 75 Na (sodium metal)

90

Process Description

Feed Drum

Reactor

Distillation Column-I

Distillation Column-II

Fresh Ethanol Feed

Ethylene Fuel Gas

Diethyl Ether Product

Waste Water

Ethanol Recycle Stream

3 Phase separator

Process Flow Diagram

Contd…

Chemical Reactions

Main Reaction (C2H5 )2O (g) 2C2H4 (g) + H2O (g)

Ethanol DEE waterSide Reaction

• (C2H5 )2O (g) C2H4 (g) + H2O (g)

DEE Ethene water

MATERIAL BALANCE

17

Basis

596 kg/hr DEE with purity 99.5 %

8.054 kgmole/hr DEE with purity 99.5 %

Overall Material Balance

ComponentMole fraction

Moles(kgmole)

Mass (kg)

Ethanol 0.7 16.401 754.44

Water 0.3 7.029 126.52

DEE 0 0

Ethene 0 0

Total flow 23.43 880.96

Component

Mole fraction

Moles (kgmole)

Mass(kg)

Ethanol 0.019948175 0.003042 0.139927

Water 0.034715944 0.005294 0.095289

DEE 0.465943968 0.071052 5.25784

Ethene 0.479391913 0.073103 2.046872Total flow 0.15249 7.539928

componentmole fraction

Moles (kgmole)

Mass(kg)

Ethanol 0.001405 0.01137 0.523043

Water 0 0 0

DEE 0.995 8.051067 595.7789

Ethene 0.003595 0.029087 0.81444

Total flow 8.091524 597.1164

ComponentMole fraction

Moles (kgmole)

Mass(kg)Ethanol 0.000667 0.010183 0.468426Water 0.999333 15.25515 274.5928DEE 0 0 0Ethene 0 0 0

Total flow 15.26534 275.0612

Cond…

Total Mass Balance:

stream 1 = stream 4 + stream 7 +stream 12

880.968 = 7.539928 + 597.1164 + 275.0612

880.968 kg = 880.968 kg

Material Balance across feed vessel

ComponentMole fraction

Moles(kgmole)

Mass(kg)

Ethanol 0.7 16.401 754.446

Water 0.3 7.029 126.522

DEE 0 0

Ethene 0 0

Total flow 23.43 880.968

ComponentMole fraction

Moles(kgmole) Mass(kg)

Ethanol 0.709456 4.050131 186.306

Water 0.2763 1.577337 28.39206

DEE 0.0142 0.081065 5.99879

Ethene 0 0 0

Total flow 220.6969

ComponentMole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.701859 20.45113 940.752

Water 0.295359 8.606337 154.9141

DEE 0.002782 0.081065 5.99879

Ethene 0 0 0

Total flow 29.13853 1101.665

Cond….Total Mass Balance:

stream 1 + stream 11 = stream 2880.968 + 220.6969 = 1101.665

1101.665 kg = 1101.665 kg

Material balance across Reactor

Component

Mole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.701859 20.45113 940.752

Water 0.295359 8.606337 154.9141

DEE 0.002782 0.081065 5.99879

Ethene 0 0 0

Total flow 29.13853 1101.665

Component Mole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.139880845 4.090226 188.1504

Water 0.575836636 16.83792 303.0825

DEE 0.280785497 8.210389 607.5688

Ethene 0.003497021 0.102256 2.863158

Total flow 29.24079 1101.665

Cond..Total Mass Balance:

stream 2 = stream 31101.665 kg = 1101.665 kg

Material Balance across 3 phase separator

ComponentMole fraction

Moles (kgmole) mass(kg)

Ethanol 0.1398808 4.090226 188.1504

Water 0.5758366 16.83792 303.0825

DEE 0.2807854 8.210389 607.5688

Ethene 0.0034970 0.102256 2.863158

Total flow 29.24079 1101.665

Component Mole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.019948175 0.003042 0.139927

Water 0.034715944 0.005294 0.095289

DEE 0.465943968 0.071052 5.25784

Ethene 0.479391913 0.073103 2.046872Total flow 0.15249 7.539928

component Mole fraction

Moles(kgmole) Mass(kg)

Ethanol 0.183305572 3.383517 155.6418

Water 0.39589992 7.307656 131.5378

DEE 0.419230067 7.738292 572.6336

Ethene 0.001564442 0.028877 0.808556

Total flow 18.45834 860.6217

Component Mole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.065984018 0.701126 32.2518

Water 0.896906995 9.530261 171.5447

DEE 0.037089211 0.394099 29.1633

Ethene 1.97761E-05 0.00021 0.005884

Total flow 10.6257 232.9657

Cond….

Total Mass Balance:

stream 3 = stream 4 + stream 5 +stream 61101.665 = 7.539928 + 860.6217 + 232.9657

1101.665 kg = 1101.665 kg

Material Balance across 1st distillation column

componentMole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.183305572 3.383517 155.6418Water 0.39589992 7.307656 131.5378DEE 0.419230067 7.738292 572.6336

Ethene 0.001564442 0.028877 0.808556Total flow 18.45834 860.6217

component Mole fractionMoles(kgmole)

Mass(kg)

Ethanol 0.06598401 0.701126 32.2518

Water 0.89690699 9.530261171.544

7

DEE 0.03708921 0.394099 29.1633

Ethene 1.97761E-05 0.000210.00588

4

Total flow 10.6257232.965

7

Component Mole fraction

Moles(kgmole) Mass(kg)

Ethanol 0.001405 0.01137 0.523043

Water 0 0 0

DEE 0.995 8.051067 595.7789

Ethene 0.003595 0.029087 0.81444

Total flow 8.091524 597.1164

ComponentMole fraction

Moles(kgmole) Mass(kg)

Ethanol 0.194035 4.073273 187.3705

Water 0.802092 16.83792 303.0825

DEE 0.003874 0.081324 6.017969

Ethene 0 0 0

Total flow 20.99251 496.471

Cond..

Total Mass Balance:

stream 5 + stream 6 = stream 7 + stream 8860.6217 + 232.9657 = 597.1164 + 496.471

1093.59 kg = 1093.59 kg

Material Balance across 2nd distillation column

ComponentMole fraction

Moles (kgmole) Mass(kg)

Ethanol 0.70944 4.063089 186.9021

Water 0.27636 1.582764 28.48976

DEE 0.0142 0.081324 6.017969

Ethene 0 0 0

Total flow 5.727177 221.4098

ComponentMole fraction

Moles(kgmole) Mass(kg)

Ethanol 0.000667 0.010183 0.468426

Water 0.999333 15.25515 274.5928

DEE 0 0 0

Ethene 0 0 0

Total flow 15.26534 275.0612

ComponentMole fraction Moles

Mass(kg)

Ethanol 0.194035 4.073273 187.3705

Water 0.802092 16.83792 303.0825

DEE 0.003874 0.081324 6.017969

Ethene 0 0 0

Total flow 20.99251 496.471

Cond..

Total Mass Balance:

stream 8 = stream 11 + stream 12496.471 = 221.4098 + 275.0612

496.471 kg = 496.471 kg

Reference conditions

•Temperature 30 C•Pressure 101.325 kPa

ENERGY BALANCE

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Energy Balance across feed vessel

Stream 1 11 2

Temperature(C) 30 88 42

Pressure(kpa) 1500 1500 1450

Enthalpy of Ethanol (kJ/hr) 0

29125.34 28752.09Enthalpy of DEE (kJ/hr) 0

887.1152 178.0244Enthalpy of water (kJ/hr) 0

6830.213 7912.582Enthalpy of Ethene (kJ/hr) 0 0 0

Total Enthalpy (kJ/hr) 036842.67 36842.7

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Cond…

Total Energy Balance:

stream 1 + stream 11 = stream 2

0 + 36842.67 = 36842.7

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36842.67 kJ/hr = 36842.7 kJ/hr

Energy balance across Reactor

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Stream 2 3

Temperature(C) 200 200

Pressure(kpa) 1450 1300

Total enthalpy1461893.8 1173604.369

Cond…Total Energy Balance:

1) Enthalpy of reaction = Hr = -190057 kJ2) Heat removed = Hrev = 474683 kJ

enthalpy of stream 2 + Hr - 474683 = enthalpy of stream 3

1461893.8 + 190057 - 474683 = 1173604.369

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1173604.369 kJ/hr = 1173604.369 kJ/hr

Energy balance across throttle valve

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Stream 3 3(a)

Temperature(C) 40 39.96

Pressure(kpa) 1250 200

Enthalpy of Ethanol (kJ/hr)4722.77

4718.61388

Enthalpy of DEE (kJ/hr) 14684.1 14652.8435

Enthalpy of water (kJ/hr) 12713.5 12759.68549

Enthalpy of Ethene (kJ/hr) 46.2371 46.4042

Total Enthalpy (kJ/hr) 32166.6 32166

Cond…

Total Energy Balance:

stream 3 = stream 3(a)

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32166.6 kJ/hr = 32166 kJ/hr

Energy balance across 3 phase seperator

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Stream 3(a) 4 5 6

Temperature(C) 39.96 40 40 40

Pressure(kpa) 200 200 200 200

Enthalpy of Ethanol (kJ/hr) 4718.6142.31388 3906.76 809.54

Enthalpy of DEE (kJ/hr) 1465.284 0.68435 13930.7 709.88

Enthalpy of water (kJ/hr) 12759.69 1.78549 5537.66 7220.3

Enthalpy of Ethene (kJ/hr) 46.4042 33.1965 13.1112 0.0965

Total Enthalpy (kJ/hr) 32166 37.9802 23388.2 8739.8

Cond…

Total Energy Balance:

stream 3(a) = stream 4 + stream 5 + stream 6

32166 = 37.9802 + 23388.2 + 8739.8

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32166 kJ/hr = 32166 kJ/hr

Energy balance across 1st distillation column

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Stream 5&6 7 8

Temperature(C) 40 45 97

Pressure(kpa) 200 165 195

Enthalpy of Ethanol (kJ/hr)4698.52 18.3698 35092.2

Enthalpy of DEE (kJ/hr) 14608.7 20139.3 1067.15Enthalpy of water (kJ/hr) 12711.9 0 85474.2

Enthalpy of Ethene (kJ/hr) 13.1616 18.5376 0

Total Enthalpy (kJ/hr) 32032.3 20356.2 121634

Cond…

Total Energy Balance:

stream 5&6 + Qr = Qc + stream 7 + stream 8

32032.3 + 463605 = 353648 + 20356.2 + 121634

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495637.3 kJ/hr = 495637.3 kJ/hr

Energy balance across 2nd distillation column

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Stream 8 11 12

Temperature(C) 97 88 116

Pressure(kpa) 195 170 175

Enthalpy of Ethanol (kJ/hr)35092.2 29700.9 116.517

Enthalpy of DEE (kJ/hr) 1067.15 904.129 0

Enthalpy of water (kJ/hr) 85466.8 1214.14 99483.8

Enthalpy of Ethene (kJ/hr) 0 0 0

Total Enthalpy (kJ/hr) 121626 31819.1 99600.3

Total Energy Balance:

stream 8 + Qr = Qc + stream 11 + stream 12

121626 + 159064 = 149271 + 31819.1 + 99600.3

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280690 kJ/hr = 280690 kJ/hr

Duties of Heat Exchangers

Exchanger Duty (kJ/hr)

E-1201(vaporizer) 1425051.103

E-1202(cooler)1126000

E-1203(condenser)353648

E-1204(reboiler)463620

E-1205(cooler) 11741

E-1206(condenser)149271

E-1207(reboiler) 160054

E-1208(cooler)88075

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