DESIGN OF CRYSTALLIZER

MANUFACTURE OF ANTHRACENE FROM COAL TAR

(150 TONNES PER DAY)

A PROJECT REPORT

Submitted by

G. ALLWIN BRITTO Reg no. 105907152501

S. JENISH ROSE Reg no. 105907152303

J. MAJEEDAHMED FAZHEEL Reg no. 105907152018

S. SAMUEL Reg no. 105907152029

in partial fulfillment for the award of the degree

of

BACHELOR OF TECHNOLOGY

IN

CHEMICAL ENGINEERING

MOHAMED SATHAK ENGINEERING COLLEGE

ANNA UNIVERSITY :: CHENNAI-600 025APRIL 2014

ANNA UNIVERSITY :: CHENNAI 600 025

BONAFIDE CERTIFICATE

Certified that this project report “__DESIGN OF CRYSTALLIZER__” is the

bonafide work of “__________________________________” who carried out the

project work under my supervision.

SIGNATURE SIGNATURE

Mr. M. D. Durai Murugan

HEADOFTHEDEPARTMENT

CHEMICALENGINEERING

Mohamed Sathak Engineering college

Ramnad-623 806

Mr. Rohan Jaikumar

SUPERVISOR

ASSISTANTPROFESSOR

CHEMICALENGINEERING

Mohamed Sathak Engineering college

Ramnad-623 806

DESIGN OF CRYSTALLIZER

MANUFACTURE OF ANTHRACENE FROM COAL

TAR

(150 TONNES PER DAY)

i

ABSTRACT

Anthracene occurs in coal tar(less than 1) and is obtained from the green oil

fractions or anthracene oil fractions(B.P 270-360 °C). On cooling, it results the

composition containing an isomer of anthracene and carbazole as impurities. During

carbonization of coal, thermal cracking occurs.

The equipment design calculations for crystallizer in the Manufacture of

Anthracene from Coal tar(150 tonnes per day), in which 3.82 * 105 kg of feed at about

2.72 * 106 kcal was fed. The commercial Anthracene obtained from washing tank

contains liquid form was obtained as crystals.

4

CONTENTS

CHAPTER TITLE PAGE NO.

ABSTRACT i

01 INTRODUCTION 5

02 VARIOUS PROCESS 8

03 PROCESS DESCRIPTION 10

04 PROPERTIES

4.1 Physical properties

4.2 Chemical properties

12

12

05 MATERIAL BALANCE 14

06 ENERGY BALANCE 20

07 DESIGN CALCULATIONS

7.1 Design of Crystallizer 32

08 COST ESTIMATION 35

09 CONCLUSION 37

10 REFERENCE 38

5

CHAPTER 1

MANUFACTURE OF ANTHRACENE FROM COAL TAR

Introduction

Anthracene occurs in coal tar (less than 1) and is obtained from the green oil

fraction or anthracene oil fraction (boiling point ranged between 270-360°C) on

cooling this, anthracene contains phenanthrene, an isomer of anthracene and

carbazole as impurities. The chemical name of Anthracene is Paranapthalene and its

molecular formula is C14H10.

Anthracene is used in the manufacture of dyes, alizarin, phenantherene,

anthraquinone carbazole calico printings, etc. It is also used as a component of smoke

screen and also finds large uses in chemical industries. Its demand is increasing fast

with the development of chemical and allied industries. At present, there exists a gap

between the demand and supply and hence the product is running in a short supply.

During the Carbonization of coal, thermal cracking occurs which yield simple

volatile aromatics and gaseous products of carbonization of bituminous coal are

indicated below:

Bituminous Coal

Residue Distillate

Coke oven Gas Light Oil Ammonia Coal tar

Liquor (cooling)

(straw oil scrubbing) (water scrubbing)

One ton of Bituminous coal yields about 17-90 gallons of Coal tar.

6

Fractions obtained in Coal Tar

Table 1:

Fraction Temperature range % by Volume Chief constituent

Light oil <170°C 5 Benzene

Middle oil 170-230°C 5-7 Toluene, Creosol

Heavy oil 230-270°C 10 Creosol

Anthracene oil 270-400°C 20 Naphthalene

Pitch Residue left 57.5 Anthracene

The above fractions collected at different temperatures are worked up for the

recovery of Aromatic compounds. Anthracene is obtained from Anthracene oil of

fractions. The oil shows Green Fluorescence, it is called Green Oil.

The structure of Anthracene is

Although coal was first carbonized in Britain towards the end of 18th century to

provide tar as a substitute for wood tar used in ship buildings, and it owes its

inception to the development of gas lighting in England during early twenty years of

19th century. Most of crude intermediates were imported from Britain.

Anthracene

7

By 20th century, tar distillation had become established as a separate and

important in Germany and United States. Notable development of coal tar distillation

gives anthracene, which was used as a dye intermediates and a component of smoke

screen, pitch as road binder and the invention of Phenol-Formaldehyde resins.

8

CHAPTER 2

VARIOUS PROCESSES

Anhracene may be obtained as:

BY FRIEDAL-CRAFT REACTIONS

Benzyl chloride reacts with itself to form 9,10-dihydroanthracene, which readily

loses two hydrogen atoms to yield anthracene.

It may also prepared by the FRIEDAL-CRAFTS Reaction between Benzene and

1,1,2,2-tetrabromomethane (anthracene tetra bromide) or between Benzene and

dibromomethane.

BY ELBS REACTION

O

C

CH3 Zn(-2h20)

400-450 °C

CH2Cl H

CH2Cl H

AlCl3

(-2 H Cl)

H H

H H9,10-dihydroanthracene

Anthracene

Anthracene

9

The conversion of a diary ketone containing a methyl or methylene group, ortho

to the carbonyl function is known as the ELBS Reaction.

O

C

CH3

450 °C

Anthracene

10

CHAPTER 3

PROCESS DESCRIPTION

ANTHRACENE FROM COAL TAR

The process of manufacture of anthracene involves a series of unit operations

and is derived from the distillation of coal tar, which is obtained during the coking of

coal. The separation of substrates is applied to collect the various chemicals. The

chamber is heated to about 800-900°C and the vapors thus formed is allowed to pass

through a long condenser at different temperatures. One cut obtained is run into a

shallow tanks and the solid component separates out on cooling.

The process requires one or two weeks. The semisolid mass is transferred to bag

filter press and much of its oil is driven out by using compressed air.

The nearly dry cake is obtained by filtration contains 10-15% Anthracene. It is

subjected to the pressure of 50000-70000psi in hydraulic press to bring anthracene

content to 25-35%. The pressed cake are grounded and washed in a closed solvent

agitator with hot solvent naphtha from the light oil.

Anthracene is thus produced by the sublimation of the washed materials. The

subliming process are similar to those used for naphthalene except that they are

heated by fire and hone jet of super heated steam impinging upon the surface by

wetting the anthracene. The oil from the crystallization of the crude anthracene is

distillate in a clean still unit. Crystals appears upon cooling the distillate, when the

residue containing the pans and are treated the same as the original fractions.

Anthracene

11

CHAPTER 4

PROPERTIES

4.1 Physical Properties

Anthracene is a colorless solid. It boils at 340°C. Anthracene is insoluble in

water, but completely dissolves in benzene. It shows a strong blue fluorescence when

exposed to UV-light. This fluorescent property of anthracene is used in critical

direction work, since small amount of finely powdered in anthracene on clothing,

skin, money, etc., is not detected under ordinary light but easily noticed when

exposed to ultraviolet radiations.

Specific gravity : 1.25

Solubility : soluble in alcohol,ethers, insoluble in water

Heat of combustion : 1707.06 cal/kg

Specific heat : 0.361 cal/kmol°C(20-210°C)

Melting point ; 213°C

4.2 Chemical Properties

Reaction with Sodium

Anthracene reacts with metallic sodium in liquid ammonia to form a deep blue

9,10-disodioanthracene. When the disodio- derivative is heated with an alkyl halide,

it gives the corresponding 9,10-di-alkyl anthracene.

+ 2NaLiq NH3 2Na+

+ CH3CH2Cl

Δ

CH2CH3

CH2CH3

Anthracene

9,10-diethylanthracene

12

Friedel Craft’s Acylation

Anthracene undergoes acylation with acetyl chloride and aluminium chloride in

benzene to form 9-acetyl anthracene.

Nitration

Anthracene undergoes nitration with concentrated nitric acid in acetic anhydride

at room temperature to yield a mixture of 9-nitranthracene and

9,10-dinitroanthracene.

Reduction

Anthracene undergoes reduction with sodium and ethyl alcohol to form

9,10-dihydroanthracene.

Oxidation

Anthracene undergoes oxidation with sodium dichromate and sulfuric acid to

form 9,10-anthraquinone

Cl

Al

Cl

Cl

AlCl3

CH3

Cl

O+

CH 3 O

Acetyl Chloride 9,10-Acetylanthracene

+ KCl

+ 2HNO3(CH3CO2)2NO2

N+

O-

ON+

O-

O

+

9-Nitroanthracene 9-Nitroanthracene

C2H2OH

Na

HH

H H

Na2Cr2O7

H2SO4O

O

O

9,10-anthraquinone

Anthracene

Anthracene

Anthracene

Anthracene

13

CHAPTER 5

MATERIAL BALANCE

TYPICAL TAR COMPOSITION IN WEIGHT BASIS

BENZENE = 1.00

OTHER LIGHT OIL = 0.70

PHENOLS = 0.30

CRESOLS = 0.30

NAPTHALENE = 4.30

CREOSTE OIL = 28.30

FLUORENE = 0.05

PHENANTHENE = 0.13

UN-IDENTIFIED = 0.04

ANTHRACENE = 0.04

CARBAZOLE = 0.04

PITCH = 64.8

_____________

TOTAL = 100.00

14

MATERIAL BALANCE FOR EQUIPMENTS

INPUT

Amount of Feed required = (0.8/0.0004)*150,000

= 300,000 tons

% of residue settled as a pitch

in distillation column = 64.8%

% of vapour leaving the distillation column = 35.2%

Amount of vapors from distillation column = 300000*0.352

= 105600 tons

DISTILLATION CHAMBER

Feed = 300000 tons

Vapors = 105600 tons

Residue = 194400 tons

CONDENSER

% of vapors condensed in the I-Cut of the condenser = 2.3%

Amount of vapors condensed in I-Cut of the condenser = 300000*0.023

= 6900 tons

% of vapors condensed in the II-Cut of the condenser = 32.6%

Amount of vapors condensed in II-Cut of the condenser = 300000*0.326

= 97800 tons

% of vapors condensed in the III-Cut of the condenser = 0.3%

15

Amount of vapors condensed in III-Cut of the condenser= 300000*0.003

= 900 tons

Input vapors = 105600 tons

OUTPUT

I Cut = 6900 tons

II Cut = 97800 tons

III Cut = 900 tons

TOTAL = 105600 tons

COOLER

Input = Output

Input = 105600 tons

FILTER PRESS

% of Anthracene in input = (120000/900000)*100

= 13.33%

% of Anthracene in liquid waste = 20% (assumed)

Amount of liquid waste removed = [{(100-13.33)/13.33}-

{(100-20)/20}]*120000

= 300225.05 kg

Amount of cake = 900000-300225

= 599775 kg

16

HYDRAULIC PRESS

% of Anthracene in the liquid = 20%

% of Anthracene in the output = 35%

Amount of liquid waste removed = [{(80/20)-(65/35)}*120000]

= 257142.85 kg

Amount of pressed cake = 599775-257142.85

= 342632.15 kg

WASHING TANK

Amount of pressed cake input = 342632.15 kg

Amount of solvent naphtha used = 39300 kg

Amount of solution as output = 342632.15+39300

= 381932.15 kg

CRYSTALLIZER

Amount of Feed to Crystallizer = 381932.15 kg

Amount of Anthracene = 171460.5 kg

Crystallized out

Amount of mother liquor = 381932.15-171460.5

= 210471.65 kg

DRYER

Let purity of crystals at inlet = 70%

Amount of crystals as feed = 171460.5 kg

17

Purity of crystals at the outlet = 80%

Amount of volatile impurities = [{(30/70)-(20/80)}]*120000

= 21460.5 kg

Dried crystals = 171460.5-21460.5

= 150000 kg

= 150 tons

18

Process Material Flow Representation

Coalstorage

condensor

pump

Cooler filterpress

hydraulicpress

washingtank

crystallizerRotarydryer

ANTHRACENECRYSTAL

vaporsSolvent Naphtha

DISTILLA

TION

CO

LUM

N

ICU

T

IICU

T

IIICU

T

(3L ton)

194400 tons

105600 tons

105600 tons

599775 kg

342632 kg

39300 kg

381932 kg

171460 kg

150032 kg

105600 tons

19

CHAPTER 6

ENERGY BALANCE

Table 1:

I-Cut

COMPONENTS WEIGHT

%

BOILING

POINT

°C

SPECIFIC

HEAT CP

Cal/gm°C

LATENT HEAT

OF

VAPOURISATION

* Cal/gm

MASS

Kg

*105

BENZENE 0.5 80.1 0.406 103.6 1.5

TOLUENE 0.5 110.8 0.5 46.8 1.5

LIGHT OILS 0.7 150 0.5 150 2.1

PHENOL 0.3 182 0.561 269.9 0.9

CRESOL 0.3 190.8 0.499 100.6 0.9

Heat to be supplied:- = m(CP ΔT + L )

1. Benzene = 1.5 * 105 [0.406(80.1-25)+103.6]

= 1.89 * 107 Kcal

2. Toluene = 1.5 * 105 [0.5(110.8-25)+46.8]

= 1.34 * 107 Kcal

3. Light oils = 2.1*105 [0.5(150-25)+150]

20

= 4.46 * 107 Kcal

4. Phenol = 0.9*105 [0.561(182-25)+269.9]

= 3.22 * 107 Kcal

5. Cresol = 0.9*105 [0.499(190.8-25)+100.6]

= 1.65 * 107 Kcal

Total heat supplied for the I-Cut = 12.56 * 107 Kcal

21

Table 2

II Cut

COMPONENTS WEIGHT

%

BOILING

POINT

°C

SPECIFIC

HEAT CP

Cal/gm°C

LATENT HEAT

OF

VAPOURISATION

* Cal/gm

MASS

Kg

*106

NAPTHALENE 4.3 217.9 0.402 75.5 1.29

PHENOL 14.15 182 0.561 269.9 4.245

CRESOL 14.15 190.8 0.499 100.6 4.245

Heat to be supplied:- = m(CP ΔT + L )

1. Naphthalene = 1.29 * 106 [0.402(217.9-25)+75.5]

= 1.974 * 108 kcal

2. Phenol = 4.245 * 106 [0.561(182-25)+269.9]

= 15.196 * 108 kcal

3. Cresol = 4.245 * 106 [0.499(190.8-25)+100.6]

= 7.78 * 108 kcal

Total heat to be supplied to the II Cut = 24.950 * 108 kcal

22

Table 3

III Cut

COMPONENTS WEIGHT

%

BOILING

POINT

°C

SPECIFIC

HEAT CP

Cal/gm°C

LATENT HEAT

OF

VAPOURISATION

* Cal/gm

MASS

Kg

*105

Phenanthrene 0.13 342 0.325 71.03 3.9

Fluorine 0.05 295 0.442 71.03 1.5

Un-identified 0.04 300 0.45 71.03 1.2

Anthracene 0.04 342 0.500 71.03 1.2

Carbazole 0.04 354.7 0.465 71.03 1.2

Heat to be supplied = m(CP ΔT + L )

1. Phenanthrene = 3.9 * 105 [0.325(342-25)+71.03]

= 6.78 * 107 kcal

2. Fluorine = 1.5 * 105 [0.442(295-25)+71.03]

= 2.85 * 107 kcal

3. Anthracene = 1.2 * 105 [0.45(342-25)+71.03]

= 2.75 * 107 kcal

23

4. Carbazole = 1.2 * 105 [0.465(354.7-25)+71.03]

= 2.69 * 107 kcal

Total heat to be supplied for III Cut = 15.07 * 107 kcal

To find the heat supplied for Pitch:

Mass(m) = 3 * 108 * 0.648

= 1.944 * 108 kg

Specific heat(Cp) = 0.5 cal/g°C

Heat supplied for pitch= m CP ΔT

= 1.944 * 108 * 0.5 (800-25)

= 7.533 * 1010 kcal

Total heat to be supplied= 15.07 * 107 + 7.533 * 1010

= 7.548 * 1010 kcal

CONDENSOR

I CUT:

Latent heat of Benzene = 1.5 * 105 * 103.6

= 1.554 * 107 kcal

24

Latent heat of Toluene = 1.5 * 105 * 46.8

= 0.702 * 107 kcal

Latent heat of Light oils = 2.1 * 105 * 150

= 3.15 * 107 kcal

Latent heat of Phenol = 0.9 * 105 * 269.9

= 2.43 * 107 kcal

Latent heat of Cresol = 0.9 * 105 * 100.6

= 0.9054 * 107 kcal

Total latent heat of I Cut = 8.7414 * 107 kcal

II CUT

Latent heat of Naphthalene = 1.29 * 106 * 75.5

= 0.974 * 108 kcal

Latent heat of Phenol = 4.245 * 106 * 269.9

25

= 11.45 * 108 kcal

Latent heat of Cresol = 4.245 * 106 * 100.6

= 4.27 * 108 kcal

Total heat of II Cut = 16.694 * 108 kcal

III CUT

Latent heat of Phenanthrene = 3.9 * 105 * 71.03

= 2.77 * 107 kcal

Latent heat of Fluorine = 1.5 * 105 * 71.03

= 1.06 * 107 kcal

Latent heat of Un-identified = 1.2 * 105 * 71.03

= 0.85 * 107 kcal

Latent heat of Anthracene = 1.2 * 105 * 71.03

= 0.85 * 107 kcal

Latent heat of Carbazole = 1.2 * 105 * 71.03

26

= 0.85 * 107 kcal

Total latent heat of III Cut = 6.38 * 107 kcal

Sensible heat = [Total heat] - [Latent heat]

Sensible heat(I Cut) = Total heat(I Cut) - Latent heat(I Cut)

= 12.56 * 107 - 8.7414 * 107

= 3.8186 * 107 kcal

Sensible heat(II Cut) = Total heat(II Cut) - Latent heat(II Cut)

= 24.95 * 108 - 16.694 * 108

= 8.256 * 108 kcal

Sensible heat(III Cut)= Total heat(III Cut) - Latent heat(III Cut)

= 15.07 * 107 - 6.38 * 107

= 8.69 * 107 kcal

COOLER

To find the heat to be removed: = m CP (B.P - 50)

Heat removed from phenanthrene = 3.9 * 105 (0.325) (342-50)

= 3.7 * 107 kcal

27

Heat removed from fluorine = 1.5 * 105 (0.442) (295-50)

= 1.62 * 107 kcal

Heat removed from un-identified = 1.2 * 105 (0.45) (300-50)

= 1.35 * 107 kcal

Heat removed from Anthracene = 1.2 * 105 (0.5) (342-50)

= 1.75 * 107 kcal

Heat removed from carbazole = 1.2 * 105 (0.465) (354.7-50)

= 1.7 * 107 kcal

Heat to be removed from cooler = 10.12 * 107 kcal

Enthalpy in the outlet of cooler = Inlet - heat removed

= 10.12 * 107 - 8.69 * 107

= 1.43 * 107 kcal

FILTER PRESS

Amount of feed to the filter press = 9 * 105 kg

Amount of liquid waste = 3 * 105 kg

Amount of cake = 6 * 105 kg

Heat input to the filter press = 1.43 * 107 kcal

Heat carried by liquid waste = [(1.43 * 107 / 9 * 105) * 3 * 105]

28

= 4.76 * 106 kcal

HYDRAULIC PRESS

Heat carried by cake = 4.76 * 106 kcal

Weight of cake = 6 * 105 kg

Heat carried by liquid waste = [(4.76 * 106 / 6 * 105) * 2.57 * 105]

= 2.04 * 106 kcal

Heat carried by pressed cake = 4.76 * 106 - 2.04 * 106

= 2.76 * 106 kcal

WASHING TANK

Heat input to washing tank in

Heat carried by pressed cake = 2.72 * 106 kcal

Temperature at the outlet = [(3.43 * 105 * 0.3165) +

3.93 * 104 * 0.5] (t0 - 25)

Heat feed at the inlet will be equal to heat delivered at the outlet

since the solvent heat is zero,

128.1 * 106 = 2.72 * 106 (t-25)

t = 48.2 °C

CRYSTALLIZER:(30°C)

Amount of heat

29

released in crystallization = 1.2 * 105 * 38.75

= 4.64 * 106 kcal

Amount of water to be used:

To remove 4.64 * 106 kcal = 4.64 * 106 / CP ΔT

Amount of water = (4.64 * 106) / [1 * (40 - 25)]

= 3.096 * 105 kg

Heat content at the inlet = heat content at the outlet

= 2.72 * 106 kcal

Feed of crystals = 3.82 * 105 kg

Amount of heat in the crystals = 2.72 * 106 * 171460.5 / 3.82 * 105

= 1.22 * 106 kcal

Amount of heat in the mother liquor = 2.72 * 106 - 1.22 * 106

r = 1.5 * 106 kcal

DRYER

Heat input to the dryer = (171460.5) * (0.5) * (t - 25)

1.22 * 106 = (171460.5) * (0.5) * (t - 25)

Outlet temperature t = 39.2 °C

Amount of heat required to = 171460.5 * 71.03

remove the volatile impurity = 12.178 * 106 kcal

30

Amount of heat required to

raise the temperature of feed = (171460.5) * (0.5) * (70 - 40.5)

= 2.64 * 106 kcal

Heat to be supplied by air = 2.64 * 106 + 12.178 * 106

= 14.818 * 106 kcal

Inlet temperature of air outlet = 120 °C

Temperature of air = 80 °C

Specific heat CP of air = 7 kcal/kmol

Amount of air = 14.818 * 106 / 7 (120 - 80)

= 14388 kmol

31

CHAPTER 7

DESIGN OF CRYSTALLIZER

Feed flow rate = 120000kg/hr

Xf = 81.1/240

= 0.33

Xm = 43.32/17

= 0.249

Xc = 178/304

= 0.585

Overall Material balance

F = M + C

120000 = M + C

21 °C, cw outlet

15 °C, cw inlet

Mothersolution(27 °C)

65 °C

Feed solution(C12H8C2H2).7H2O

CRYSTALLIZER

32

Solute Balance

F Xf = M Xm + C Xc

(120000) * 0.3 = M * (0.249) + C * (0.585)

C = 28928.57 kg/hr

M = 91071.4 kg/hr

Energy balance

Q = F Cp ΔT + (ΔHc) C

Q = 120000 * 7 (65 - 27) + 1602 * 28298.57

Q = 3660642.83 Kcal/hr

Cooling water required

Q = Mw Cp ΔT

Mw = 610107.1 kg/hr

Area

A = Q/ U ΔT

= 3660642.83 / 175 * 38

A = 550.47 m2

Length

Length = A / cooling surface requied

= 550.47 / 15

L = 36.69 m

33

DESIGN SUMMARY

Cooling water required(Mw) = 610107.1 kg

Area required, A = 550.47 m2

Length, L = 36.69 m

34

CHAPTER 8

COST ESTIMATION

LIST OF EQUIPMENTS

1. Distillation column = Rs. 45.57 L

2. Condensor = Rs. 21.36 L

3. Cooler = Rs. 18.63 L

4. Filter press = Rs. 32.35 L

5. Hydraulic press = Rs. 34.42 L

6. Crystallizer = Rs. 12.78 L

7. Dryer = Rs. 8.79 L

8. Pump = Rs. 1.02 L

Total cost of purchased equipments = Rs. 1.74 C

Fixed Capital investment = Rs. 1.74/0.35

= Rs. 5.00 C

Total Direct cost = Rs. 3.44 C

Total Indirect cost = Rs. 78.21 L

Fixed Capital cost = Total direct cost + Total indirect cost

= Rs. 4.22 C

Total capital cost = Rs. 4.22/0.8

35

= Rs. 5.27 C

Total Production cost = Rs. 3 * 109

Turnover = Rs. 3.03 * 109

Profit = Rs. 1.30 C

Payback period =

= 2.48 years (≈30 months)

on)Depreciati (Profit investment capital Fixed

36

CONCLUSION

The manufacture of Anthracene from coal tar thus produces about

150tons of Anthracene and the crystallized product is 1.71 * 105 kg, which is more

approximated to the total quality of end product. More purity in quality was obtained

from the crystallizer unit.

Addition to that, the crystallizer is used for the purification of many

organic components in the industries. The enthalpy of crystallization are generally much

lower than the enthalpies of vaporization.

37

REFERENCE

i. N. N. Lebedev, Chemistry and Technology of Basic Organic and Chemical

Synthesis(541-548) Vol-II, Mir publishers Moscow.

ii. Kirk-Othmer, Encyclopedia of Chemical Technology vol 16 (541-551) 4th edition,

Awiley-Interscience.

iii. Robert Meyers, a Handbook of Chemical Production Processes, (300-315) McGraw

Hill, Newyork, 1SG6.

iv. George T. Austin, Shreves Chemical Industries, (760-775) 5th edition, McGraw Hill

Book company, Singapore.

v. B. I. Bhatt and S. M. Vora, Stoichiometry (110-119) 3rd edition 1998, McGraw Hill

Book Company, New Delhi.

vi. L. M. Rose, Chemical Reactor Design in Practice (247-300) Elseiver Scientific

publishing company, 1931.

vii. Max. S. Peters, Klaus D. Tmmerhaus, Plant Design and Economics for Chemical

Engineers (400-423) McGraw Hill International, 4th Edition.