-
Notifications
You must be signed in to change notification settings - Fork 4
/
Copy pathHFGP.acmf
1021 lines (881 loc) · 41.2 KB
/
HFGP.acmf
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
69
70
71
72
73
74
75
76
77
78
79
80
81
82
83
84
85
86
87
88
89
90
91
92
93
94
95
96
97
98
99
100
101
102
103
104
105
106
107
108
109
110
111
112
113
114
115
116
117
118
119
120
121
122
123
124
125
126
127
128
129
130
131
132
133
134
135
136
137
138
139
140
141
142
143
144
145
146
147
148
149
150
151
152
153
154
155
156
157
158
159
160
161
162
163
164
165
166
167
168
169
170
171
172
173
174
175
176
177
178
179
180
181
182
183
184
185
186
187
188
189
190
191
192
193
194
195
196
197
198
199
200
201
202
203
204
205
206
207
208
209
210
211
212
213
214
215
216
217
218
219
220
221
222
223
224
225
226
227
228
229
230
231
232
233
234
235
236
237
238
239
240
241
242
243
244
245
246
247
248
249
250
251
252
253
254
255
256
257
258
259
260
261
262
263
264
265
266
267
268
269
270
271
272
273
274
275
276
277
278
279
280
281
282
283
284
285
286
287
288
289
290
291
292
293
294
295
296
297
298
299
300
301
302
303
304
305
306
307
308
309
310
311
312
313
314
315
316
317
318
319
320
321
322
323
324
325
326
327
328
329
330
331
332
333
334
335
336
337
338
339
340
341
342
343
344
345
346
347
348
349
350
351
352
353
354
355
356
357
358
359
360
361
362
363
364
365
366
367
368
369
370
371
372
373
374
375
376
377
378
379
380
381
382
383
384
385
386
387
388
389
390
391
392
393
394
395
396
397
398
399
400
401
402
403
404
405
406
407
408
409
410
411
412
413
414
415
416
417
418
419
420
421
422
423
424
425
426
427
428
429
430
431
432
433
434
435
436
437
438
439
440
441
442
443
444
445
446
447
448
449
450
451
452
453
454
455
456
457
458
459
460
461
462
463
464
465
466
467
468
469
470
471
472
473
474
475
476
477
478
479
480
481
482
483
484
485
486
487
488
489
490
491
492
493
494
495
496
497
498
499
500
501
502
503
504
505
506
507
508
509
510
511
512
513
514
515
516
517
518
519
520
521
522
523
524
525
526
527
528
529
530
531
532
533
534
535
536
537
538
539
540
541
542
543
544
545
546
547
548
549
550
551
552
553
554
555
556
557
558
559
560
561
562
563
564
565
566
567
568
569
570
571
572
573
574
575
576
577
578
579
580
581
582
583
584
585
586
587
588
589
590
591
592
593
594
595
596
597
598
599
600
601
602
603
604
605
606
607
608
609
610
611
612
613
614
615
616
617
618
619
620
621
622
623
624
625
626
627
628
629
630
631
632
633
634
635
636
637
638
639
640
641
642
643
644
645
646
647
648
649
650
651
652
653
654
655
656
657
658
659
660
661
662
663
664
665
666
667
668
669
670
671
672
673
674
675
676
677
678
679
680
681
682
683
684
685
686
687
688
689
690
691
692
693
694
695
696
697
698
699
700
701
702
703
704
705
706
707
708
709
710
711
712
713
714
715
716
717
718
719
720
721
722
723
724
725
726
727
728
729
730
731
732
733
734
735
736
737
738
739
740
741
742
743
744
745
746
747
748
749
750
751
752
753
754
755
756
757
758
759
760
761
762
763
764
765
766
767
768
769
770
771
772
773
774
775
776
777
778
779
780
781
782
783
784
785
786
787
788
789
790
791
792
793
794
795
796
797
798
799
800
801
802
803
804
805
806
807
808
809
810
811
812
813
814
815
816
817
818
819
820
821
822
823
824
825
826
827
828
829
830
831
832
833
834
835
836
837
838
839
840
841
842
843
844
845
846
847
848
849
850
851
852
853
854
855
856
857
858
859
860
861
862
863
864
865
866
867
868
869
870
871
872
873
874
875
876
877
878
879
880
881
882
883
884
885
886
887
888
889
890
891
892
893
894
895
896
897
898
899
900
901
902
903
904
905
906
907
908
909
910
911
912
913
914
915
916
917
918
919
920
921
922
923
924
925
926
927
928
929
930
931
932
933
934
935
936
937
938
939
940
941
942
943
944
945
946
947
948
949
950
951
952
953
954
955
956
957
958
959
960
961
962
963
964
965
966
967
968
969
970
971
972
973
974
975
976
977
978
979
980
981
982
983
984
985
986
987
988
989
990
991
992
993
994
995
996
997
998
999
1000
Version "30.0-0";
Libraries "Modeler.acml", "SystemLibrary.acml";
Parameter IPselector Uses StringParameter
Valid as StringSet (["Initial","Rigorous"]);
Value: "Rigorous";
End
Model HFGPnoS
/* Hollow Fiber Gas Permeation Membrane Model, v0.1.c1 No Sweep
Juan Morinelly (2011)
The syntax below describes a rigorous model for a counter-current hollow fiber asymmetric membrane gas permeation module under
the following assumptions:
• The feed gas enters the shell side of the hollow fiber membrane and permeates to the fiber's bore. The permeate gas outlet is
at the same end as the feed. The gases in the retentate (shell) and permeate (fiber bore) sides flow from one discretized node
to the next in the direction of flow accumulating to form the retentate and permeate outlet streams (Counter-current flow).
• The fibers that make up the bundle are identical, perfectly straight, and uniform diameter, cylindrical hollow tubes. The
feed gas mixture it is evenly distributed throughout a cross section of the fiber bundle. This is also the start point of the
discretized length domain of integration. The end point is at the retentate outlet stream. Radial concentration and flow
gradients in the fiber bundle are neglected (Problem is reduced to one dimension).
• Under the expected operation conditions, the gas mixtures in the module are assumed to behave ideally. The driving force for
gas permeation is the difference of component partial pressure across the dense skin.
• The dense skin layer of the asymmetrical hollow fiber membrane faces the shell side. The molar composition at the boundary of
the dense skin layer and the porous support is equal to the bulk molar composition at the fiber bore. This assumption implies
that there is no flux resistance imposed by the porous support.
• Pressure in the shell is constant. The pressure in fiber bore varies due to constrained flow and can be described by the
Hagen-Poiseuille equation for a compressible fluid.
• Isothermal conditions (No energy balance required).
• Constant permeances: Q.CO2 = 1000 GPU = 0.12047 kmol/hr*m2*bar. Selectivity with respect to CO2: H2O = 0.5, N2 = 50,
O2 = 50.
References
• T.C. Merkel, H. Lin, X. Wei, R. Baker, Power Plant Post-Combustion Carbon Dioxide Capture: An Opportunity for Membranes,
Journal of Membrane Science 359 (2010) 123-139
Modified by Juan Morinelly, September 2012: Initialization procedure variables and equations inclusion
See LICENSE.md for license and copyright details
...Kayode Ajayi (2015)
// Pressure drop model was included in the shell side of the membrane. It was based on Hagen-Posiellie equation by introducing
hydraulic diameter (Daejun Chang, Joonho MIn, Sehern Oh, Kilo Moon, Effect of Pressure Drop on performance of Hollow membrane model for gas permeation,
Koren J. Chemg. Eng., 15(4), (1998), 396-403.
Li-Hua Cheng, Ping-Chung Wu, Junghui Chen, Modelling and optimisation of hollow fiber DCMD module for desalination, Journal of Membernae Science, 154 (2008),
154-166
*/
//===============================================================================================================================================================
//Global Parameters
R as RealParameter (Description:"Universal gas constant ((bar*m3)/(kmol*K))", 8.314472e-2);
pi as RealParameter (3.14159);
//Membrane Parameters
Dfi as Length (Description:"Inner fiber diameter (m)", 0.0004, Fixed);
Dfo as Length (Description:"Outter fiber diameter (m)", 0.0006, Fixed);
L as Length (Description:"Effective fiver length (m)", 1.0, Fixed);
nf as Notype (Description:"Number of fibers in the module");
A as Notype (Description:"Total membrane area required (m2)", 1.0e6);
theta as Fraction (Description:"Overall stage cut, permeate to feed ratio");
Qcd as Notype (Description:"Permeance of carbon dioxide across the membrane (kmol/(m2*hr*bar))", 0.12047, Fixed);
alpha(ComponentList) as Notype (Description:"Membrane selectivity of gas with respect to carbon dioxide (Qcd/Qgas)", Fixed);
dPper as Press_Drop (Description:"Pressure drop in the permeate side due to capillary flow in the permeate side (bar)");
CCfct as Fraction (Description:"Percentage of carbon dioxide in the feed (mol basis) that permeates", Fixed);
Rhoret as Dens_Mol (Description:"Retentate outlet stream molar density (kmol/m3)");
Rhoper as Dens_Mol (Description:"Permeate outlet stream molar density (kmol/m3)");
D_e as length (Description: "Hydraulic diameter of shell(m)");
phi as Notype (Description: "packing density", 0.8,Fixed);
ds as length (Description: "Inside diameter of shell (m)");
SA as Area (Description: "cross sectional flow area of shell side (m2)");
//Initialization Procedure Parameters
IPselectA as IPselector (Description:"Permeate side flow IP selector");
IPselectB as IPselector (DEscription:"Permeate side pressure drop IP selector");
IPselectC as IPselector (DEscription:"Shell side pressure drop IP selector");
//Component Properties
m as RealParameter (1/Size(ComponentList));
//Domain of Integration
k as RealParameter (Description:"Number of integration steps", 20);
Axial as LengthDomain (Length: L, DiscretizationMethod: "CFD2", NumSections: 1, SpacingPreference: L/k, Description: "Axis of fiber bundle");
//Ports
Feed as Input MoleFractionPort;
Retentate as Output MoleFractionPort;
Permeate as Output MoleFractionPort;
//Distributed Variables
Fret as Distribution1D (XDomain is Axial, Description:"Feed side molar flow rate (kmol/hr)", 0.9*Feed.F) of Flow_Mol;
Fper as Distribution1D (XDomain is Axial, Description:"Permeate side molar flow rate (kmol/hr)", 0.1*Feed.F) of Flow_Mol;
Zret(ComponentList) as Distribution1D (XDomain is Axial, Description:"Shell side molar composition", m) of Molefraction;
Zflu(ComponentList) as Distribution1D (XDomain is Axial, Description:"J/Jt", m) of Notype;
Zper(ComponentList) as Distribution1D (XDomain is Axial, Description:"Fiber bore side molar composition", m) of Molefraction;
J(ComponentList) as Distribution1D (XDomain is Axial, Description:"Species molar flow rate accross the membrane (kmol/(hr*m))") of Notype;
Jt as Distribution1D (XDomain is Axial, Description:"Total molar flow rate accross the membrane (kmol/(hr*m))") of Notype;
Pper as Distribution1D (XDomain is Axial, Description:"Pressure in fiber bore, permeate side (bar)") of Pressure;
Pret as Distribution1D (XDomain is Axial, Description:"Pressure in shell side, retentate side (bar)") of Pressure;
Prat as Distribution1D (XDomain is Axial, Description:"Local fiber bore pressure to shell side pressure ratio") of Notype;
nucP as Distribution1D (XDomain is Axial, Description:"Vapor viscosity (cP) (3.6e11 cP = 1 bar*hr)", 1.0e-2) of Visc_Vap;
nu as Distribution1D (XDomain is Axial, Description:"Adjusted units viscosity (bar*hr)", 1.0e-14) of Notype;
rhore as Distribution1D (XDomain is Axial, Description:"shell side(retenate) density(kmol/m3)") of dens_mol_vap;
nuretcP as Distribution1D (XDomain is Axial, Description:"Vapor viscosity (cP) (3.6e11 cP = 1 bar*hr)", 1.0e-2) of Visc_Vap;
nuret as Distribution1D (XDomain is Axial, Description:"Adjusted units viscosity (bar*hr)", 1.0e-14) of Notype;
Vret as Distribution1D (XDomain is Axial, Description: "Shell side velocity(m/s)") of velocity;
//===============================================================================================================================================================
//Feed Inlet Boundary Conditions for Distributed Variables
Jt(0) = Sigma(ForEach(comp in ComponentList)J(comp)(0));
Fret(0) = Feed.F;
Fper(0) = Feed.F - Fret(Axial.EndNode);
Prat(0) = Pper(0)/Feed.P;
Call(nucP(0)) = pVisc_Vap(Feed.T,Pper(0),Zper(ComponentList)(0));
nu(0) = nucP(0)/3.6e11;
Pret(0) = Feed.P;
Vret(0) = Fret(0)/(SA*rhore(0)*3600);
Call(rhore(0)) = pDens_mol_vap(Feed.T,Pret(0),Zret(ComponentList)(0));
Call(nuretcP(0)) = pVisc_Vap(Feed.T,Pret(0),Zret(ComponentList)(0));
nuret(0) = nuretcP(0)/3.6e11;
For comp in ComponentList Do
Zret(comp)(0) = Feed.z(comp);
If IPselectA == "Rigorous" Then
alpha(comp)*J(comp)(0) = pi*Dfo*nf*Qcd*Pret(0)*(Zret(comp)(0) - Prat(0)*Zper(comp)(0));
Fper(0)*Zper(comp)(0).ddx = Jt(0)*Zper(comp)(0) - J(comp)(0);
Else
alpha(comp)*J(comp)(0) = pi*Dfo*nf*Qcd*Pret(0)*(Zret(comp)(0) - Prat(0)*Zret(comp)(0));
Zper(comp)(0) = Zret(comp)(0);
EndIf
Zflu(comp)(0) = J(comp)(0)/Jt(0);
EndFor
//Mass Trasport Equations for Distributed Variables in Domain of Integration
For x in [Axial.Interior + Axial.EndNode] Do
Jt(x) = Sigma(ForEach(comp in ComponentList)J(comp)(x));
Fret(x).ddx = - Jt(x);
Fper(x).ddx = - Jt(x);
If IPselectB == "Rigorous" Then
Pper(x)*(Pper(x).ddx) = 128*R*(Feed.T + 273.15)*nu(x)*Fper(x)/(pi*(Dfi^4)*nf);//Hagen-Poiseuille equation for compressible fluid
Else
Pper(x).ddx = 0;
EndIf
Prat(x) = Pper(x)/Pret(x);
For comp in ComponentList Do
Fret(x)*Zret(comp)(x).ddx = Jt(x)*Zret(comp)(x) - J(comp)(x);
If IPselectA == "Rigorous" Then
alpha(comp)*J(comp)(x) = pi*Dfo*nf*Qcd*Pret(x)*(Zret(comp)(x) - Prat(x)*Zper(comp)(x));
Fper(x)*Zper(comp)(x).ddx = Jt(x)*Zper(comp)(x) - J(comp)(x);
Else
alpha(comp)*J(comp)(x) = pi*Dfo*nf*Qcd*Pret(x)*(Zret(comp)(x) - Prat(x)*Zret(comp)(x));
Zper(comp)(x) = Zret(comp)(x);
EndIf
Zflu(comp)(x) = J(comp)(x)/Jt(x);
Endfor
Call(nucP(x)) = pVisc_Vap(Feed.T,Pper(x),Zper(ComponentList)(x));
nu(x) = nucP(x)/3.6e11;
Endfor
// Hydraulic diameter
d_e = ((Ds^2) - (nf*(dfo^2)))/(ds + (nf*dfo));
//Packing density of module used to calculate the inner diameter of shell
ds = dfo*sqrt(nf/phi);
// Cross sectional flow area for shell side
SA = (pi/4)*(ds^2- nf*(dfo^2));
For x in [Axial.Interior + Axial.EndNode] Do
If IPselectC == "Rigorous" Then
Pret(x).ddx = -8*nuret(x)*3600*Vret(x)/((d_e/2)^2);
Else
Pret(x) = Feed.P;
EndIf
//Fluid velocity in shell side
Vret(x) = Fret(x)/(rhore(x)*SA*3600);
//Fluid properties in shell side
Call(rhore(x)) = pDens_mol_vap(Feed.T,Pret(x),Zret(ComponentList)(x));
Call(nuretcP(x)) = pVisc_Vap(Feed.T,Pret(x),Zret(ComponentList)(x));
nuret(x) = nuretcP(x)/3.6e11;
Endfor
//Module Performance Parameters
A = pi*Dfo*nf*L;
theta = (Feed.F - Retentate.F)/Feed.F;
dPper = Pper(Axial.EndNode) - Pper(0);
CCfct = (Feed.F*Feed.z("CO2") - Retentate.F*Retentate.z("CO2"))/(Feed.F*Feed.z("CO2"));
//===============================================================================================================================================================
//Retentate Outlet Stream Properties
Retentate.F = Fret(Axial.EndNode);
For comp in ComponentList Do
Retentate.z(comp) = Zret(comp)(Axial.EndNode);
EndFor
Retentate.T = Feed.T;
Retentate.P = Pret(Axial.Endnode);
Call(Retentate.h) = pEnth_Mol_Vap(Retentate.T, Retentate.P, Retentate.z);
Call(Rhoret) = pDens_Mol_Vap(Retentate.T, Retentate.P, Retentate.z);
Retentate.V = 1/Rhoret;
//Permeate Outlet Stream Properties
Permeate.F = Fper(0);
For comp in ComponentList Do
Permeate.z(comp) = ZPer(comp)(0);
EndFor
Permeate.T = Feed.T;
Permeate.P = Pper(0);
Call(Permeate.h) = pEnth_Mol_Vap(Permeate.T, Permeate.P, Permeate.z);
Call(Rhoper) = pDens_Mol_Vap(Permeate.T, Permeate.P, Permeate.z);
Permeate.V = 1/Rhoper;
//SYSTEM SECTION - WARNING: DO NOT EDIT
Current_Icon : "System";
TYPE M1_T0 ROLE "ICON" text
Name = Module
lines = 36
sub main
call Path.Begin
call Path.Shift(-2.000000,0.750000)
'' <<Path:0
call Path.Box(0,0,4,-1.5,0,25600,5)
call Path.Line(0,-1.5,4,0,0,5)
'' >>
call Path.End
end sub
sub LabPos
call Label.at(-1.5,0.25)
end sub
sub ports
call Port.name("UniversalIN")
call Port.at(-1.99865,0.00110369)
call Port.direction(0)
call Port.name("UniversalOUT")
call Port.at(1.9993,0.00110369)
call Port.IOtype(1)
call Port.direction(0)
call Port.name("Feed")
call Port.at(-1.99865,0.00110369)
call Port.direction(0)
call Port.name("Permeate")
call Port.at(1.9993,0.00110369)
call Port.IOtype(1)
call Port.direction(0)
call Port.name("Retentate")
call Port.at(-0.0041032,0.750536)
call Port.IOtype(1)
call Port.direction(90)
end sub
endtext
M1_T0_I0 as M1_T0;
SystemData : Text
<FORMLIST DEFAULTFORM="DeviceVariables">
<FORM NAME="DeviceVariables" CLSID="{6BA76840-806B-11D0-BE51-0000C09984EF}">
{ Version : 1
SizeX : 5250
SizeY : 3750
ShowAllVariables : False
ShowAllAttributes : False
ExpandAll : True
ShowRegistryAttributes : True
VariablesPaths : [ alpha(*) CCfct Dfi Dfo L Qcd ]
AttributesPaths : [ Value Spec Units Description ]
ColumnWidths : [ 2265 1215 1215 1200 1230 ]
}
</FORM>
</FORMLIST>
EndText;
TYPE IPsolve ROLE "SCRIPT" TEXT ' Solution script for the HFGPnoS with sequential initialization procedure.
' The script solves the model in incremental steps of complexity by using
' initialization procedure selectors (described below). The selectors are
' switched from an 'Initial' state that selects a set of simplified model
' equations to 'Rigorous' which selects a set of more accurate equations.
' This script is meant to be used on an empty unit once enough variables
' have been specified to satisfy the degrees of freedom.
' For a more complete understanding, please refer to the HFGPnoS model syntax.
' Juan Morinelly, September 2012
' IPselector Description
' ---------------------------------------------
' IPselectA Permeate side mass flow
' IPselectB Permeate side pressure drop
' IPselectC Shell side pressure drop
IPselectA.value = "Initial"
IPselectB.value = "Initial"
IPselectC.value = "Initial"
Simulation.Run(True)
IPselectA.value = "Rigorous"
Simulation.Run(True)
IPselectB.value = "Rigorous"
Simulation.Run(True)
IPselectC.value = "Rigorous"
Simulation.Run(True)
ENDTEXT
//SYSTEM SECTION END
End
Model HFGPw_S
/* Hollow Fiber Gas Permeation Membrane Model, v0.1.c1 With Sweep
Juan Morinelly (2011)
The syntax below describes a rigorous model for a counter-current hollow fiber asymmetric membrane gas permeation module under
the following assumptions:
• The feed gas enters the shell side of the hollow fiber membrane and permeates to the fiber's bore. The sweep gas (for M2 only)
enters the fiber bore side at the opposite end from the feed. The gases in the retentate (shell) and permeate (fiber bore)
sides flow from one discretized node to the next in the direction of flow accumulating to form the retentate and permeate
outlet streams (Counter-current flow).
• The fibers that make up the bundle are identical, perfectly straight, and uniform diameter, cylindrical hollow tubes. The
feed gas mixture it is evenly distributed throughout a cross section of the fiber bundle. This is also the start point of the
discretized length domain of integration. The end point is at the retentate outlet stream. Radial concentration and flow
gradients in the fiber bundle are neglected (Problem is reduced to one dimension).
• Under the expected operation conditions, the gas mixtures in the module are assumed to behave ideally. The driving force for
gas permeation is the difference of component partial pressure across the dense skin.
• The dense skin layer of the asymmetrical hollow fiber membrane faces the shell side. The molar composition at the boundary of
the dense skin layer and the porous support is equal to the bulk molar composition at the fiber bore. This assumption implies
that there is no flux resistance imposed by the porous support.
• Pressure in the shell is constant. The pressure in fiber bore varies due to constrained flow and can be described by the
Hagen-Poiseuille equation for a compressible fluid.
• Isothermal conditions (No energy balance required).
• Constant permeances: Q.CO2 = 1000 GPU = 0.12047 kmol/hr*m2*bar. Selectivity with respect to CO2: H2O = 0.5, N2 = 50,
O2 = 50.
• Oxigen depletion (ODfct) is defined for a system where there is one mol of air sweep available for every mol of feed. See
the README document attached for the details of the equation development.
References
• T.C. Merkel, H. Lin, X. Wei, R. Baker, Power Plant Post-Combustion Carbon Dioxide Capture: An Opportunity for Membranes,
Journal of Membrane Science 359 (2010) 123-139
Modified by Juan Morinelly, September 2012: Initialization procedure variables and equations inclusion
Modified by Kayode Ajayi (2015)
// Pressure drop model was included in the shell side of the membrane. It was based on Hagen-Posiellie equation by introducing
hydraulic diameter (Daejun Chang, Joonho MIn, Sehern Oh, Kilo Moon, Effect of Pressure Drop on performance of Hollow membrane model for gas permeation,
Koren J. Chemg. Eng., 15(4), (1998), 396-403.
Li-Hua Cheng, Ping-Chung Wu, Junghui Chen, Modelling and optimisation of hollow fiber DCMD module for desalination, Journal of Membernae Science, 154 (2008),
154-166
See LICENSE.md for license and copyright details.
*/
//===============================================================================================================================================================
//Global Parameters
R as RealParameter (Description:"Universal gas constant ((bar*m3)/(kmol*K))", 8.314472e-2);
pi as RealParameter (3.14159);
//Membrane Parameters
Dfi as Length (Description:"Inner fiber diameter (m)", 0.0004, Fixed);
Dfo as Length (Description:"Outter fiber diameter (m)", 0.0006, Fixed);
L as Length (Description:"Effective fiver length (m)", 1.0, Fixed);
nf as Notype (Description:"Number of fibers in the module");
A as Notype (Description:"Total membrane area required (m2)", 1.0e6);
theta as Fraction (Description:"Overall stage cut, permeate to feed ratio");
Qcd as Notype (Description:"Permeance of carbon dioxide across the membrane (kmol/(m2*hr*bar))", 0.12047, Fixed);
alpha(ComponentList) as Notype (Description:"Membrane selectivity of gas with respect to carbon dioxide (Qcd/Qgas)", Fixed);
dPper as Press_Drop (Description:"Pressure drop in the permeate side due to capillary flow in the permeate side (bar)");
CCfct as Fraction (Description:"Percentage of carbon dioxide in the feed (mol basis) that permeates", Fixed);
ODfct as Notype (Description:"Percentage of oxygen depleted from the sweep (mol basis) due to reverse permeation");
Rhoret as Dens_Mol (Description:"Retentate outlet stream molar density (kmol/m3)");
Rhoper as Dens_Mol (Description:"Permeate outlet stream molar density (kmol/m3)");
D_e as length (Description: "Hydraulic diameter of shell(m)");
phi as Notype (Description: "packing density", 0.8,Fixed);
ds as length (Description: "Inside diameter of shell (m)");
SA as Area (Description: "cross sectional flow area of shell side (m2)");
//Initialization Procedure Parameters
IPselectA as IPselector (Description:"Permeate side flow IP selector");
IPselectB as IPselector (DEscription:"Permeate side pressure drop IP selector");
IPselectC as IPselector (DEscription:"Shell side pressure drop IP selector");
//Component Properties
m as RealParameter (1/Size(ComponentList));
//Domain of Integration
k as RealParameter (Description:"Number of integration steps", 20);
Axial as LengthDomain (Length: L, DiscretizationMethod: "CFD2", NumSections: 1, SpacingPreference: L/k, Description: "Axis of fiber bundle");
//Ports
Feed as Input MoleFractionPort;
Sweep as Input MoleFractionPort;
Retentate as Output MoleFractionPort;
Permeate as Output MoleFractionPort;
//Distributed Variables
Fret as Distribution1D (XDomain is Axial, Description:"Feed side molar flow rate (kmol/hr)", 0.9*Feed.F) of Flow_Mol;
Fper as Distribution1D (XDomain is Axial, Description:"Permeate side molar flow rate (kmol/hr)", 0.1*Feed.F) of Flow_Mol;
Zret(ComponentList) as Distribution1D (XDomain is Axial, Description:"Shell side molar composition", m) of Molefraction;
Zflu(ComponentList) as Distribution1D (XDomain is Axial, Description:"J/Jt", m) of Notype;
Zper(ComponentList) as Distribution1D (XDomain is Axial, Description:"Fiber bore side molar composition", m) of Molefraction;
J(ComponentList) as Distribution1D (XDomain is Axial, Description:"Species molar flow rate accross the membrane (kmol/(hr*m))") of Notype;
Jt as Distribution1D (XDomain is Axial, Description:"Total molar flow rate accross the membrane (kmol/(hr*m))") of Notype;
Pper as Distribution1D (XDomain is Axial, Description:"Pressure in fiber bore, permeate side (bar)") of Pressure;
Pret as Distribution1D (XDomain is Axial, Description:"Pressure in shell side, retentate side (bar)") of Pressure;
Prat as Distribution1D (XDomain is Axial, Description:"Local fiber bore pressure to shell side pressure ratio") of Notype;
nucP as Distribution1D (XDomain is Axial, Description:"Vapor viscosity (cP) (3.6e11 cP = 1 bar*hr)", 1.0e-2) of Visc_Vap;
nu as Distribution1D (XDomain is Axial, Description:"Adjusted units viscosity (bar*hr)", 1.0e-14) of Notype;
rhore as Distribution1D (XDomain is Axial, Description:"shell side(retenate) density(kmol/m3)") of dens_mol_vap;
nuretcP as Distribution1D (XDomain is Axial, Description:"Vapor viscosity (cP) (3.6e11 cP = 1 bar*hr)", 1.0e-2) of Visc_Vap;
nuret as Distribution1D (XDomain is Axial, Description:"Adjusted units viscosity (bar*hr)", 1.0e-14) of Notype;
Vret as Distribution1D (XDomain is Axial, Description: "Shell side velocity(m/s)") of velocity;
//===============================================================================================================================================================
//Feed Inlet Boundary Conditions for Distributed Variables
Jt(0) = Sigma(ForEach(comp in ComponentList)J(comp)(0));
Fret(0) = Feed.F;
Fper(0).ddx = - Jt(0);
Prat(0) = Pper(0)/Pret(0);
Call(nucP(0)) = pVisc_Vap(Feed.T,Pper(0),Zper(ComponentList)(0));
nu(0) = nucP(0)/3.6e11;
Pret(0) = Feed.P;
Vret(0) = Fret(0)/(SA*rhore(0)*3600);
Call(rhore(0)) = pDens_mol_vap(Feed.T,Pret(0),Zret(ComponentList)(0));
Call(nuretcP(0)) = pVisc_Vap(Feed.T,Pret(0),Zret(ComponentList)(0));
nuret(0) = nuretcP(0)/3.6e11;
If IPselectB == "Rigorous" Then
Pper(0)*(Pper(0).ddx) = 128*R*(Feed.T + 273.15)*nu(0)*Fper(0)/(pi*(Dfi^4)*nf);//Hagen-Poiseuille equation for compressible fluid
Else
Pper(0).ddx = 0;
EndIf
For comp in ComponentList Do
Zret(comp)(0) = Feed.z(comp);
If IPselectA == "Rigorous" Then
alpha(comp)*J(comp)(0) = pi*Dfo*nf*Qcd*Pret(0)*(Zret(comp)(0) - Prat(0)*Zper(comp)(0));
Fper(0)*Zper(comp)(0).ddx = Jt(0)*Zper(comp)(0) - J(comp)(0);
Else
alpha(comp)*J(comp)(0) = pi*Dfo*nf*Qcd*Pret(0)*(Zret(comp)(0) - Prat(0)*Zret(comp)(0));
Zper(comp)(0) = Zret(comp)(0);
EndIf
Zflu(comp)(0) = J(comp)(0)/Jt(0);
EndFor
//Sweep Inlet Boundary Conditions for Distributed Variables
Jt(Axial.EndNode) = Sigma(ForEach(comp in ComponentList)J(comp)(Axial.Endnode));
Fret(Axial.EndNode).ddx = - Jt(Axial.EndNode);
Fper(Axial.EndNode) = Sweep.F;
Prat(Axial.EndNode) = Pper(Axial.EndNode)/Pret(Axial.Endnode);
Call(nucP(Axial.EndNode)) = pVisc_Vap(Feed.T,Pper(Axial.EndNode),Zper(ComponentList)(Axial.EndNode));
nu(Axial.EndNode) = nucP(Axial.EndNode)/3.6e11;
Pper(Axial.EndNode) = Sweep.P;
For comp in ComponentList Do
Fret(Axial.EndNode)*Zret(comp)(Axial.EndNode).ddx = Jt(Axial.EndNode)*Zret(comp)(Axial.EndNode) - J(comp)(Axial.EndNode);
If IPselectA == "Rigorous" Then
alpha(comp)*J(comp)(Axial.EndNode) = pi*Dfo*nf*Qcd*Pret(Axial.Endnode)*(Zret(comp)(Axial.EndNode) - Prat(Axial.EndNode)*Zper(comp)(Axial.EndNode));
Else
alpha(comp)*J(comp)(Axial.EndNode) = pi*Dfo*nf*Qcd*Pret(Axial.Endnode)*(Zret(comp)(Axial.EndNode) - Prat(Axial.EndNode)*Zret(comp)(Axial.EndNode));
EndIf
Zflu(comp)(Axial.EndNode) = J(comp)(Axial.EndNode)/Jt(Axial.EndNode);
Zper(comp)(Axial.EndNode) = Sweep.z(comp);
EndFor
//Mass Trasport Equations for Distributed Variables in Domain of Integration
For x in [Axial.Interior] Do
Jt(x) = Sigma(ForEach(comp in ComponentList)J(comp)(x));
Fret(x).ddx = - Jt(x);
Fper(x).ddx = - Jt(x);
If IPselectB == "Rigorous" Then
Pper(x)*(Pper(x).ddx) = 128*R*(Feed.T + 273.15)*nu(x)*Fper(x)/(pi*(Dfi^4)*nf);//Hagen-Poiseuille equation for compressible fluid
Else
Pper(x) = 1.01325;
EndIf
Prat(x) = Pper(x)/Pret(x);
Call(nucP(x)) = pVisc_Vap(Feed.T,Pper(x),Zper(ComponentList)(x));
nu(x) = nucP(x)/3.6e11;
For comp in ComponentList Do
Fret(x)*Zret(comp)(x).ddx = Jt(x)*Zret(comp)(x) - J(comp)(x);
If IPselectA == "Rigorous" Then
alpha(comp)*J(comp)(x) = pi*Dfo*nf*Qcd*Pret(x)*(Zret(comp)(x) - Prat(x)*Zper(comp)(x));
Fper(x)*Zper(comp)(x).ddx = Jt(x)*Zper(comp)(x) - J(comp)(x);
Else
alpha(comp)*J(comp)(x) = pi*Dfo*nf*Qcd*Pret(x)*(Zret(comp)(x) - Prat(x)*Zret(comp)(x));
Zper(comp)(x) = Zret(comp)(x);
EndIf
Zflu(comp)(x) = J(comp)(x)/Jt(x);
Endfor
Endfor
//Hydraulic diameter
d_e = ((Ds^2) - (nf*(dfo^2)))/(ds + (nf*dfo));
//Packing density of the module used to calculate inside diameter of shell
ds = dfo*sqrt(nf/phi);
//Cross sectional flow area for shell side
SA = (3.142/4)*(ds^2- nf*(dfo^2));
//Shell side Pressure drop calculation
For x in [Axial.Interior + Axial.EndNode] Do
If IPselectC == "Rigorous" Then
Pret(x).ddx = -8*nuret(x)*3600*Vret(x)/((d_e/2)^2);
Else
Pret(x) = Feed.P;
EndIf
//Fluid velocity in shell side
Vret(x) = Fret(x)/(rhore(x)*SA*3600);
//Fluid properties in shell side
Call(rhore(x)) = pDens_mol_vap(Feed.T,Pret(x),Zret(ComponentList)(x));
Call(nuretcP(x)) = pVisc_Vap(Feed.T,Pret(x),Zret(ComponentList)(x));
nuret(x) = nuretcP(x)/3.6e11;
Endfor
//Module Performance Parameters
A = pi*Dfo*nf*L;
theta = (Feed.F - Retentate.F)/Feed.F;
dPper = Pper(Axial.EndNode) - Pper(0);
CCfct = (Feed.F*Feed.z("CO2") - Retentate.F*Retentate.z("CO2"))/(Feed.F*Feed.z("CO2"));
ODfct = (Sweep.F*Sweep.z("O2") - Permeate.F*Permeate.z("O2"))/(Sweep.F*Sweep.z("O2"));
//===============================================================================================================================================================
//Retentate Outlet Stream Properties
Retentate.F = Fret(Axial.EndNode);
For comp in ComponentList Do
Retentate.z(comp) = Zret(comp)(Axial.EndNode);
EndFor
Retentate.T = Feed.T;
Retentate.P = Pret(Axial.Endnode);
Call(Retentate.h) = pEnth_Mol_Vap(Retentate.T, Retentate.P, Retentate.z);
Call(Rhoret) = pDens_Mol_Vap(Retentate.T, Retentate.P, Retentate.z);
Retentate.v = 1/Rhoret;
//Permeate Outlet Stream Properties
Permeate.F = Fper(0);
For comp in ComponentList Do
Permeate.z(comp) = ZPer(comp)(0);
EndFor
Permeate.T = Feed.T;
Permeate.P = Pper(0);
Call(Permeate.h) = pEnth_Mol_Vap(Permeate.T, Permeate.P, Permeate.z);
Call(Rhoper) = pDens_Mol_Vap(Permeate.T, Permeate.P, Permeate.z);
Permeate.v = 1/Rhoper;
//SYSTEM SECTION - WARNING: DO NOT EDIT
Current_Icon : "System";
TYPE M2_T0 ROLE "ICON" text
Name = Module
lines = 39
sub main
call Path.Begin
call Path.Shift(-2.000000,0.750000)
'' <<Path:0
call Path.Box(0,0,4,-1.5,0,25600,5)
call Path.Line(0,-1.5,4,0,0,5)
'' >>
call Path.End
end sub
sub LabPos
call Label.at(-1.5,0.25)
end sub
sub ports
call Port.name("Feed")
call Port.at(-2.00027,-0.000814975)
call Port.direction(0)
call Port.name("Sweep")
call Port.at(-0.00211499,-0.749594)
call Port.direction(90)
call Port.name("Permeate")
call Port.at(1.99991,-0.000814975)
call Port.IOtype(1)
call Port.direction(0)
call Port.name("Retentate")
call Port.at(-0.00211499,0.75132)
call Port.IOtype(1)
call Port.direction(90)
call Port.name("UniversalIN")
call Port.at(-2.00027,-0.000814975)
call Port.direction(0)
call Port.name("UniversalOUT")
call Port.at(1.99991,-0.000814975)
call Port.IOtype(1)
call Port.direction(0)
end sub
endtext
M2_T0_I0 as M2_T0;
SystemData : Text
<FORMLIST DEFAULTFORM="DeviceVariables">
<FORM NAME="DeviceVariables" CLSID="{6BA76840-806B-11D0-BE51-0000C09984EF}">
{ Version : 1
SizeX : 5250
SizeY : 3750
ShowAllVariables : False
ShowAllAttributes : False
ExpandAll : True
ShowRegistryAttributes : True
VariablesPaths : [ alpha(*) CCfct Dfi Dfo L Qcd ]
AttributesPaths : [ Value Spec Units Description ]
ColumnWidths : [ 2265 1215 1215 1200 1230 ]
}
</FORM>
</FORMLIST>
EndText;
TYPE IPsolve ROLE "SCRIPT" TEXT ' Solution script for the HFGPw_S with sequential initialization procedure.
' The script solves the model in incremental steps of complexity by using
' initialization procedure selectors (described below). The selectors are
' switched from an 'Initial' state that selects a set of simplified model
' equations to 'Rigorous' which selects a set of more accurate equations.
' This script is meant to be used on an empty unit once enough variables
' have been specified to satisfy the degrees of freedom.
' For a more complete understanding, please refer to the HFGPnoS model syntax.
' Juan Morinelly, September 2012
' IPselector Description
' ---------------------------------------------
' IPselectA Permeate side mass flow
' IPselectB Permeate side pressure drop
' IPselectC Shell side pressure drop
IPselectA.value = "Initial"
IPselectB.value = "Initial"
IPselectC.value = "Initial"
Simulation.Run(True)
IPselectA.value = "Rigorous"
Simulation.Run(True)
IPselectB.value = "Rigorous"
Simulation.Run(True)
IPselectCvalue = "Rigorous"
Simulation.Run(True)
ENDTEXT
//SYSTEM SECTION END
End
SystemData : Text
globaldatasection
EndText;
SystemData : Text
<FORMLIST DEFAULTFORM="AllGlobals">
<FORM NAME="AllGlobals" CLSID="{6BA76840-806B-11D0-BE51-0000C09984EF}">
{ Version : 1
SizeX : 5250
SizeY : 3750
ShowAllVariables : True
ShowAllAttributes : False
ExpandAll : True
ShowRegistryAttributes : True
VariablesPaths : [ ]
AttributesPaths : [ Value Spec Units Description ]
ColumnWidths : [ 2265 1215 1215 1200 2925 ]
}
</FORM>
</FORMLIST>
EndText;
FLOWSHEET
CONSTRAINTS
// Flowsheet variables and equations...
END
//SYSTEM SECTION - WARNING: DO NOT EDIT
SystemData : Text
<FORMLIST DEFAULTFORM="AllVariables">
</FORMLIST>
EndText;
//SYSTEM SECTION END
ActiveTasks : [];
Graphics : TEXT CLSID {A0DFFFE6-908E-11CE-A964-0000C08C668E}
# of PFS Objects = 1
SIZE -5.34665 -1.62243 -0.330884 1.68524
LEGEND
Version: 2
Dim: -3.78265 -3.2 -2.84936 -3.39176
Size: 0.0110172
Font: 1 0 =Times New Roman
# of PFS Objects = 0
VIEWPORT -7.366420 10.944214 2.491439 -7.391015
LAYOUT
TableFormat 1
Pages 1 1 1 1
PAGESETUP
PAPERSIZE
PAPERSOURCE
ORIENTATION -1
PRINTPAGENO 1 1
LEFTMARGIN 0.5"
RIGHTMARGIN 0.5"
TOPMARGIN 0.5"
BOTTOMMARGIN 0.5"
VISIBILITY 0.030000
PFDFLAG 255 255
PFDMODE 0
SCALE 0.011017
ENDTEXT;
END
Properties
Package : "Aprpdf";
WorkingDirectory : "C:\Users\mzamarripa\Documents\Superstructure_project\Membrane_CO2capture\membr_proj\AM_MEMCAP\";
RunID : "propsplus.aprpdf";
Default as ComponentList;
Within Default
Components :["CO2","H2O","N2","O2"];
EndWithin
End
Options
AbsoluteSingularityTol: 1.e-004;
AbsPerturb: 1.e-005;
AbsTearTol: 1.e-005;
AbsTol: 1.e-005;
AssignmentWarningsEnabled: True;
ChangeTol: 1.e-005;
CheckProcDerivs: "Off";
Compression: True;
CurrentUOMSet: "Metric";
Decomposer.ProgID: "AspenTech.Decomposer";
Decomposition.MultipleGroup: True;
DerivAbsTol: 1.e-003;
DerivRelTol: 0.1;
EqnTol: 1.e-005;
EquationSensCheck: False;
EquationSensTol: 10000000000.;
EstimationPrintLevel: "Medium";
EstimationReturntoBestPoint: False;
EstimationSolver: 2;
Estimator: 1;
ExplicitEventTolerance: 1.e-005;
Feasopt.MaxAbsStep: 10.;
Feasopt.MaxEval: 100;
Feasopt.MaxRelStep: 10.;
Feasopt.OptTol: 1.e-004;
Homotopy.InitialStep: 0.1;
Homotopy.MaximumStep: 1.;
Homotopy.MinimumStep: 1.e-002;
Homotopy.StepDecrement: 0.5;
Homotopy.StepIncrement: 10;
Integration.AbsErrorTol: 1.e-005;
Integration.AbsTearTol: 1.e-005;
Integration.DiscontinuityEventTol: 1.e-005;
Integration.EnforceMinStep: False;
Integration.IncSensErrors: False;
Integration.InitStepSize: 5.e-003;
Integration.ItplToComTime: True;
Integration.LocateIEvents: False;
Integration.MaxOrder: 5;
Integration.MaxStepSize: 1.;
Integration.MinStepSize: 1.e-003;
Integration.ProgID: "AspenTech.UnifiedIntegrator";
Integration.RcvTornVars: False;
Integration.ReInitAfterEE: False;
Integration.ReInitAfterIE: False;
Integration.RelErrorTol: 1.e-005;
Integration.RelTearTol: 1.e-005;
Integration.RewindToLastConvStep: False;
Integration.ShowHIErrors: 0;
Integration.ShowHTIErrors: 0;
Integration.StepRedFact: 0.5;
Integration.StepSize: 1.e-002;
Integration.StepSizeType: "Variable";
Integration.TestSAndAVars: False;
Integration.UsePrevAfterEE: False;
Integrator: "ImplicitEuler";
KeepCompiledEvaluationFiles: False;
LinearSolver: "MA48";
ListEquivalenceVariables: True;
LogLikelihood.MaxIter: 100;
LogLikelihood.SolTol: 1.e-004;
MA48.DropTol: 0.;
MA48.EnableRefineIter: True;
MA48.MaxRefineIter: 10;
MA48.PivotSearch: 3;
MA48.PivotTol: 1.e-050;
MA48.Repivot: 0;
MA48.UseTranspose: 0;
MaxTearIter: 100;
Nl2sol.AbsFuncTol: 1.e-020;
Nl2sol.FalseConvTol: 0.;
Nl2sol.MaxIter: 50;
Nl2sol.RelFuncTol: 1.e-004;
Nl2sol.SolTol: 1.e-004;
NLASolver: "DMO";
Nonlinear.AbsPert: 1.e-005;
Nonlinear.BestOnFail: True;
Nonlinear.BoundClip: 1.e-006;
Nonlinear.BoundFrac: 1.;
Nonlinear.ConvCrit: "Residual";
Nonlinear.CreepIter: 0;
Nonlinear.CreepSize: 0.1;
Nonlinear.Dogleg: False;
Nonlinear.HiResidual: 0;
Nonlinear.HiVarSteps: 0;
Nonlinear.MathsPrint: 0;
Nonlinear.MaxDivSteps: 10;
Nonlinear.MaxFastNewtonSteps: 5;
Nonlinear.MaxIter: 100;
Nonlinear.MaxStepRed: 10;
Nonlinear.MaxVarStep: 50.;
Nonlinear.Method: "Mixed Newton";
Nonlinear.RangeFrac: 0.;
Nonlinear.SingPert: 1.e-002;
OptimizationObjFun: "Minimize";
OptimizationPrintLevel: "Medium";
Optimizer: 1;
PrintLevel: 2;
PropInfo: -1;
RelativeSingularityCheck: True;
RelativeSingularityTol: 1.e-002;
RelPerturb: 1.e-005;
RelTearTol: 1.e-005;
RelTol: 1.e-005;
RunMode: "SteadyState";
SaveFreeVariableValues: True;
Scaling: False;
SensErrorCheck: True;
SnapshotSettings.EnableDynInitialization: True;
SnapshotSettings.EnableFileSaved: False;
SnapshotSettings.EnableInitialization: True;
SnapshotSettings.EnableInitialSpec: True;
SnapshotSettings.EnableMaximum: True;
SnapshotSettings.EnableonReinitialization: False;
SnapshotSettings.EnableProblemEdit: True;
SnapshotSettings.EnableRegularSnapshot: False;
SnapshotSettings.EnableSteadyState: True;
SnapshotSettings.Interval: 2.;
SnapshotSettings.Maximum: 10;
SnapshotSettings.SaveConvergedOnly: True;
SnapshotSettings.TakeAutoSnapshots: True;
SyncSteps: "Full";
Tearing: "update";
TearUpdate: "Direct";
TimeSettings.CommunicationInterval: 1.e-002;
TimeSettings.CommunicationUnits: "Hours";
TimeSettings.DisplayUpdateInterval: 2000;
TimeSettings.EnablePauseAt: False;
TimeSettings.EnableStepFor: False;
TimeSettings.PauseAt: 0.;
TimeSettings.RealTimeSyncFactor: 0.;
TimeSettings.RecordHistory: False;
TimeSettings.StepFor: 0;
TimeSettings.TimeDisplayUnits: "Hours";
UseCompiledEvaluation: False;
UseSavedSnapshotOnLoad: False;
WatchGroup: 0;
WatchSubGroup: 0;
Wegstein.MaxAcceleration: 0.;
Wegstein.MinAcceleration: -5.;
OpenLASolver: "";
OpenNLASolver: "aos_dmo.dll";
OpenNLASolverParameters.ACTIVEINIT: 0;
OpenNLASolverParameters.ACTIVERPT: 0;
OpenNLASolverParameters.ACTIVESAVE: 0;
OpenNLASolverParameters.ACTIVESPACE: 2;
OpenNLASolverParameters.ADCVITER: 100;
OpenNLASolverParameters.ADCVMETH: 0;
OpenNLASolverParameters.ADCVOBJCVG: 1.e-006;
OpenNLASolverParameters.ADCVRESCVG: 1.e-006;
OpenNLASolverParameters.ANALYSISTHRES: 2.;
OpenNLASolverParameters.BOUNDRPT: 1;
OpenNLASolverParameters.BTF: 1;
OpenNLASolverParameters.CREEPFLAG: 0;
OpenNLASolverParameters.CREEPITER: 10;
OpenNLASolverParameters.CREEPSIZE: 0.1;
OpenNLASolverParameters.CWORKF: 1.;
OpenNLASolverParameters.DENSITYRATIO: 0.7;
OpenNLASolverParameters.DROPTOL: 1.e-020;
OpenNLASolverParameters.FACTORSPACE: 6;
OpenNLASolverParameters.FACTORSPEED: 1;
OpenNLASolverParameters.FREEONLY: 0;
OpenNLASolverParameters.HESSIANSCL: 1.;
OpenNLASolverParameters.HESSIANUPDATES: 10;
OpenNLASolverParameters.IPSIRPT: 1;
OpenNLASolverParameters.IWORKF: 1.;
OpenNLASolverParameters.LINESEARCH: 3;
OpenNLASolverParameters.LINESRCMODE: 0;
OpenNLASolverParameters.LSMODEITER: 0;
OpenNLASolverParameters.LUSTATS: 0;
OpenNLASolverParameters.MAXITER: 50;
OpenNLASolverParameters.MINBTFSIZE: 1;
OpenNLASolverParameters.MINITER: 0;
OpenNLASolverParameters.OBJCVG: 1.e-006;
OpenNLASolverParameters.PIVOTANAL: 1;
OpenNLASolverParameters.PIVOTSEARCH: 10;
OpenNLASolverParameters.PIVOTTHRESH: 0.1;
OpenNLASolverParameters.PIVOTZERO: 0.;
OpenNLASolverParameters.PRINTFREQ: -1;
OpenNLASolverParameters.QPCONVTOL: 1.e-010;
OpenNLASolverParameters.QPDEPDIAG: 2;
OpenNLASolverParameters.QPHESSIANUPD: 20;
OpenNLASolverParameters.QPITER: 10;
OpenNLASolverParameters.QPMICROINF: 0;
OpenNLASolverParameters.QPMICROMAX: 5;
OpenNLASolverParameters.QPMICROTOL: 1.e-012;
OpenNLASolverParameters.QPSTATS: 0;
OpenNLASolverParameters.QUICKRTN: 1;
OpenNLASolverParameters.RESCVG: 1.e-006;
OpenNLASolverParameters.RETRYFACT: 1;
OpenNLASolverParameters.RIGORUPDATES: 25;
OpenNLASolverParameters.RWORKF: 1.;
OpenNLASolverParameters.SAVEJDFFILE: 0;
OpenNLASolverParameters.SCREENFORM: 1;
OpenNLASolverParameters.SEARCHMODE: 1;
OpenNLASolverParameters.SINGULARHAND: 0;
OpenNLASolverParameters.TRUSTITER: 2;
OpenNLASolverParameters.TRUSTMODE: 0;
OpenNLASolverParameters.TRUSTRAMPIT: 2;
OpenNLASolverParameters.TRUSTSIZE: 0.1;
OpenNLASolverParameters.USEDROPTOL: 0;
OpenNLASolverParameters.VARSCALE: 1;
OpenNLASolverParameters.VMS_P1: 0;
OpenNLASolverParameters.WORKINGDIR: "C:\Users\mzamarripa\Documents\GitHub\CCSI_work\membrane_model\AM_HFGP";
OpenOPTSolver: "";
OpenESTSolver: "";
End
Optimization
IsDynamic : FALSE;
ElementSizeBoundsAutomatic : TRUE;
EndTime : 1.000000000000000;
Control.FinalTime_Initial : 1.000000000000000;
Control.FinalTime_Upper : 2.000000000000000;
Control.FinalTime_Lower : 0.5000000000000000;
Control.FinalTime_IsFixed : TRUE;
Control.FinalTime_IsObjective : FALSE;
Control.Elements : 5;
Control.FixedInterval : TRUE;
Control.MovingElementsVarying : FALSE;
Control.PiecewiseLinear : FALSE;
Control(0) : 0.2000000000000000, 0.05000000000000000, 0.4000000000000000 ;
Control(1) : 0.2000000000000000, 0.05000000000000000, 0.4000000000000000 ;
Control(2) : 0.2000000000000000, 0.05000000000000000, 0.4000000000000000 ;
Control(3) : 0.2000000000000000, 0.05000000000000000, 0.4000000000000000 ;
Control(4) : 0.2000000000000000, 0.05000000000000000, 0.4000000000000000 ;
End
Estimation
CalcHeteroParams : TRUE;