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T.R. EGE UNIVERSITY Chemical Engineering Department CONCEPTUAL DESIGN I PROJECT I Prepared by; 05068062 Deniz TOSUN 05057350 Onur ASLAN 05068091 M.Serkan ACARSER 05068113 Baturalp AYTAN 05068052 Ali KÜÇÜK Submitted to: Prof.Dr.Ferhan ATALAY Res.Assist. Meral DÜKKANCI Dr.Sezai ERDEM March 2010 Bornova-İZMİR Date: 29.03.2010
Transcript
Page 1: 38621213 Project I Acrolein Production

T.R. EGE UNIVERSITY

Chemical Engineering Department

CONCEPTUAL DESIGN I PROJECT I

Prepared by;

05068062 Deniz TOSUN 05057350 Onur ASLAN

05068091 M.Serkan ACARSER 05068113 Baturalp AYTAN

05068052 Ali KÜÇÜK

Submitted to: Prof.Dr.Ferhan ATALAY

Res.Assist. Meral DÜKKANCI Dr.Sezai ERDEM

March 2010 Bornova-İZMİR

Date: 29.03.2010

Page 2: 38621213 Project I Acrolein Production

i

SUMMARY

Acrolein is a highly toxic, flammable material with extreme lacrimatory properties. It

is a widely used intermediate in the production of building materials, herbicides and

algaecides, water treatment chemicals, and essential amino acids like methionine. The overall

objective of this process is to produce 69.000 ton Acrolein per year.

The current industry standard for production of Acrolein is via the catalytic partial

oxidation of Propylene. First propylene and water heated up to a suitable temperature for the

reaction and sent to the reactor. In the reactor part propylene is burned with excess oxygen. The

stream coming from the reactor is cooled by using a quench cooler and has got 2 exit streams. The

main stream enters into Acrolein absorber and the other directly enters to water distillation. In the

Acrolein absorber some of the Acrolein and propylene sent to incinerator to be burned. The other

stream is sent to water distillation. Water distillation separates the stream for waste water and

another distillation to obtain pure product. To obtain purified product the stream coming from the

water distillation unit enters into Acrolein distillation unit where Acrolein obtained with %98

purity. Detailed flowchart and calculations of the streams are given in Appendix part of the report.

During the calculation process we had to choose or assume some variables and calculations may

contain errors due to calculation errors and neglected values. All these effecting situations are

discussed in Discussion part of the report.

Finally; we believe that this report will help the reader to understand Acrolein production

process and will facilitate further calculations in this subject.

Page 3: 38621213 Project I Acrolein Production

TABLE OF CONTENTS

Summary i

1.Introduction 1

2.Results 2

3.Discussions and Conclusions 5

4.Nomenclature 7

5.References 8

6.Appendix 9

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1.0 INTRODUCTION

Acrolein is primarily used as an intermediate in the synthesis of acrylic acid and as a biocide. It may be formed from the breakdown of certain pollutants in outdoor air or from the burning of organic matter including tobacco, or fuels such as gasoline or oil. It is toxic to humans following inhalation, oral or dermal exposures. Acute (short-term) inhalation exposure may result in upper respiratory tract irritation and congestion. No information is available on its reproductive, developmental, or carcinogenic effects in humans, and the existing animal cancer data are considered inadequate to make a determination that Acrolein is carcinogenic to humans.

The largest single use for Acrolein is as an unisolated intermediate in the manufacture of acrylic acid, most of which is converted to its lower alkyl esters. Acrolein is also used as a herbicide and algicide in irrigation waters and drainage ditches; as a biocide in the control of algae, weeds, and mollusks in recirculating process water systems; as a slimicide in the paper industry; as a biocide in oil wells and liquid petrochemical fuels; in the cross-linking of protein collagen in leather tanning; as a tissue fixative in histological samples; in the manufacture of colloidal forms of metals; in the production of perfumes; as a warning agent in methyl chloride refrigerant; and as an intermediate in the manufacture of methionine and its hydroxyl analogue, glutaraldehyde, ally1 alcohol, pyridines, and tetrahydrobenzaldehyde. Isolated, refined acrolein is used mainly as a biocide and as an intermediate in the production of methionine, which is a protein supplement used in animal feed. Acrolein has been used to make modified food starch, synthetic glycerine, acrolein polymers, polyurethane, and polyester resins. It has also been used in military poison gas mixtures. Partial oxidation of Acrolein is a commercially important reaction, its product acrylic acid being widely used industrially for producing resins, dyes, glues, nonwoven fabrics, etc.

Partial oxidation of Acrolein is also a convenient model reaction because, the number of reaction products is moderate (CO, CO2

, acrylic acid) and their difference in acid-base properties from the starting material makes it possible to select desirable catalysts by applying directly.

The study of the reaction mechanism includes determination of structures and energy characteristics of the surface intermediates and the elucidation of their connection with catalyst chemical composition and reaction routes to particular products. This reliable information helps us to understand the nature of catalyst action and to elaborate the theory of catalyst selection. We have used this method to approach the problem of the systematic selection of catalysts for the oxidation of Acrolein to acrylic acid.

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2.0 RESULTS Table 1.Calculated basis mol and mass values of substances

Acrolein Acrolein Water Water PP PP O2 O2 N2 N2

kmol/h ton/year kmol/h ton/year kmol/h ton/year kmol/h ton/year kmol/h ton/year 1 - - - - 100 36792 - - - - 2 - - - - 100 36792 - - - - 3 - - 419,22 66102,61 - - - - - - 4 - - 419,22 66102,61 - - - - - - 5 - - - - - - 126,97 35592,23 477,65 117158 6 - - - - - - 126,97 35592,23 477,65 117158 7 - - 419,22 66102,61 100 36792 126,97 35592,23 477,65 117158 8 - - 419,22 66102,61 100 36792 126,97 35592,23 477,65 117158 9 47 23081,02 500 78840,00 33 12141,36 29,3 8213,376 477,65 117158 10 - - 14880,43 2346345,41 - - - - - - 11 - - 14880,43 2346345,41 - - - - - - 12 0,94 461,62 15226,6 2400930,29 - - - - - - 13 46,06 22619,40 153,8 24251,18 33 12141,36 29,3 8213,376 477,65 117158 14 - - 9900 1561032,00 - - - - - - 15 3,362 1651,03 - - 33 12141,36 29,3 8213,376 477,65 117158 16 42,698 20968,37 10052,6 1585093,97 - - - - - - 17 43,638 21429,99 25280,43 3986218,20 - - - - - - 18 0,436 214,11 25252,76 3981855,20 - - - - - - 19 43,202 21215,88 27,67 4363,01 - - - - - - 20 42,98 21106,86 0,86 135,60 - - - - - - 21 0,216 106,07 26,81 4227,40 - - - - - - 23 0,652 320,19 25279,57 3986082,60 - - - - - -

Table 2. Molecular weight and scale-up factor

Molecular Weight [kg/kmol]

Boiling Point Temperature [0C]

Melting Point Temperature [0C]

Standart Entaphy of Formations [kJ/kmol]

Acrolein 56.06 53 -88 -81800 Water 18 100 0 -241814

Propylene 42 -47.6 -185.2 20230 O2 32 -182.95 -218.79 0 N2 28 -195.79 -210 0

Acrylic Acid 72.06 141 14 -355910 CO2 44 -57 -78 -393510

Scale Up Factor 3.269079483

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Table 3. Calculated desired mol and mass values of substances

Scale up

Acrolein Acrolein Water Water PP PP O2 O2 N2 N2

kmol/h ton/year kmol/h ton/year kmol/h ton/year kmol/h ton/year kmol/h ton/year 1 - - - - 326,91 120275,97 - - - - 2 - - - - 326,91 120275,97 - - - - 3 - - 1370,46 216094,68 - - - - - - 4 - - 1370,46 216094,68 - - - - - - 5 - - - - - - 415,08 116353,83 1561,48 382998,79 6 - - - - - - 415,08 116353,83 1561,48 382998,79 7 - - 1370,46 216094,68 326,91 120275,97 415,08 116353,83 1561,48 382998,79 8 - - 1370,46 216094,68 326,91 120275,97 415,08 116353,83 1561,48 382998,79 9 153,65 75453,70 1634,54 257734,23 107,88 39691,07 95,78 26850,18 1561,48 382998,79 10 - - 48645,29 7670389,65 - - - - - - 11 - - 48645,29 7670389,65 - - - - - - 12 3,07 1509,07 49776,97 7848831,95 - - - - - - 13 150,57 73944,63 502,78 79279,05 107,88 39691,07 95,78 26850,18 1561,48 382998,79 14 - - 32363,89 5103137,68 - - - - - - 15 10,99 5397,35 - - 107,88 39691,07 95,78 26850,18 1561,48 382998,79 16 139,58 68547,28 32862,75 5181798,17 - - - - - - 17 142,66 70056,35 82643,74 13031264,14 - - - - - - 18 1,43 699,95 82553,28 13017001,13 - - - - - - 19 141,23 69356,40 90,46 14263,01 - - - - - - 20 140,51 69000 2,81 443,30 - - - - - - 21 0,71 346,77 87,64 13819,71 - - - - - - 23 2,13 1046,72 82640,92 13030820,84 - - - - - -

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Equipment List Displayed

Text Description

C-101 Feed Air Compressor E-101 Reactor Preheater E-102 Condenser E-103 Reboiler E-104 Condenser E-105 Reboiler E-106 Condenser E-107 Reboiler E-108 Reboiler Q-101 Quench Cooler T-101 Acrolein Absorber T-102 Water Distillation Tower T-103 Acrolein Distillation Tower V-101 Reflux Vessel V-102 Reflux Vessel V-103 Reflux Vessel E-104 Condenser E-105 Reboiler E-106 Condenser

Q-101

Figure 1. Flowsheet for Acrolein Production

Page 8: 38621213 Project I Acrolein Production

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3.0 DISCUSSIONS AND CONCLUSIONS

Acrolein is a clear or yellow liquid with a burnt, sweet, pungent odor. It is primarily

used to make other chemicals and may also be found in some livestock feed. It is a pesticide

and is added to irrigation canals and the water supplies of some industrial plants to control

underwater plant, algae and slime growth. At much higher concentrations it may be used to

make chemical weapons. It is widely used as intermediate in the production of building materials

as well.

For the production of Acrolein there are two processes mainly considered in industry. One

of them is partial oxidation of propylene, the other process is production with Glycerin. In this

report we prefer to use partial oxidation of propylene process. But economically since Propylene

is obtained from crude-oil resources, this process is not considered to be feasible in long term

because of increasing crude oil prices and the depletion of crude oil resources. Today another

option namely production by glycerin can be considered as an economic alternative since glycerin

can be obtained from soap production. In addition glycerin is a side product of the

transesterification of vegetable oils to manufacture biodiesel. This means as the biodiesel

production increases it would be easy to find great amount of glycerin at lower costs. From the

environmental perspective glycerin process would be more environments friendly since there is no

any oxidation reactions, no carbon dioxide emissions.

For partial oxidation of propylene; the process starts with preheater. Preheater is used to

heat the inlet stream before it enters into reactor. The reason we heat the inlet stream to 250°C is

to maintain reaction rate and kinetics optimum. After obtaining the desired temperature for the

reaction, reaction data such as fractional conversion, selectivity and yield allowed us to find extent

of reactions for each reaction. Using these data we made first the mass balance. Water stream was

added to reactor to prevent reactor temperature increasing sharply and for to keep the system in

safe. The amount of this water stream is determined by mass balance and given design restrictions

such as percent inert, percent propylene, percent oxygen. Water amount should be between 353

kmol/h and 489 kmol/h. As the designer we assign water to be 419 kmol /h. For energy balance

heat released equals to the difference between outlet and inlet enthalpies and additionally heats of

reactions. For this purpose all heat of reactions multiplied by their extents of reactions and added

to heat term and the total heat from the reactor was calculated as 6456.85 kW.

Page 9: 38621213 Project I Acrolein Production

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In the quench cooler section the reactor effluent is directly sent to quench cooler to be

quenched in cold water. According to given data mass balance of the unit made. Energy balance

should be done using inlet and outlet enthalpies of streams and in addition heats of condensations

should be considered. In the calculations section we did not include heats of condensation so

energy balance only includes outlet and inlet enthalpies. Also specific heat values are calculated

using correlations of Perry’s Chemical Engineers Handbook for various temperatures. They may

contain errors. We have two outlet streams from quench cooler. First one is to Acrolein absorber

the other is directly to water distillation. By the givens mass balances made on Acrolein absorber

and the required energy is calculated as 51.75

kW using energy balance equation. Outlet and inlet

enthalpies at different temperatures using specific heats calculated assuming no phase change.

Phase change terms are not included in our calculations. So, they may greatly affect the results we

found.

In the water distillation tower same procedure was made for the calculations and the

results were found as mass and energy terms for significant products. The top product of the tower

that is Acrolein was found as 43.2 kmol/h and the bottom product that is water was obtained as

25132.75 kmol/h. The outlet stream enthalpy was calculated as 143.42*106 kJ/h and the inlet

steam enthalpy was found as 0.242*106 kJ/h. Finally total enthalpy was determined as 39.77*103

kW. The reason of the high value of total enthalpy from the tower is that the usage of the cooling

water is too much for the system conditions.

At the end of the process the Acrolein distillation tower calculations were found as 42.98

kmol/h for the desired product Acrolein and the total heat value was determined as 13.9 kW.

The total heat required for this process is found to be 51.88 kW. This is a great amount of

energy if we think of a great production scale. To maintain the reactions and operations in a

proper way, we should think of energy requirements or releases of each unit and related heating or

cooling systems to be installed. But of course these systems like jackets, coils will mean

additional investment and operating costs.

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4.0 NOMENCLATURE

MW = Molecular Weight [kg/kmol]

n = molar flow rate [kmol/h]

y = mol or mass fraction of gas stream [-]

x = mol or mass fraction of liquid stream [-]

PT

P

= Total Pressure [bar]

i

P

* = Vapour Pressure of Component [bar]

v

T = Temperature [°C]

* = Vapour Pressure [bar]

∆Hvap

T

= Latent Heat of Vaporisation [kJ/kg]

C

P

= Critical Temperature [°C]

C

T

= Critical Pressure [bar]

b

Q = Heat [kJ]

= Normal Boiling Point [°C]

m = Mass Flow Rate [kg/h]

Cp=Specific Heat Capacity [kJ/kmolK]

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5.0 REFERENCES

1. Elemantary Principles of Chemical Processes 3rd Ed. Felder, Rousseau ,2003 John Wiley and Sons

2. http://en.wikipedia.org/

3. Perry's Chemical Engineers Handbook-8th ed – 2007.

4. Project I Data Sheet –Conceptual Design I Course ,Department of Chemical Engineering, Ege University 2010

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6.0 APPENDIX

6.1 Mass Balance Calculation

6.1.1 Reactor

4 reactions will be carried out in the reactor. These are;

: Extent of Reaction

Taking 100 kmol/h basis ;

Fractional Conversion of fed to the reactor is % 67 so ;

= 0.67

Selectivity of to is 5 kmol/kmol

Yield of to

: 100 kmol/h

: W kmol/h

Air : 604.62 kmol/h

(0.79 N2, 0.21 O2)

: 33 kmol/h

: 46 kmol/h

: 13.11 kmol/h

: 20.677 kmol/h

: W+80.78 kmol/h

: 29.3 kmol/h

: 477.65 kmol/h

R-101

8 9

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Conversion of to is %8.7

Solving these equations four equations simultaneously we obtain

required for the reaction : + 3.5* + 0.5 * + 4.5 * = 97.67 kmol/h

For our process we prefer to use %30 excess oxygen so;

Fed = Reacted * 1.3 = 126.971 kmol/h

To supply 126.971 kmol/h oxygen we need;

Air fed = = 604.62 kmol/h

balance

Input=Output + Consumption

100 kmol/h=Output + ( + )

Output=33 kmol/h

balance

Generation=Output+Consumption

= Output + +

Output=47 kmol/h

Page 14: 38621213 Project I Acrolein Production

- 11 -

balance

Generation=Output

=Output

Output=13.11 kmol/h

balance

Generation=output

=

Output=20.677 kmol/h

balance

input+generation=output

W+ +2* +3* =

Output= W+80.87 kmol/h

balance

input=output+consumption

126.971 =output+97.67

Output=29.3 kmol /h

input=output

output=604.62*0.79 = 477.6 kmol/h

Page 15: 38621213 Project I Acrolein Production

- 12 -

To decide amount of water to be used in the process we have some restrictions. Applying these restrictions;

Mol % Oxygen must be smaller than %12

Mol % Propylene must be smaller than %12

Mol % inert must be greater than %40 ( in the inlet feed)

kmol

Therefore 353.47 < W < 489.5

As we choose water amount between this interval ; we prefer inlet water to be 419.22 kmol.

Page 16: 38621213 Project I Acrolein Production

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6.1.2 Quench Cooler

*DATA: %2 of the acrolein,%80 of acrylic acid and %99 of water are bottom products. Calculation of Stream 12

47 kmol/h acrolein * 0.02 =0.94 kmol/h Acrolein.

13.11 kmol/h acrylic acid * 0.8 = 10.488 kmol/h Acrylic acid

(M+500 kmol/h water) * 0.99 =0.99M+495 kmol/h Water

Calculation of 13

(M+500 kmol/h water) *0.01=0.01M+5 kmol/h Water

33 kmol/h

47 kmol/h

13.11 kmol/h Same molar ratio with R

20.677 kmol/h

29.3 kmol/h

477.65 kmol/h

M value was calculated as 14880.425 kmol/h in energy balance part.

Que

nch

Coo

ler

11

9

12

13

Q-101

T11=25oC T12=50oC

T9=330oC

T13=50oC

: M kmol/h : 0,94 kmol/h : 10,488 kmol/h

: 0.99M+495 kmol/h

: 33 kmol/h : 47 kmol/h : 13.11 kmol/h

: 500 kmol/h : 20.677 kmol/h

: 29.3 kmol/h : 477.65 kmol/h

: 33 kmol/h : 47 kmol/h : 13.11 kmol/h

: 0.01M+5 kmol/h : 20.677 kmol/h

: 29.3 kmol/h : 477.65 kmol/h

Page 17: 38621213 Project I Acrolein Production

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6.1.3 Acrolein Absorber

o14T =25 C

2H O 9900 kmol/hn =

*DATA : 92.7% of C3H4O in feed stream are to be sent to the water distillation column. *DATA: 100% of C3H6 is recovered in the top product.

3 6

3 4

2

3 6

3 6

3 4

3 4

2

H O 2

For C H33 kmol/h *(100 /100) 33 kmol/h C H goes to top product

For C H O46.06 kmol/h *(1 92.7 /100) 3.36238 kmol/h C H O goes to top product

For H O9900 152.6042 10052.6 kmol/h H O goes

C H

C H O

n

n

n

= =

= − =

= + =

2

2

2

2 2 2

to bottom product

CO , O and N do not change in this process unit which go to bottom product20.67 kmol/h

29.301 kmol/h

477.6528 kmol/h

CO

O

N

n

n

n

=

=

=

T13=50o C

T16=50o C 3 6

3 4

3 4 2

2

2

2

2

H O

33 kmol/h

46.06 kmol/h

2.622 kmol/h

20.67 kmol/h

152.6042 kmol/h

29.301 kmol/h

477.6528 kmol/h

C H

C H O

C H O

CO

O

N

n

n

n

n

n

n

n

=

=

=

=

=

=

=

3 6

3 4

2

2

2

33 kmol/h

3.36238 kmol/h

29.301 kmol/h

477.6528 kmol/h

20.67 kmol/h

C H

C H O

O

N

CO

n

n

n

n

n

=

=

=

=

=

3 4

3 4 2

2H O

42.69762 kmol/h

2.622 kmol/h

10052.6 kmol/h

C H O

C H O

n

n

n

=

=

=

14

16

13

15

T-101

T15=50o C

Page 18: 38621213 Project I Acrolein Production

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6.1.4 Water Distillation Tower

3 4 3 4 3 4 3 4

3 4 2 3 4 2 3 4 2 3 4 2

2 2 2

C H O 17 C H O 12 C H O 16 C H O 17

C H O 17 C H O 12 C H O 16 C H O 17

H2O 17H O 17 H O 12 H O 16

n n n ; n 0.94 42.69762=43.63762

n n n ; n 10.488 2.622=13.11

n n n ; n 15107.82 10052.6 251

Inlet Streamkmol h

kmol h

= + = +

= + = +

= + = = + = 60.42 /kmol h

*DATA: 99.89% of water is recovered in bottom product *DATA: 1% of acrolein and 100% of acrolic acid is sent to be the waste water treatment with water

3 4 3 4 3 4

3 4 2 3 4 2 3 4 2

2 2 2

3 4 3 4

C H O 18 C H O 17 C H O 18

C H O 18 C H O 17 C H O 18

H O 18 H O 17 H O 18

C H O 19 C H O 17

n n *0.01 ; n 43.63762*0.01 0.436376

n n *1 ; n 13.11

n n *0.9989 ; n 25160.42*0.9989 25132.75

n n

Outlet Streamskmol h

kmol h

kmol h

= = =

= =

= = =

= −3 4 3 4

2 2 2 2

C H O 18 C H O 19

H O 19 H O 17 H O 18 H O 19

n ; n 43.63762 0.436376 0.436

n n n ; n 25160.42 25132.75=27.67647

kmol h

kmol h

= − =

= − = −

17

18

19

C3H4O : 43.63 kmol/h

C3H4O2 : 13.11 kmol/h

O2 : 29.301 kmol/h

C3H4O : 43.2 kmol/h

H2O : 27.67 kmol/h

C3H4O : 0.436 kmol/h

C3H4O2 : 13.11 kmol/h

H2O : 25132.75 kmol/h

T17=50oC

T19=52oC

T18=100oC

Page 19: 38621213 Project I Acrolein Production

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6.1.5 Acrolein Distillation Tower

*DATA : 99.5% of C3H4*DATA : C

O is feed stream are to be sent to Top Product 3H4

O is 98% purity.

Calculation of Top Product (20)

Calculation of Bottom Product (21)

19

21

20

T-103

: 43.2 kmol/h

: 27.67 kmol/h

T19=52o C

: 0.216 kmol/h

: 26.81kmol/h

: 42.98 kmol/h

: 0.86 kmol/h

T20=48oC

T21=82o C

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6.2 Energy Balance Calculation

6.2.1 Preheater

For C3H

3 6

3 6

3 6

523

393

5231 4 2 8 3

393

100* (3.71 2.345*10 * 1.16*10 * 2.204*10 * )

1157053.076 kJ/h

C H p

C H

C H

Q m c dT

Q T T T

Q

− − −

=

= + − +

=

6

For H2

2

2

2

523

393

5233 5 2 9 3

393

419.22* (32.243 1.923*10 * 1.055*10 * 3.569*10 * )

1907549.93 kJ/h

H O p

H O

H O

Q m c dT

Q T T T

Q

− − −

=

= + − −

=

O

For O

2

2

2

523

393

5236

393

126.971* (28.106 3.68*10 * )

463896.2801 kJ/h

O p

O

O

Q m c dT

Q T

Q

=

= −

=

2

T7=100o

T8=250oC

7 8

C3H6 : 100 kmol/h

H2O : 419.22 kmol/h

O2 : 126.971 kmol/h

N2 : 477.6528 kmol/h

C3H6 : 100 kmol/h

H2O : 419.22 kmol/h

O2 : 126.971 kmol/h

N2 : 477.6528 kmol/h

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For N

2

2

2

523

393

5232 5 2 8 3

393

477.6528* (31.15 1.356*10 * 2.679*10 * 1.168*10 * )

1828824.485 kJ/h

N p

N

N

Q m c dT

Q T T T

Q

− − −

=

= + + −

=

2

1157053.076 1907549.93 1828824.485

3747944.945 kJ/h 1041.09Total

Total

QQ kW

= + +

= =

6.2.2 Reactor

25 C

*

=

=(100 kmol/h * 97.8 kJ/kmolK + 419.22 kmol/h * 87.660 kJ/kmolK +477.6528

kmol/h *29.092 kJ/kmolK + 126.971 kmol/h * 29.216 kJ/kmolK) *(250-25)

=14430214 kJ/h

R-101

8 9 T8=250o

T9=330o

: 100 kmol/h

: W kmol/h

Air : 604.62 kmol/h

(0.79 N2, 0.21 O2)

: 33 kmol/h

: 46 kmol/h

: 13.11 kmol/h

: 20.677 kmol/h

: W+80.78 kmol/h

: 29.3 kmol/h

: 477.65 kmol/h

Page 22: 38621213 Project I Acrolein Production

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*

=

= (33 kmol/h * 108 kJ/kmolK + 47 kmol/h * 104 kj/kmolK + 13.11 kmol/h * 124 kj/kmolK +20.677 kmol/h * 47.3 kj/kmolK + 500 kmol/h * 135.576 kJ/kmolK + 29.301 kmol/h * 32.096 kj/kmolK + 477.65 kmol/h * 30.1 kJ/kmolK) * (330-25)

= 28719143 kJ/h

* + * + * *

Standart enthalpy of formations for each species shown in Table 2. (

=(-81800 -393510) - 20230

= -343844 kJ/kmol

By following the same way ;

-1582358 kJ/kmol

-274110 kJ/kmol

-1926202 kJ/kmol

-343844 kJ/kmol

-1582358 kJ/kmol

-274110 kJ/kmol

-1926202 kJ/kmol

Page 23: 38621213 Project I Acrolein Production

- 20 -

* + * + * *

=65.55* 343844 kJ/kmol +5.44 * -1582358 kJ/kmol +13.11* 274110 kJ/kmol +1.45 *-1926202 kJ/kmol

= -37533577 kJ/h

28719143 kJ/h-14430214 kJ/h+(-37533577 kJ/h)

-23244648 kj/h

6.2.3 Quench Cooler

Que

nch

Coo

ler

11

9

12

13

Q-101

T11=25oC T12=50oC

T9=330oC

T13=50oC

: M kmol/h : 0,94 kmol/h : 10,488 kmol/h

: 0.99M+495 kmol/h

: 33 kmol/h : 47 kmol/h : 13.11 kmol/h

: 500 kmol/h : 20.677 kmol/h

: 29.3 kmol/h : 477.65 kmol/h

: 33 kmol/h : 47 kmol/h : 13.11 kmol/h

: 0.01M+5 kmol/h : 20.677 kmol/h

: 29.3 kmol/h : 477.65 kmol/h

Page 24: 38621213 Project I Acrolein Production

- 21 -

0 C

= 1.95*106

= 1.127*10

+ 3724.875M kJ/h

6

= 1890M kJ/h

+ 37.625M kJ/h

= 3.107*107

M = 14880.425 kmol/h

kJ/h

• M is inlet cold water in Quench Cooler.

( ) ( )( ) ( )

12 13 9 11

6 6

6

6

1.95*10 14880.425*3724.874 1.127*10 14880.425*37.625

31.07*10 14880.425*1890

2.1*10 577.61

Total

Total

Total

Q Q Q Q Q

Q

kJQ kWh

= + − −

= + + +

− −

= − = −

Page 25: 38621213 Project I Acrolein Production

- 22 -

6.2.4 Acrolein Absorber

o14T =25 C

2H O 9900 kmol/hn =

25 C

∆H=

*

T13=50o C

T16=50o C 3 6

3 4

3 4 2

2

2

2

2

H O

33 kmol/h

46.06 kmol/h

2.622 kmol/h

20.67 kmol/h

152.6042 kmol/h

29.301 kmol/h

477.6528 kmol/h

C H

C H O

C H O

CO

O

N

n

n

n

n

n

n

n

=

=

=

=

=

=

=

3 6

3 4

2

2

2

33 kmol/h

3.36238 kmol/h

29.301 kmol/h

477.6528 kmol/h

20.67 kmol/h

C H

C H O

O

N

CO

n

n

n

n

n

=

=

=

=

=

3 4

3 4 2

2H O

42.69762 kmol/h

2.622 kmol/h

10052.6 kmol/h

C H O

C H O

n

n

n

=

=

=

T-101

15 T15=50o C

14

16

13

Page 26: 38621213 Project I Acrolein Production

- 23 -

6.2.5 Water Distillation Tower

25 C

∆H=

*

17

18

19

C3H4O : 43.63 kmol/h

C3H4O2 : 13.11 kmol/h

O2 : 29.301 kmol/h

C3H4O : 0.436 kmol/h

C3H4O2 : 13.11 kmol/h

H2O : 25132.75 kmol/h

T17=50oC

T19=52oC

T18=100oC

C3H4O : 43.2 kmol/h

H2O : 27.67 kmol/h

Page 27: 38621213 Project I Acrolein Production

- 24 -

6.2.6 Acrolein Distillation Tower

25 C

∆H=

*

( )Re . . . .

3

3

1041.09 6456.85 577.61 5175 39.77*10 13.9

51.88*10

system Preheater actor Q Cooler Acr Abs Water Dist Acr Dist

system

system

Q = Q Q Q Q Q Q

Q =

Q = kW

+ + + + +

+ + − + + +

19

21

20

T-103

: 43.2 kmol/h

: 27.67 kmol/h

T19=52o C

: 0.216 kmol/h

: 26.81kmol/h

T20=48oC

T21=82o C

: 42.98 kmol/h

: 0.86 kmol/h


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