Modelling, Estimation and Optimization of the Methanol Synthesis With Catalyst Deactivation.

8/11/2019 Modelling, Estimation and Optimization of the Methanol Synthesis With Catalyst Deactivation.

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Methanol Distillation

Methanol Synthesis

Steam Reforming

Autothermal Reforming

Product Methanol

Prereforming

DesuphurizationSteam

Natural Gas

Oxygen

Fuel


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0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 00 00 00 0

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 11 11 11 1

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 00 00 00 0

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 11 11 11 1

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 00 0 00 0 00 0 0

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 11 1 11 1 11 1 1

Synthesis gas

Purge

Crude methanol

MP Steam

MP Steam


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0.0

0.2

0.4

0.6

0.8

1.0

0 10 20 30 40 50 60 70 80 90

Activity

Time [days]

a1 a2


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500

510

520

530

540

0 0.2 0.4 0.6 0.8 1

z[m/m]

I II III

500

510

520

530

540

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

T[K]

z [m/m]

I II III


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0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 00 00 00 0

0 0

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 11 11 11 1

1 1

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 0

0 00 00 00 0

0 0

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 1

1 11 11 11 1

1 1

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 0

0 0 00 0 00 0 00 0 0

0 0 0

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 1

1 1 11 1 11 1 11 1 1

1 1 1

Synthesis gas

Purge

Crude methanol

MP Steam

MP Steam

RE

ACT

OR

HEATEXCH.

SEPARATOR

SPLITTER

COMPRESSORMIXER

Synthesisgas

Crude

methanol

Purge

STEAMPROD.

MP steam


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515

520

525

530

535

300 600 900 1200

Tc

[K]

Time [days]

2000

2200

2400

2600

0 300 600 900 1200

Fme

oh

[ton

/day]

Time [days]


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0

20

40

6080

100

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

r1[mol/kgs]

z [m/m]

480

500

520

540

560

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

Tr,max[K]

z [m/m]


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515

520

525

530

300 600 900 1200

Tc[K]

Time [days]

3.0

4.0

5.0

300 600 900 1200

R

[kmol/kmol]

Time [days]

2300

2350

2400

2450

300 600 900 1200

Fmeoh[ton/day

]

Time [days]

1300

1350

1400

1450

300 600 900 1200

Fsteam[

ton/day]

Time [days]


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1.0000.946

0.891

0.837

0.782

0.728

0.673

0.619

0.564

0.510

0.4550.401

0.4

0.6

0.8

1.0

300 600 900 1200

a(z=0.5

)

Time [days]


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0.30

0.35

0.40

0.45

300 600 900 1200

Xmeoh

Time [days]

10

15

20

25

30

300 600 900 1200

dTeq1[K]

Time [days]

0.64

0.65

0.66

0.670.68

0.69

300 600 900 1200

y_

in(H2)

Time [days]

2100

2200

2300

2400

2500

2600

300 600 900 1200

Fmeoh,r

[ton/day]

Time [days]


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515

520

525

530

300 600 900 1200

Tc[K]

Time [days]

515

520

525

530

300 600 900 1200

Tc[K]

Time [days]


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1.0000.9460.8910.8370.7820.7280.6740.6190.5650.5100.4560.402

0.4

0.6

0.8

1.0

300 600 900 1200

a(z=0.5

)

Time [day]


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0.30

0.35

0.40

300 600 900 1200

Xmeoh

Time [days]

10

20

30

40

300 600 900 1200

dTeq1[K]

Time [days]

515

520

525

530

700 720 740 760 780 800 820

Tc[K]

Time [days]


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515

520

525

530

300 600 900 1200

Tc[K]

Time [days]

1600


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3.0

3.5

4.0

4.5

5.0

300 600 900 1200

R

[kmol/kmol]

Time [days]

2340

2360

2380

2400

300 600 900 1200

Fmeoh[ton/day]

Time [days]

1300

1400

1500

1600

300 600 900 1200

Fsteam[to

n/day]

Time [days]


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0.4820


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10

1 10

10.38

0.4

0.42

0.44

0.46

Kd

Ed

a(x=0.5,t=t l)

10

1 10

116

17

18

19

KdEd

Obj

1

0

1 1

0

10.34

0.36

0.38

0.4

0.42

0.44

0.46

KdEd

a(z=

0.5,t=

t l)

1

0

1 1

0

117

18

19

20

21

22

23

KdEd

Obj


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1 0

11

01

518

520

522

EdKd

Tc(1)[K]

1 0

11

01

522

524

526

EdKd

Tc(2)

[K]

1 0 1

101

525

526

527

EdKd

Tc(3)

[K]

10

1

10.500.51526

528

530

EdKd

Tc(4)[K]

10

1

10.500.51

528

529

530

EdKd

Tc(5)[K]

1 0

1

10

1529

530

531

EdKd

Tc(6)[K]

1

0

1

10.500.5

1530

531

532

EdKd

Tc(7)[K

]

10

1

10.500.51

531

532

533

EdKd

Tc(8)[K

]

0.46


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1 0 1 1

0

1

0.36

0.38

0.4

0.42

0.44

0.46

Kd

a(z=

0.5,t=

t l)

10

1 1

0

1

20

20.5

21

21.5

22

22.5

Kd

Ed

Obj


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0 500 1000 1500520

522

524

526

528

530

532

Time[days]

Tc[K]


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0

10

20

30

40

0 0.5 1z

T-Tin

0[K]

Measured Predicted

MeasuredPredicted


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30

35

40

45

0 100 200 300Time[days]

Tout-Tin0[K]

Measured Predicted

0.7

0.8

0.9

1.0

1.1

1.2

0 100 200 300

Time[days]

FMeOH

/F0MeOH

Measured Predicted

0

5

10

15

20

25

0 200 400Time[days]

Tm

1

-Tin

0[K]

Predicted

25

30

35

40

0 200 400

Time[days]

Tm

2

-Tin

0[K]

30

35

40

45

0 200 400Time[days]

Tm

3

-Tin

0[K]

30

35

40

45

0 200 400

Tm

4

-Tin

0[K]

Time[days]

30

35

40

45

0 200 400

Time[days]

Tm

5

-Tin

0[K]

25

30

35

40

45

0 200 400Time[days]

Tm

6

-Tin

0[K]


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Regular control

Plant

Supervisory control

Optimization layer

minutes

hour/day

seconds

Controllayer

Scheduling weeks


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Modelling, Estimation and Optimization of the Methanol Synthesis With Catalyst Deactivation.

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Transcript of Modelling, Estimation and Optimization of the Methanol Synthesis With Catalyst Deactivation.