10万吨 /年轻汽油醚化工业反应器设计The Design of Etherification Reactor for FCC Light Gasoline

Reporter:

Supervisor:

Wenjun Lv

Feng Xin

2012/09/25

Contents

1. The Flow Chart and Design Task

2. The Design of Reactor

3. The Selection of Process Condition

4. The Next Plans

2012/09/25

1.The Flow Chart and Design TaskThe design of adiabatic reactors and control schemeHeat Balance and Mass Balance

FirstReactor

EtherDistillation Second

Reactor

Feed

Pressure:1MPa

Pressure:0.3MPa Pressure:

1MPa

1

2

3

4

56

7

8

9

<=70°C <=70°C

50°C50°C

Product

2012/09/25

2. The Design of ReactorThe composition of light gasoline

Component mass fraction Component mass

fraction Component mass fraction

METHANOL 16.67 3-METHYL-1-BUTENE 0.493 2-METHYL-2-PENTENE 2.953

1-BUTENE 2.368 1-PENTENE 2.008 3-METHYL-1-PENTENE 4.451

CIS-2-BUTENE 1.763 CIS-2-PENTENE 3.532 3-METHYL-CIS-2-PENTENE 1.614

TRANS-2-BUTENE 1.822 TRANS-2-PENTENE 6.126 4-METHYL-CIS-2-PENTENE 0.42

N-BUTANE 0.495 2-METHYL-BUTANE 8.223 3-METHYL-TRANS-2-

PENTENE 2.982

ISOBUTANE 1.029 N-PENTANE 1.702 1-METHYLCYCLOPENTENE 2.417

CYCLOPENTENE 0.92 METHYL-ISOBUTYL-ETHER 0.347 3-METHYLCYCLOPENTENE 0.508

2-METHYL-1,3-BUTADIENE 0.143 1-HEXENE 1.869 2,3-DIMETHYL-BUTANE 1.973

2-PENTYNE 0.388 CIS-2-HEXENE 1.717 N-HEXANE 6.106

CYCLOPENTANE 0.18 TRANS-2-HEXENE 2.033 2-ETHYL-1-PENTENE 2.308

2-METHYL-1-BUTENE 3.67 METHYLCYCLOPE

NTANE 2.548 3-ETHYL-1-PENTENE 1.188

2-METHYL-2-BUTENE 8.462 2-METHYL-1-

PENTENE 7.352

2012/09/25

The rate law and some assumptionsThe intrinsic rate law

Assumptions:① Substitute the ethanol of rate law for C6 for the

methanol of that;② Neglect C7 components;③ Substitute 2M2P for C3M2P , T3M2P and 1MCP.

2012/09/25

The kinetic modelConsider circulation, axial diffusion coefficient at

the base of PFRCirculation

Back mixing

2

2i i

a id c dcD u rdZ dZ

2'

2 20

1a i ii

D d F dFr

Q dZ r dZ

The boundary condition:

00 : i iZ F F : 0i

L

dFZ LdZ

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The solutionInstrument: MATLAB and ASPENThe algorithm for calculation

𝐬𝐭𝐚𝐫𝐭Initial value and

|𝐹 𝑖+1−𝐹 𝑖|<10− 2

Calculate , when . Then

Output and calculate

Calculate z,generate

Output z and conversion

Use Function File (bvp4c.m and bc.m) to calculate

|𝑇 𝑜𝑢𝑡−343.3|<0.15

𝐞𝐧𝐝

𝑧=𝑧+∆ 𝑧

Y

N Y

N

2012/09/25

3.The Selection of Process condition The inlet and outlet temperature and reaction

pressure is fixed Consider the Circulation Ratio (the Circulation

Ratio of First and Second Reactor , and the total Circulation Ratio ) and the methanol/olefin molar ratios (1.05, 1.15, 1.25 and 1.35).

Definition:

The First Reactor

First reactor a

z/m /% b /% b /℃

1.05 2.2 12.3 66.6 66.9 70

1.15 2.2 13.5 67.7 67.9 70

1.25 2.2 14.8 68.7 69 70

1.35 2.2 16.3 69.7 70.1 70

a The diameter of reactor is 1400mm;a The axial diffusion coefficient is 10m2/s;b The conversion is defined as total conversion.

2012/09/25

The second reactor and the processSecond reactor The process

z/m /% /% /℃ /% /%

1.050 9.0 56.4 58.3 67 1 90.3 90.1

1 12.8 64.8 69.7 64.5 0 88.0 89.3

1.150 11.7 62.6 62.5 67 1 91.9 91.1

1 16.58 70.5 73.6 64.5 0 90.3 89.3

1.250 15.1 67.3 67.7 67 1 93.4 92.3

1 22.7 73.1 76.9 64.5 0 90.6 91.2

1.350 20.7 71.1 73.6 67 1 94.6 93.8

1 19.3 72.3 74.6 63.5 0 90.9 90.5

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The length

12.313.5

14.816.3

9

11.7

15.1

20.7

12.8

16.58

22.7

19.3

0

5

10

15

20

25

1.05 1.15 1.25 1.35

the

leng

th z

/m

the methanol/olefin molar ratio nmo

z1(n1=2.2) z2(n2=1; nt=0) z2(n2=0; nt=1)

The selection of process condition Consider the conversion (>90%) and ; Consider the length of reactor; Consider the distillation column, the flow of

distillate is 224kmol/h (=1) and 123.5kmol/h (=1) when =1.15.

FirstReactor

EtherDistillation Second

Reactor

Feed

Pressure:1MPa

Pressure:0.3MPa Pressure:

1MPa

1

2

3

4

56

7

8

9

<=70°C <=70°C

50°C50°C

Product

2012/09/25

4. The next plans

① The heat balance and mass balance

② Control scheme and the treatment of

③ Find the references about data of etherification reactor

④ Find the references about simulation, improve the code and do some further research

THANKS !