source: branches/gui/eml/stage_separators/reboiler.mso @ 806

Last change on this file since 806 was 806, checked in by gerson bicca, 13 years ago

updates

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1#*-------------------------------------------------------------------
2* EMSO Model Library (EML) Copyright (C) 2004 - 2007 ALSOC.
3*
4* This LIBRARY is free software; you can distribute it and/or modify
5* it under the therms of the ALSOC FREE LICENSE as available at
6* http://www.enq.ufrgs.br/alsoc.
7*
8* EMSO Copyright (C) 2004 - 2007 ALSOC, original code
9* from http://www.rps.eng.br Copyright (C) 2002-2004.
10* All rights reserved.
11*
12* EMSO is distributed under the therms of the ALSOC LICENSE as
13* available at http://www.enq.ufrgs.br/alsoc.
14*
15*----------------------------------------------------------------------
16* Author: Paula B. Staudt
17* $Id: reboiler.mso 555 2008-07-18 19:01:13Z rafael $
18*--------------------------------------------------------------------*#
19
20using "streams";
21
22Model reboilerSteady
23
24ATTRIBUTES
25        Pallete         = true;
26        Icon            = "icon/ReboilerSteady";
27        Brief           = "Model of a  Steady State reboiler with no thermodynamics equilibrium - thermosyphon.";
28        Info            =
29"== ASSUMPTIONS ==
30* perfect mixing of both phases;
31* no thermodynamics equilibrium;
32
33== SET ==
34* the pressure drop in the reboiler;
35
36== SPECIFY ==
37* the InletLiquid stream;
38* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model)
39OR the outlet temperature (OutletVapour.T);
40
41== OPTIONAL ==
42* the reboiler model has two control ports
43** TI OutletVapour Temperature Indicator;
44** PI OutletVapour Pressure Indicator;
45";     
46
47PARAMETERS
48        outer PP                as Plugin               (Brief = "External Physical Properties", Type="PP");
49        outer NComp     as Integer              (Brief="Number of Components");
50        Pdrop                   as press_delta  (Brief="Pressure Drop in the reboiler", Symbol = "\Delta P");
51        FlowConstant                    as Real (Brief = "Flow Constant");
52        k                       as Real (Brief = "Flow Constant", Hidden = true, Unit='mol^3/(kg*m^2)');
53
54SET
55
56        k = 1*'mol^3/(kg*m^2)';
57       
58VARIABLES
59        in      InletLiquid     as stream                               (Brief="Liquid inlet stream", PosX=0.345, PosY=1, Symbol="_{inL}");
60        out     OutletVapour    as streamPH                             (Brief="Vapour outlet stream", PosX=0.17, PosY=0, Symbol="_{outV}");
61        in      InletQ                  as power                                (Brief="Heat supplied", PosX=1, PosY=0.08, Symbol="Q_{in}", Protected = true);
62        vV                              as volume_mol                   (Brief="Vapour Molar volume", Protected = true);
63        rhoV                    as dens_mass                    (Brief="Vapour Density", Symbol = "\rho", Protected = true);
64       
65        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=0.44, PosY=0);
66        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=0.35, PosY=0);
67
68EQUATIONS
69
70"Molar Flow Balance"
71        InletLiquid.F = OutletVapour.F;
72
73"Molar Composition Balance"
74        InletLiquid.z = OutletVapour.z;
75       
76"Vapour Volume"
77        vV = PP.VapourVolume(OutletVapour.T, OutletVapour.P, OutletVapour.z);
78       
79"Vapour Density"
80        rhoV = PP.VapourDensity(OutletVapour.T, OutletVapour.P, OutletVapour.z);
81
82"Energy Balance"
83        InletLiquid.F*InletLiquid.h + InletQ = OutletVapour.F*OutletVapour.h;
84       
85"Pressure Drop"
86        OutletVapour.P = InletLiquid.P - Pdrop;
87
88"Temperature indicator"
89        TI * 'K' = OutletVapour.T;
90
91"Pressure indicator"
92        PI * 'atm' = OutletVapour.P;
93       
94"Flow through the reboiler"
95        OutletVapour.F^3 = FlowConstant*k*InletQ;
96
97end
98
99Model thermosyphon
100
101ATTRIBUTES
102        Pallete         = true;
103        Icon            = "icon/Thermosyphon";
104        Brief           = "Model of a  Steady State reboiler thermosyphon.";
105        Info            =
106"== ASSUMPTIONS ==
107* perfect mixing of both phases;
108* no thermodynamics equilibrium;
109
110== SET ==
111* the pressure drop in the reboiler;
112
113== SPECIFY ==
114* the InletLiquid stream;
115* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model)
116OR the outlet temperature (OutletVapour.T);
117
118== OPTIONAL ==
119* the reboiler model has two control ports
120** TI OutletVapour Temperature Indicator;
121** PI OutletVapour Pressure Indicator;
122";     
123
124PARAMETERS
125        outer PP                as Plugin               (Brief = "External Physical Properties", Type="PP");
126        outer NComp     as Integer              (Brief="Number of Components");
127        Pdrop                   as press_delta  (Brief="Pressure Drop in the reboiler", Symbol = "\Delta P");
128        FlowConstant                    as Real (Brief = "Flow Constant");
129        k                       as Real (Brief = "Flow Constant", Hidden = true, Unit='mol^3/(kg*m^2)');
130
131SET
132
133        k = 1*'mol^3/(kg*m^2)';
134       
135VARIABLES
136        in      InletLiquid     as stream                               (Brief="Liquid inlet stream", PosX=0.44, PosY=1, Symbol="_{inL}");
137        out     OutletVapour    as streamPH                             (Brief="Vapour outlet stream", PosX=0, PosY=0.09, Symbol="_{outV}");
138        in      InletQ                  as power                                (Brief="Heat supplied", PosX=1, PosY=0.77, Symbol="Q_{in}", Protected = true);
139       
140        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=1, PosY=0.57);
141        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=1, PosY=0.35);
142
143EQUATIONS
144
145"Molar Flow Balance"
146        InletLiquid.F = OutletVapour.F;
147
148"Molar Composition Balance"
149        InletLiquid.z = OutletVapour.z;
150       
151"Energy Balance"
152        InletLiquid.F*InletLiquid.h + InletQ = OutletVapour.F*OutletVapour.h;
153       
154"Pressure Drop"
155        OutletVapour.P = InletLiquid.P - Pdrop;
156
157"Temperature indicator"
158        TI * 'K' = OutletVapour.T;
159
160"Pressure indicator"
161        PI * 'atm' = OutletVapour.P;
162       
163"Flow through the thermosyphon reboiler"
164        OutletVapour.F^3 = FlowConstant*k*InletQ;
165
166end
167
168Model reboilerSteady_fakeH
169
170        ATTRIBUTES
171        Pallete         = true;
172        Icon            = "icon/ReboilerSteady";
173        Brief           = "Model of a  Steady State reboiler with fake calculation of outlet conditions.";
174        Info            =
175"Model of a  Steady State reboiler with fake calculation of
176vaporisation fraction and output temperature, but with a real
177calculation of the output stream enthalpy.
178";
179       
180PARAMETERS
181        outer PP        as Plugin(Brief = "External Physical Properties", Type="PP");
182        outer NComp as Integer;
183        Pdrop           as press_delta  (Brief="Pressure Drop in the reboiler", Symbol = "\Delta P");
184        FlowConstant                    as Real (Brief = "Flow Constant");
185        k                       as Real (Brief = "Flow Constant", Hidden = true, Unit='mol^3/(kg*m^2)');
186
187SET
188
189        k = 1*'mol^3/(kg*m^2)';
190       
191VARIABLES
192        in      InletLiquid     as stream                               (Brief="Liquid inlet stream", PosX=0.345, PosY=1, Symbol="_{inL}");
193        out     OutletVapour    as stream                               (Brief="Vapour outlet stream", PosX=0.17, PosY=0, Symbol="_{outV}");
194        in      InletQ                  as power                                (Brief="Heat Duty", PosX=1, PosY=0.08, Symbol="Q_{in}", Protected = true);
195
196        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=0.44, PosY=0);
197        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=0.35, PosY=0);
198
199EQUATIONS
200
201"Molar Balance"
202        InletLiquid.F = OutletVapour.F;
203       
204"Composition Balance"
205        InletLiquid.z = OutletVapour.z;
206       
207"Energy Balance"
208        InletLiquid.F*InletLiquid.h + InletQ = OutletVapour.F*OutletVapour.h;
209       
210"Pressure Drop"
211        OutletVapour.P = InletLiquid.P - Pdrop ;
212
213#"Fake Vapourisation Fraction"
214#       OutletVapour.v = 0.6;
215
216"Fake output temperature"
217        OutletVapour.T = (58+273)*'K';
218
219        #OutletVapour.v = PP.VapourFraction(OutletVapour.T, OutletVapour.P, OutletVapour.z);
220        #OutletVapour.h = OutletVapor.v * PP.VapourEnthalpy(OutletVapour.T, OutletVapour.P, OutletVapour.z)
221        #       +  (1-OutletVapor.v) * PP.LiquidEnthalpy(OutletVapour.T, OutletVapour.P, OutletVapour.z)
222
223"Temperature indicator"
224        TI * 'K' = OutletVapour.T;
225
226"Pressure indicator"
227        PI * 'atm' = OutletVapour.P;
228       
229"Flow through the reboiler"
230        OutletVapour.F^3 = FlowConstant*k*InletQ;
231
232end
233
234Model reboilerReact
235        ATTRIBUTES
236        Pallete         = false;
237        Icon            = "icon/Reboiler";
238        Brief           = "Model of a dynamic reboiler with reaction.";
239        Info            =
240"== Assumptions ==
241* perfect mixing of both phases;
242* thermodynamics equilibrium;
243* no liquid entrainment in the vapour stream;
244* the reaction takes place only in the liquid phase.
245       
246== Specify ==
247* the kinetics variables;
248* the inlet stream;
249* the liquid inlet stream;
250* the outlet flows: OutletVapour.F and OutletLiquid.F;
251* the heat supply.
252
253== Initial Conditions ==
254* the reboiler temperature (OutletLiquid.T);
255* the reboiler liquid level (Level);
256* (NoComps - 1) OutletLiquid (OR OutletVapour) compositions.
257";
258       
259PARAMETERS
260        outer PP as Plugin(Type="PP");
261        outer NComp as Integer;
262        Across as area (Brief="Cross Section Area of reboiler");
263        V as volume (Brief="Total volume of reboiler");
264
265        stoic(NComp) as Real(Brief="Stoichiometric matrix");
266        Hr as energy_mol;
267
268        Initial_Level                           as length               (Brief="Initial Level of liquid phase");
269        Initial_Temperature                     as temperature  (Brief="Initial Temperature of Reboiler");
270        Initial_Composition(NComp)      as fraction     (Brief="Initial Liquid Composition");
271       
272VARIABLES
273in      InletLiquid     as stream                       (Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
274out     OutletLiquid as liquid_stream   (Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
275out     OutletVapour as vapour_stream   (Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
276        InletQ  as power                        (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");
277
278        M(NComp)        as mol                  (Brief="Molar Holdup in the tray");
279        ML                      as mol                  (Brief="Molar liquid holdup");
280        MV                      as mol                  (Brief="Molar vapour holdup");
281        E                       as energy               (Brief="Total Energy Holdup on tray");
282        vL                      as volume_mol   (Brief="Liquid Molar Volume");
283        vV                      as volume_mol   (Brief="Vapour Molar volume");
284        Level           as length               (Brief="Level of liquid phase");
285        Vol             as volume;
286        rhoV            as dens_mass;
287        r3                      as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
288        C(NComp)        as conc_mol     (Brief = "Molar concentration", Lower = -1);
289
290INITIAL
291
292        Level                                   = Initial_Level;
293        OutletLiquid.T                          = Initial_Temperature;
294        OutletLiquid.z(1:NComp-1)       = Initial_Composition(1:NComp-1)/sum(Initial_Composition);
295
296EQUATIONS
297"Molar Concentration"
298        OutletLiquid.z = vL * C;
299       
300"Reaction"
301        r3 = exp(-7150*'K'/OutletLiquid.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4)) * 'l/mol/s';
302
303"Component Molar Balance"
304        diff(M)= InletLiquid.F*InletLiquid.z- OutletLiquid.F*OutletLiquid.z - OutletVapour.F*OutletVapour.z + stoic*r3*ML*vL;
305       
306"Energy Balance"
307        diff(E) = InletLiquid.F*InletLiquid.h- OutletLiquid.F*OutletLiquid.h - OutletVapour.F*OutletVapour.h + InletQ + Hr * r3 * vL*ML;
308       
309"Molar Holdup"
310        M = ML*OutletLiquid.z + MV*OutletVapour.z;
311       
312"Energy Holdup"
313        E = ML*OutletLiquid.h + MV*OutletVapour.h - OutletLiquid.P*V;
314       
315"Mol fraction normalisation"
316        sum(OutletLiquid.z)=1.0;
317       
318"Liquid Volume"
319        vL = PP.LiquidVolume(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z);
320
321"Vapour Volume"
322        vV = PP.VapourVolume(OutletVapour.T, OutletVapour.P, OutletVapour.z);   
323
324"Vapour Density"
325        rhoV = PP.VapourDensity(OutletVapour.T, OutletVapour.P, OutletVapour.z);
326       
327"Level of liquid phase"
328        Level = ML*vL/Across;
329
330        Vol = ML*vL;
331       
332"Mechanical Equilibrium"
333        OutletLiquid.P = OutletVapour.P;
334       
335"Thermal Equilibrium"
336        OutletLiquid.T = OutletVapour.T;       
337       
338"Geometry Constraint"
339        V = ML*vL + MV*vV;             
340
341"Chemical Equilibrium"
342        PP.LiquidFugacityCoefficient(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z)*OutletLiquid.z =
343        PP.VapourFugacityCoefficient(OutletVapour.T, OutletVapour.P, OutletVapour.z)*OutletVapour.z;
344
345        sum(OutletLiquid.z)=sum(OutletVapour.z);
346       
347end
348
349Model reboiler
350       
351ATTRIBUTES
352        Pallete = true;
353        Icon    = "icon/Reboiler";
354        Brief   = "Model of a dynamic reboiler - kettle with control.";
355        Info            =
356"== ASSUMPTIONS ==
357
358* perfect mixing of both phases;
359* thermodynamics equilibrium;
360* no liquid entrainment in the vapour stream.
361       
362== SPECIFY ==
363
364* the InletLiquid stream;
365* the outlet flows: OutletVapour.F and OutletLiquid.F;
366* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model).
367
368== OPTIONAL ==
369* the reboiler model has three control ports
370** TI OutletLiquid Temperature Indicator;
371** PI OutletLiquid Pressure Indicator;
372** LI Level Indicator of Reboiler;
373
374== INITIAL CONDITIONS ==
375
376* Initial_Temperature :  the reboiler temperature (OutletLiquid.T);
377* Initial_Level : the reboiler liquid level (Level);
378* Initial_Composition : (NoComps) OutletLiquid compositions.
379";     
380       
381PARAMETERS
382        outer PP                as Plugin       (Brief = "External Physical Properties", Type="PP");
383        outer NComp     as Integer      (Brief="Number of Components");
384        Across                  as area         (Brief="Cross Section Area of reboiler");
385        V                               as volume       (Brief="Total volume of reboiler");
386       
387        Initial_Level                           as length               (Brief="Initial Level of liquid phase");
388        Initial_Temperature                     as temperature  (Brief="Initial Temperature of Reboiler");
389        Initial_Composition(NComp)      as positive     (Brief="Initial Liquid Composition",Lower=1E-6);
390
391VARIABLES
392
393in      InletLiquid     as stream                       (Brief="Liquid inlet stream", PosX=0.17, PosY=1, Symbol="_{in}^{Liquid}");
394out     OutletLiquid    as liquid_stream        (Brief="Liquid outlet stream", PosX=0.53, PosY=1, Symbol="_{out}^{Liquid}");
395out     OutletVapour    as vapour_stream        (Brief="Vapour outlet stream", PosX=0.17, PosY=0, Symbol="_{out}^{Vapour}");
396in      InletQ                  as power                        (Brief="Heat supplied", Protected = true, PosX=1, PosY=0.08, Symbol="Q_{in}");
397
398        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=0.44, PosY=0);
399        out     LI as control_signal    (Brief="Level Indicator of Reboiler", Protected = true, PosX=0.53, PosY=0);
400        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=0.35, PosY=0);
401       
402        M(NComp)        as mol                  (Brief="Molar Holdup in the tray", Protected = true);
403        ML                      as mol                  (Brief="Molar liquid holdup", Protected = true);
404        MV                      as mol                  (Brief="Molar vapour holdup", Protected = true);
405        E                       as energy               (Brief="Total Energy Holdup on tray", Protected = true);
406        vL                      as volume_mol   (Brief="Liquid Molar Volume", Protected = true);
407        vV                      as volume_mol   (Brief="Vapour Molar volume", Protected = true);
408        rhoV            as dens_mass    (Brief="Vapour Density", Protected = true, Symbol="\rho");
409        Level           as length               (Brief="Level of liquid phase", Protected = true);
410        Pdrop           as press_delta  (Brief = "Pressure Drop", DisplayUnit = 'kPa', Symbol ="\Delta P", Protected=true);
411
412INITIAL
413
414"Initial Level"
415        Level   = Initial_Level;
416
417"Initial Temperature"
418        OutletLiquid.T  = Initial_Temperature;
419
420"Initial Composition"
421        OutletLiquid.z(1:NComp-1) = Initial_Composition(1:NComp-1)/sum(Initial_Composition);
422
423EQUATIONS
424
425"Component Molar Balance"
426        diff(M)= InletLiquid.F*InletLiquid.z    - OutletLiquid.F*OutletLiquid.z - OutletVapour.F*OutletVapour.z;
427
428"Energy Balance"
429        diff(E) = InletLiquid.F*InletLiquid.h   - OutletLiquid.F*OutletLiquid.h - OutletVapour.F*OutletVapour.h + InletQ;
430
431"Molar Holdup"
432        M = ML*OutletLiquid.z + MV*OutletVapour.z;
433
434"Energy Holdup"
435        E = ML*OutletLiquid.h + MV*OutletVapour.h - OutletLiquid.P*V;
436
437"Mol Fraction Normalisation"
438        sum(OutletLiquid.z)=1.0;
439
440"Mol fraction Constraint"
441        sum(OutletLiquid.z)=sum(OutletVapour.z);
442
443"Vapour Density"
444        rhoV = PP.VapourDensity(OutletVapour.T, OutletVapour.P, OutletVapour.z);
445
446"Liquid Volume"
447        vL = PP.LiquidVolume(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z);
448
449"Vapour Volume"
450        vV = PP.VapourVolume(OutletVapour.T, OutletVapour.P, OutletVapour.z);
451
452"Chemical Equilibrium"
453        PP.LiquidFugacityCoefficient(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z)*OutletLiquid.z = PP.VapourFugacityCoefficient(OutletVapour.T, OutletVapour.P, OutletVapour.z)*OutletVapour.z;
454
455"Mechanical Equilibrium"
456        OutletLiquid.P = OutletVapour.P;
457
458"Thermal Equilibrium"
459        OutletLiquid.T = OutletVapour.T;
460
461"Pressure Drop"
462        OutletLiquid.P  = InletLiquid.P - Pdrop;
463
464"Geometry Constraint"
465        V = ML*vL + MV*vV;
466
467"Level of liquid phase"
468        Level = ML*vL/Across;
469
470"Temperature Indicator"
471        TI * 'K' = OutletLiquid.T;
472
473"Pressure Indicator"
474        PI * 'atm' = OutletLiquid.P;
475
476"Level indicator"
477        LI*V = Level*Across;
478
479end
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