source: branches/new_gui/eml/stage_separators/reboiler.mso @ 889

Last change on this file since 889 was 889, checked in by gerson bicca, 13 years ago

fixed: relocated folders

File size: 14.9 KB
Line 
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* $Id$
18*--------------------------------------------------------------------*#
19
20using "tank";
21
22Model thermosyphon
23
24ATTRIBUTES
25        Pallete         = true;
26        Icon            = "icon/Thermosyphon";
27        Brief           = "Model of a  Steady State reboiler 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* the FlowConstant that relates the Flow through the reboiler and the heat duty
36**      Flow^3 = FlowConstant*InletQ
37
38== SPECIFY ==
39* the InletLiquid stream;
40* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model)
41OR the outlet temperature (OutletVapour.T);
42
43== OPTIONAL ==
44* the reboiler model has two control ports
45** TI OutletVapour Temperature Indicator;
46** PI OutletVapour Pressure Indicator;
47";     
48
49PARAMETERS
50        outer PP                as Plugin               (Brief = "External Physical Properties", Type="PP");
51        outer NComp     as Integer              (Brief="Number of Components");
52        Pdrop                   as press_delta  (Brief="Pressure Drop in the reboiler", Symbol = "\Delta P");
53        FlowConstant                    as Real (Brief = "Flow Constant");
54        k                       as Real (Brief = "Flow Constant", Hidden = true, Unit='mol^3/(kg*m^2)');
55
56SET
57
58        k = 1*'mol^3/(kg*m^2)';
59       
60VARIABLES
61        in      InletLiquid     as stream                               (Brief="Liquid inlet stream", PosX=0.44, PosY=1, Symbol="_{inL}");
62        out     OutletVapour    as streamPH                             (Brief="Vapour outlet stream", PosX=0, PosY=0.09, Symbol="_{outV}");
63        in      InletQ                  as power                                (Brief="Heat supplied", PosX=1, PosY=0.77, Symbol="Q_{in}", Protected = true);
64       
65        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=1, PosY=0.57);
66        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=1, PosY=0.35);
67
68EQUATIONS
69
70"Molar Flow Balance"
71        InletLiquid.F = OutletVapour.F;
72
73"Molar Composition Balance"
74        InletLiquid.z = OutletVapour.z;
75       
76"Energy Balance"
77        InletLiquid.F*InletLiquid.h + InletQ = OutletVapour.F*OutletVapour.h;
78       
79"Pressure Drop"
80        OutletVapour.P = InletLiquid.P - Pdrop;
81
82"Temperature indicator"
83        TI * 'K' = OutletVapour.T;
84
85"Pressure indicator"
86        PI * 'atm' = OutletVapour.P;
87       
88"Flow through the thermosyphon reboiler"
89        OutletVapour.F^3 = FlowConstant*k*InletQ;
90
91end
92
93Model reboilerSteady
94
95ATTRIBUTES
96        Pallete         = true;
97        Icon            = "icon/ReboilerSteady";
98        Brief           = "Model of a  Steady State reboiler with no thermodynamics equilibrium - thermosyphon.";
99        Info            =
100"Model of a  Steady State reboiler with two approaches:
101**Fake Conditions: fake calculation of vaporisation fraction and output temperature, but with a real
102calculation of the output stream enthalpy.
103
104**Flash PH: in the outlet stream a PH Flash is performed to obtain the outlet conditions.
105
106== ASSUMPTIONS ==
107* perfect mixing of both phases;
108* no thermodynamics equilibrium;
109
110== SET ==
111* the option Flash_Calculation
112* the fake Outlet temperature;
113* the fake outlet vapour fraction;
114* the pressure drop in the reboiler;
115* the FlowConstant that relates the Flow through the reboiler and the heat duty
116**      Flow^3 = FlowConstant*InletQ
117
118== SPECIFY ==
119* the InletLiquid stream;
120* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model)
121OR the outlet temperature (OutletVapour.T);
122
123== OPTIONAL ==
124* the reboiler model has two control ports
125** TI OutletVapour Temperature Indicator;
126** PI OutletVapour Pressure Indicator;
127";     
128
129PARAMETERS
130        outer PP                as Plugin               (Brief = "External Physical Properties", Type="PP");
131        outer NComp     as Integer              (Brief="Number of Components");
132        Flash_Calculation as Switcher (Brief="Flash Calculation", Valid=["Flash_PH","Fake_Conditions"],Default="Fake_Conditions");
133        Pdrop                   as press_delta  (Brief="Pressure Drop in the reboiler", Symbol = "\Delta P");
134        FlowConstant                    as Real (Brief = "Flow Constant");
135        Fake_Temperature                as temperature  (Brief="Fake temperature", Symbol = "T_{fake}");
136        Fake_Vfrac              as fraction     (Brief="Fake vapour fraction", Symbol = "v_{fake}");
137        k                       as Real (Brief = "Flow Constant", Hidden = true, Unit='mol^3/(kg*m^2)');
138
139SET
140
141        k = 1*'mol^3/(kg*m^2)';
142       
143VARIABLES
144        in      InletLiquid     as stream                       (Brief="Liquid inlet stream", PosX=0.345, PosY=1, Symbol="_{inL}", Protected = true);
145        out     OutletVapour    as stream                       (Brief="Vapour outlet stream", PosX=0.17, PosY=0, Symbol="_{outV}", Protected = true);
146        in      InletQ                  as power                        (Brief="Heat supplied", PosX=1, PosY=0.08, Symbol="Q_{in}", Protected = true);
147
148        x(NComp) as fraction    (Brief = "Liquid Molar Fraction",Hidden=true);
149        y(NComp) as fraction    (Brief = "Vapour Molar Fraction",Hidden=true);
150
151        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=0.44, PosY=0);
152        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=0.35, PosY=0);
153
154EQUATIONS
155
156"Molar Flow Balance"
157        InletLiquid.F = OutletVapour.F;
158
159"Molar Composition Balance"
160        InletLiquid.z = OutletVapour.z;
161       
162"Energy Balance"
163        InletLiquid.F*InletLiquid.h + InletQ = OutletVapour.F*OutletVapour.h;
164       
165"Pressure Drop"
166        OutletVapour.P = InletLiquid.P - Pdrop;
167
168"Temperature indicator"
169        TI * 'K' = OutletVapour.T;
170
171"Pressure indicator"
172        PI * 'atm' = OutletVapour.P;
173       
174"Flow through the reboiler"
175        OutletVapour.F^3 = FlowConstant*k*InletQ;
176
177switch  Flash_Calculation
178
179        case "Flash_PH":
180
181#*"Flash Calculation"
182        [OutletVapour.v, x, y] = PP.FlashPH(OutletVapour.P, OutletVapour.h, OutletVapour.z);
183       
184"Enthalpy"
185        OutletVapour.h = (1-OutletVapour.v)*PP.LiquidEnthalpy(OutletVapour.T, OutletVapour.P, x) +
186        OutletVapour.v*PP.VapourEnthalpy(OutletVapour.T, OutletVapour.P, y);
187*#
188
189"Fake Vapourisation Fraction"
190        OutletVapour.v = Fake_Vfrac;
191
192"Fake output temperature"
193        OutletVapour.T = Fake_Temperature;
194
195"Fake Liquid Molar Fraction"
196        x = 1;
197
198 "Fake Vapour Molar Fraction"
199        y = 1;
200
201        case "Fake_Conditions":
202
203"Fake Vapourisation Fraction"
204        OutletVapour.v = Fake_Vfrac;
205
206"Fake output temperature"
207        OutletVapour.T = Fake_Temperature;
208
209"Fake Liquid Molar Fraction"
210        x = 1;
211
212 "Fake Vapour Molar Fraction"
213        y = 1;
214
215end
216
217end
218
219Model reboilerReact
220        ATTRIBUTES
221        Pallete         = false;
222        Icon            = "icon/Reboiler";
223        Brief           = "Model of a dynamic reboiler with reaction.";
224        Info            =
225"== Assumptions ==
226* perfect mixing of both phases;
227* thermodynamics equilibrium;
228* no liquid entrainment in the vapour stream;
229* the reaction takes place only in the liquid phase.
230       
231== Specify ==
232* the kinetics variables;
233* the inlet stream;
234* the liquid inlet stream;
235* the outlet flows: OutletVapour.F and OutletLiquid.F;
236* the heat supply.
237
238== Initial Conditions ==
239* the reboiler temperature (OutletLiquid.T);
240* the reboiler liquid level (Level);
241* (NoComps - 1) OutletLiquid (OR OutletVapour) compositions.
242";
243       
244PARAMETERS
245        outer PP as Plugin(Type="PP");
246        outer NComp as Integer;
247        Across as area (Brief="Cross Section Area of reboiler");
248        V as volume (Brief="Total volume of reboiler");
249
250        stoic(NComp) as Real(Brief="Stoichiometric matrix");
251        Hr as energy_mol;
252
253        Initial_Level                           as length               (Brief="Initial Level of liquid phase");
254        Initial_Temperature                     as temperature  (Brief="Initial Temperature of Reboiler");
255        Initial_Composition(NComp)      as fraction     (Brief="Initial Liquid Composition");
256       
257VARIABLES
258in      InletLiquid     as stream                       (Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
259out     OutletLiquid as liquid_stream   (Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
260out     OutletVapour as vapour_stream   (Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
261        InletQ  as power                        (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");
262
263        M(NComp)        as mol                  (Brief="Molar Holdup in the tray");
264        ML                      as mol                  (Brief="Molar liquid holdup");
265        MV                      as mol                  (Brief="Molar vapour holdup");
266        E                       as energy               (Brief="Total Energy Holdup on tray");
267        vL                      as volume_mol   (Brief="Liquid Molar Volume");
268        vV                      as volume_mol   (Brief="Vapour Molar volume");
269        Level           as length               (Brief="Level of liquid phase");
270        Vol             as volume;
271        rhoV            as dens_mass;
272        r3                      as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
273        C(NComp)        as conc_mol     (Brief = "Molar concentration", Lower = -1);
274
275INITIAL
276
277        Level                                   = Initial_Level;
278        OutletLiquid.T                          = Initial_Temperature;
279        OutletLiquid.z(1:NComp-1)       = Initial_Composition(1:NComp-1)/sum(Initial_Composition);
280
281EQUATIONS
282"Molar Concentration"
283        OutletLiquid.z = vL * C;
284       
285"Reaction"
286        r3 = exp(-7150*'K'/OutletLiquid.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4)) * 'l/mol/s';
287
288"Component Molar Balance"
289        diff(M)= InletLiquid.F*InletLiquid.z- OutletLiquid.F*OutletLiquid.z - OutletVapour.F*OutletVapour.z + stoic*r3*ML*vL;
290       
291"Energy Balance"
292        diff(E) = InletLiquid.F*InletLiquid.h- OutletLiquid.F*OutletLiquid.h - OutletVapour.F*OutletVapour.h + InletQ + Hr * r3 * vL*ML;
293       
294"Molar Holdup"
295        M = ML*OutletLiquid.z + MV*OutletVapour.z;
296       
297"Energy Holdup"
298        E = ML*OutletLiquid.h + MV*OutletVapour.h - OutletLiquid.P*V;
299       
300"Mol fraction normalisation"
301        sum(OutletLiquid.z)=1.0;
302       
303"Liquid Volume"
304        vL = PP.LiquidVolume(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z);
305
306"Vapour Volume"
307        vV = PP.VapourVolume(OutletVapour.T, OutletVapour.P, OutletVapour.z);   
308
309"Vapour Density"
310        rhoV = PP.VapourDensity(OutletVapour.T, OutletVapour.P, OutletVapour.z);
311       
312"Level of liquid phase"
313        Level = ML*vL/Across;
314
315        Vol = ML*vL;
316       
317"Mechanical Equilibrium"
318        OutletLiquid.P = OutletVapour.P;
319       
320"Thermal Equilibrium"
321        OutletLiquid.T = OutletVapour.T;       
322       
323"Geometry Constraint"
324        V = ML*vL + MV*vV;             
325
326"Chemical Equilibrium"
327        PP.LiquidFugacityCoefficient(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z)*OutletLiquid.z =
328        PP.VapourFugacityCoefficient(OutletVapour.T, OutletVapour.P, OutletVapour.z)*OutletVapour.z;
329
330        sum(OutletLiquid.z)=sum(OutletVapour.z);
331       
332end
333
334Model reboiler
335       
336ATTRIBUTES
337        Pallete = true;
338        Icon    = "icon/Reboiler";
339        Brief   = "Model of a dynamic reboiler - kettle with control.";
340        Info            =
341"== ASSUMPTIONS ==
342* perfect mixing of both phases;
343* thermodynamics equilibrium;
344* no liquid entrainment in the vapour stream.
345
346== SET ==
347*Orientation: vessel position - vertical or horizontal;
348*Heads (bottom and top heads are identical)
349**elliptical: 2:1 elliptical heads (25% of vessel diameter);
350**hemispherical: hemispherical heads (50% of vessel diameter);
351*Diameter: Vessel diameter;
352*Lenght: Side length of the cylinder shell;
353
354== SPECIFY ==
355* the InletLiquid stream;
356* the outlet flows: OutletVapour.F and OutletLiquid.F;
357* the InletQ (the model requires an energy stream, also you can use a controller for setting the heat duty using the heat_flow model).
358
359== OPTIONAL ==
360* the reboiler model has three control ports
361** TI OutletLiquid Temperature Indicator;
362** PI OutletLiquid Pressure Indicator;
363** LI Level Indicator of Reboiler;
364
365== INITIAL CONDITIONS ==
366* Initial_Temperature :  the reboiler temperature (OutletLiquid.T);
367* Levelpercent_Initial : the reboiler liquid level in percent (LI);
368* Initial_Composition : (NoComps) OutletLiquid compositions.
369";     
370       
371PARAMETERS
372        outer PP                as Plugin       (Brief = "External Physical Properties", Type="PP");
373        outer NComp     as Integer      (Brief="Number of Components");
374       
375        Levelpercent_Initial            as positive     (Brief="Initial liquid height in Percent", Default = 0.70);
376        Initial_Temperature                     as temperature  (Brief="Initial Temperature of Reboiler");
377        Initial_Composition(NComp)      as positive     (Brief="Initial Liquid Composition",Lower=1E-6);
378
379VARIABLES
380
381        Geometry                as VesselVolume (Brief="Vessel Geometry", Symbol=" ");
382
383in      InletLiquid     as stream                       (Brief="Liquid inlet stream", PosX=0.17, PosY=1, Symbol="_{in}^{Liquid}");
384out     OutletLiquid    as liquid_stream        (Brief="Liquid outlet stream", PosX=0.53, PosY=1, Symbol="_{out}^{Liquid}");
385out     OutletVapour    as vapour_stream        (Brief="Vapour outlet stream", PosX=0.17, PosY=0, Symbol="_{out}^{Vapour}");
386in      InletQ                  as power                        (Brief="Heat supplied", Protected = true, PosX=1, PosY=0.08, Symbol="Q_{in}");
387
388        out     TI as control_signal    (Brief="Temperature  Indicator of Reboiler", Protected = true, PosX=0.44, PosY=0);
389        out     LI as control_signal    (Brief="Level Indicator of Reboiler", Protected = true, PosX=0.53, PosY=0);
390        out     PI as control_signal    (Brief="Pressure Indicator of Reboiler", Protected = true, PosX=0.35, PosY=0);
391       
392        M(NComp)        as mol                  (Brief="Molar Holdup in the tray", Protected = true);
393        ML                      as mol                  (Brief="Molar liquid holdup", Protected = true);
394        MV                      as mol                  (Brief="Molar vapour holdup", Protected = true);
395        E                       as energy               (Brief="Total Energy Holdup on tray", Protected = true);
396        vL                      as volume_mol   (Brief="Liquid Molar Volume", Protected = true);
397        vV                      as volume_mol   (Brief="Vapour Molar volume", Protected = true);
398        rhoV            as dens_mass    (Brief="Vapour Density", Protected = true, Symbol="\rho");
399        Pdrop           as press_delta  (Brief = "Pressure Drop", DisplayUnit = 'kPa', Symbol ="\Delta P", Protected=true);
400
401INITIAL
402
403"Initial level Percent"
404        LI = Levelpercent_Initial;
405
406"Initial Temperature"
407        OutletLiquid.T  = Initial_Temperature;
408
409"Initial Composition"
410        OutletLiquid.z(1:NComp-1) = Initial_Composition(1:NComp-1)/sum(Initial_Composition);
411
412EQUATIONS
413
414"Component Molar Balance"
415        diff(M)= InletLiquid.F*InletLiquid.z    - OutletLiquid.F*OutletLiquid.z - OutletVapour.F*OutletVapour.z;
416
417"Energy Balance"
418        diff(E) = InletLiquid.F*InletLiquid.h   - OutletLiquid.F*OutletLiquid.h - OutletVapour.F*OutletVapour.h + InletQ;
419
420"Molar Holdup"
421        M = ML*OutletLiquid.z + MV*OutletVapour.z;
422
423"Energy Holdup"
424        E = ML*OutletLiquid.h + MV*OutletVapour.h - OutletLiquid.P*Geometry.Vtotal;
425
426"Mol Fraction Normalisation"
427        sum(OutletLiquid.z)=1.0;
428
429"Mol fraction Constraint"
430        sum(OutletLiquid.z)=sum(OutletVapour.z);
431
432"Vapour Density"
433        rhoV = PP.VapourDensity(OutletVapour.T, OutletVapour.P, OutletVapour.z);
434
435"Liquid Volume"
436        vL = PP.LiquidVolume(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z);
437
438"Vapour Volume"
439        vV = PP.VapourVolume(OutletVapour.T, OutletVapour.P, OutletVapour.z);
440
441"Chemical Equilibrium"
442        PP.LiquidFugacityCoefficient(OutletLiquid.T, OutletLiquid.P, OutletLiquid.z)*OutletLiquid.z = PP.VapourFugacityCoefficient(OutletVapour.T, OutletVapour.P, OutletVapour.z)*OutletVapour.z;
443
444"Mechanical Equilibrium"
445        OutletLiquid.P = OutletVapour.P;
446
447"Thermal Equilibrium"
448        OutletLiquid.T = OutletVapour.T;
449
450"Pressure Drop"
451        OutletLiquid.P  = InletLiquid.P - Pdrop;
452
453"Geometry Constraint"
454        Geometry.Vtotal = ML*vL + MV*vV;
455
456"Liquid Level"
457        ML * vL = Geometry.Vfilled;
458
459"Temperature Indicator"
460        TI * 'K' = OutletLiquid.T;
461
462"Pressure Indicator"
463        PI * 'atm' = OutletLiquid.P;
464
465"Level indicator"
466        LI*Geometry.Vtotal= Geometry.Vfilled;
467
468end
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