source: trunk/BioModel/separators/evaporator.mso @ 1008

Last change on this file since 1008 was 1008, checked in by Argimiro Resende Secchi, 21 months ago

Adding BioModel? to the MSO library.
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1#*-------------------------------------------------------------------
2* Biorrefinaria Petrobras
3*--------------------------------------------------------------------
4* Nome do arquivo: evaporator.mso
5* Projeto: Modelo integrado de producao de etanol 1G/2G
6* Conteudo: evaporador
7*--------------------------------------------------------------------*#
8
9#*-------------------------------------------------------------------
10*
11* Versao 2.2
12* Data:    03/2016
13* Autores:   Anderson R. A. Lino e Gabriel C. Fonseca
14*
15*--------------------------------------------------------------------
16*Descricao: modelo do evaporador que sera empregado na biorrefinaria
17*--------------------------------------------------------------------
18
19*--------------------------------------------------------------------
20*Hipoteses assumidas: 1 - mistura perfeita
21*                     2 - sem perdas de calor para o ambiente
22*                     3 - modelo estacionario
23*Bibliografia:
24        [1] JESUS, C. D. F. Desenvolvimento de simulador dinamico do
25        processo de acucar.
26        Sao Carlos, SP, UFSCar, 2000 (Dissertacao). 131p.
27*--------------------------------------------------------------------
28
29*--------------------------------------------------------------------
30*Notas: Foram feitos 2 flowsheets para averiguar os modelos
31*--------------------------------------------------------------------*#
32
33using "main_stream";
34using "water_stream";
35using "assumptions";
36
37Model evaporator3
38
39        ATTRIBUTES
40        Pallete         = true;
41        Icon            = "icon/evaporator";
42        Brief           = "Model of an Evaporator";
43        Info =
44"== GENERAl ==
45        Model of an evaporator, with calculated boiling point elevation and
46        supposing that only water leaves the system as vapour.
47        The boiling point elevation is given by:
48       
49        BPE * 0.355 * (1.036 - Brix) = Brix * (0.3 + Brix) * (0.22 * 'K' + 0.0078 * Tsat[C]).
50       
51        With BPE being the boiling point elevation, Outlet_Brix the mass fraction
52        of soluble solids inside the evaporator and Tsat is the saturation
53        temperature of pure water at the internal pressure.
54
55== ASSUMPTIONS ==
56* Steady-state;
57* Only water leaves the system as vapour;
58* The heating steam leaves the system as saturated water;
59* Adiabatic.
60
61== SPECIFY ==
62* The inlet stream:
63  flow rate
64  temperature
65  pressure
66  stream composition;
67* The inlet water stream:
68  Temperature
69  Vapourization fraction;
70* The outlet vapour temperature;
71* The outlet brix.
72
73== SET ==
74* Basic composition (mass or molar);
75* Number of stream components(Ncomp/NcompS);
76* The compounds that participate in the Brix calculation
77        (1 if participates, 0 if not).
78       
79== REFERENCES ==
80        [1] JESUS, C. D. F. Desenvolvimento de simulador dinamico do processo de acucar.
81        Sao Carlos, SP, UFSCar, 2000 (Dissertacao). 131p.
82";
83#*-------------------------------------------------------------------
84* Parametros
85*--------------------------------------------------------------------*#
86
87PARAMETERS
88
89                propterm        as Plugin               (Brief = "IAPWS 97 properties of water",Type = "water");
90outer   PP                      as Plugin               (Brief = "External Physical Properties (Fluid Phase)", Type="PP");
91outer   PPS             as Plugin               (Brief = "External Physical Properties (Solid Phase)", Type="PP");
92outer   NComp           as Integer              (Brief = "Number of Chemical Components for the Fluid Phase", Lower = 1);
93outer   NCompS          as Integer              (Brief = "Number of Chemical Components for the Solid Phase", Lower = 1);
94                M(NComp)        as molweight    (Brief = "Component Mol Weight (Fluid Phase), Vector Size = NComp", Protected=true);
95                MS(NCompS)  as molweight        (Brief = "Component Mol Weight (Solid Phase), Vector Size = NCompS", Protected=true);
96outer   flu as ConstituentFluid(Symbol = " ", Protected = true);
97                Brix(NComp)     as Integer              (Brief = "Flag for the Compound that Enters the Brix Calculation");
98                Brix_max        as fraction             (Brief = "Maximum Total Soluble Solids-Inlet", Default = 1, Symbol = "Brix_{max}");
99
100#*-------------------------------------------------------------------
101* Define o valor dos parametros declarados no modelo
102*--------------------------------------------------------------------*#
103
104        SET
105       
106        M  = PP.MolecularWeight();
107        MS = PPS.MolecularWeight();
108        OutletV.ValidPhases = "Vapour-Only";
109
110#*-------------------------------------------------------------------
111* Declaracao de variaveis
112*--------------------------------------------------------------------*#
113
114VARIABLES
115
116in      Inlet           as main_stream                    (Brief = "Feed Stream", PosX=1, PosY=0.3, Protected = false, Symbol="_{in}");
117in  InletS      as water_stream                   (Brief = "Steam Inlet", PosX=1, PosY=0.63, Protected = true, Symbol = "_{in_S}");
118out     OutletL         as main_stream_eq                 (Brief = "Liquid Outlet Stream", PosX=0, PosY=0.85, Protected = false, Symbol="_{out Liquid}");
119out OutletS     as water_stream_vapfrac   (Brief = "Condensed Steam Outlet",PosX=0,PosY=0.63, Protected = false, Symbol = "_{out_S}");
120out OutletV     as water_stream_eq                (Brief = "Vapour Outlet Stream", PosX=0, PosY=0.15, Protected =false, Symbol="_{outVapour}");
121        Q                       as power                                  (Brief = "Heat Duty", PosX=0.5, PosY=1, Protected = true, Symbol="_{in}");
122       
123        A                       as area                                 (Brief="Area of heat exchange");
124        U                       as heat_trans_coeff     (Brief="Global coefficient of heat exchange");
125        vfrac           as fraction                             (Brief = "Vaporization Fraction", Symbol="\phi", Protected = true);
126        Tsat            as temperature                  (Brief = "Saturation Temperature", Symbol = "T_{sat}", Protected = true);
127        P                       as pressure                     (Brief = "Pressure Inside the Evaporator");
128        Inlet_Brix  as fraction                         (Brief = "Total Soluble Solids-Inlet", Symbol = "Brix_{in}");
129        Outlet_Brix as fraction                         (Brief = "Total Soluble Solids-Outlet", Symbol = "Brix_{out}");
130        BPE                     as temp_delta                   (Brief = "Boiling Point Elevation", Protected = true);
131       
132        Hv                      as enth_mass            (Brief = "Mass Enthalpy for the Outlet Vapour Phase in the Reference State", Hidden = true);
133        Sv                      as entr_mass            (Brief = "Mass Entropy for the Vapour Phase in the Reference State", Hidden = true);
134        hl1                     as enth_mol                     (Brief = "Molar Enthalpy for the inlet Liquid Phase in the Reference State (Fluid Phase)", Hidden = true);
135        hlsol1          as enth_mol                     (Brief = "Molar Enthalpy for the inlet Liquid Phase in the Reference State (Solid Phase)", Hidden = true);
136        hl2                     as enth_mol                     (Brief = "Molar Enthalpy for the OutletL Liquid Phase in the Reference State (Fluid Phase)", Hidden = true);
137        hlsol2          as enth_mol                     (Brief = "Molar Enthalpy for the OutletL Liquid Phase in the Reference State (Solid Phase)", Hidden = true);
138       
139        SET
140        OutletL.Phase = "Liquid";
141        OutletV.ValidPhases = "Vapour-Only";
142       
143#*-------------------------------------------------------------------
144* Equacoes do modelo
145*--------------------------------------------------------------------*#
146
147        EQUATIONS
148               
149        if Inlet_Brix > Brix_max then
150
151        "Global Mass Balance (Fluid Phase)"
152        Inlet.Fluid.Fw = OutletV.Fw + OutletL.Fluid.Fw;
153       
154        "Component Molar Balance (Fluid Phase)"
155        Inlet.Fluid.z = OutletL.Fluid.z;
156       
157        "Vapour Fraction"
158        vfrac = 1e-6;
159       
160        "Heat Required by the Effect"
161        Q = InletS.Fw * (InletS.H - OutletS.H);
162       
163        "General equation of heat exchange"
164        Q = U * A * ( InletS.T - OutletL.T );
165       
166        "Total Soluble Solids-Outlet"
167        Outlet_Brix = Inlet_Brix;
168       
169        "Saturation Temperature for Pure Water"
170        Tsat = propterm.Tsat(OutletV.P);
171       
172        "Boiling Point Elevation"
173        BPE = 1 * 'K';
174       
175        "Thermal Equilibrium 2"
176        OutletL.T = Inlet.T;
177       
178        "Mechanical Equilibrium 2"
179        OutletL.P  = 1 * 'atm';
180               
181        "Thermal Equilibrium"
182        OutletV.T = Tsat + BPE;
183       
184        else   
185       
186        "Global Mass Balance (Fluid Phase)"
187        Inlet.Fluid.Fw = OutletV.Fw + OutletL.Fluid.Fw;
188       
189        for i in [1:NComp] do
190                if i equal flu.Water then
191                        "Component Mass Balance (Fluid Phase)"
192                        Inlet.Fluid.Fw * Inlet.Fluid.zw(i) = OutletL.Fluid.Fw * OutletL.Fluid.zw(i) + OutletV.Fw;
193                else
194                        "Component Mass Balance (Fluid Phase)"
195                        Inlet.Fluid.Fw * Inlet.Fluid.zw(i) = OutletL.Fluid.Fw * OutletL.Fluid.zw(i);
196                end
197        end
198       
199        "Vapour Fraction"
200        OutletV.Fw = Inlet.Total.Fw * vfrac;
201       
202        "Energy Balance"
203        Q = (OutletV.H - Hv) * OutletV.Fw + (OutletL.Fluid.h - hl2) * OutletL.Fluid.F + (OutletL.Solid.h - hlsol2) * OutletL.Solid.F
204                - (Inlet.Fluid.h - hl1) * Inlet.Fluid.F - (Inlet.Solid.h - hlsol1) * Inlet.Solid.F;
205       
206        "Heat Required by the Effect"
207        Q = InletS.Fw * (InletS.H - OutletS.H);
208       
209        "General equation of heat exchange"
210        Q = U * A * ( InletS.T - OutletL.T );
211       
212        "Total Soluble Solids-Outlet"
213        Outlet_Brix = sum(OutletL.Fluid.zw * Brix);
214       
215        "Saturation Temperature for Pure Water at Pressure P"
216        Tsat = propterm.Tsat(OutletV.P);
217       
218        "Boiling Point Elevation"
219        BPE * 0.355 * ( 1.036 - Outlet_Brix) = Outlet_Brix * ( 0.3 + Outlet_Brix) * ( 0.22 * 'K' + 0.0078 * (Tsat - 273.15* 'K'));
220       
221        "Thermal Equilibrium 2"
222        OutletL.T = Tsat + BPE;
223       
224        "Thermal Equilibrium 1"
225        OutletV.T = OutletL.T;
226       
227        end
228       
229        "Global Mass Balance (Steam)"
230        InletS.Fw = OutletS.Fw;
231       
232        "Global Molar Balance (Solid Phase)"
233        Inlet.Solid.F = OutletL.Solid.F;
234       
235        "Component Molar Balance (Solid Phase)"
236        Inlet.Solid.z = OutletL.Solid.z;
237       
238        "Total Soluble Solids-Inlet"
239        Inlet_Brix = sum(Inlet.Fluid.zw * Brix);
240       
241        "Enthalpy of Steam, array = [OutletS.S, OutletS.H]"
242        [OutletS.S, OutletS.H] = propterm.propPTl(OutletS.P, propterm.Tsat(OutletS.P));
243       
244        "Outlet Vapour Mass Entropy and Enthalpy at the Reference State, array = [Sv, Hv]"
245        [Sv, Hv] = propterm.propPTl(Inlet.P, 300 * 'K');
246       
247        "Inlet Molar Enthalpy at the Reference State (Fluid Phase)"
248        hl1 = PP.LiquidEnthalpy(300 * 'K', Inlet.P, Inlet.Fluid.z);
249       
250        "Inlet Molar Enthalpy at the Reference State (Solid Phase)"
251        hlsol1 = PPS.VapourEnthalpy(300 * 'K', Inlet.P, Inlet.Solid.z);
252       
253        "Outlet Liquid Molar Enthalpy at the Reference State (Fluid Phase)"
254        hl2 = PP.LiquidEnthalpy(300 * 'K', Inlet.P, OutletL.Fluid.z);
255       
256        "Outlet Liquid Molar Enthalpy at the Reference State (Solid Phase)"
257        hlsol2 = PPS.VapourEnthalpy(300 * 'K', Inlet.P, OutletL.Solid.z);
258       
259        "Mechanical Equilibrium 1"
260                OutletV.P = OutletL.P;
261       
262        "Mechanical Equilibrium 2"
263                OutletL.P  = P;
264       
265        "Mechanical Equilibrium 3"
266                OutletS.P = InletS.P;
267       
268        "Outlet Condensed Steam Temperature"
269                OutletS.T = propterm.Tsat(InletS.P);
270       
271        "Heat transference coefficient"
272                U = 4.65 * (OutletL.T - 273.15 * 'K' ) / Outlet_Brix * 'kg /s^3 /K^2';
273
274end
275
276
277FlowSheet teste_evaporator3
278       
279#*-------------------------------------------------------------------
280* Declaracao de dispositivos (ou blocos contendo o modelo)
281*--------------------------------------------------------------------*#
282       
283        DEVICES
284        S101 as main_sourceR;
285        S102 as water_sourceL;
286        Ev101 as evaporator3;
287       
288#*-------------------------------------------------------------------
289* Especifica as conexoes entre os modelos
290*--------------------------------------------------------------------*#
291       
292        CONNECTIONS
293        S101.Outlet to Ev101.Inlet;
294        S102.Outlet to Ev101.InletS;
295
296#*-------------------------------------------------------------------
297* Define o valor dos parametros declarados no modelo
298*--------------------------------------------------------------------*#
299
300        SET
301        S101.ValidPhases = "Vapour-Liquid";
302        S102.ValidPhases = "Vapour-Liquid";
303        NComp = PP.NumberOfComponents();
304        NCompS = PPS.NumberOfComponents();
305       
306#*-------------------------------------------------------------------
307* Especifica variaveis definidas no modelo
308*--------------------------------------------------------------------*#
309       
310        SPECIFY
311        S101.Fluid.Fw = 441130 * 'kg/h';
312        S101.Solid.Fw = 6303.1 * 'kg/h';
313        S101.T = 373.15 * 'K';
314        S101.P = 0.957834 * 'atm';
315        S101.CompositionOfSolid = [0.4, 0.37, 0.21, 0.02, 0, 0, 0, 0, 0.002];
316        S101.CompositionOfFluid = [0.83, 0.16, 0.01, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
317       
318        Ev101.OutletV.T = 358.15 * 'K';
319        Ev101.Outlet_Brix = 0.52;
320        S102.P = 1.29927 * 'atm';
321        S102.v = 1;
322
323#*-------------------------------------------------------------------
324#Parametros
325*--------------------------------------------------------------------*#
326
327        PARAMETERS
328        PP as Plugin    (Brief = "External Physical Properties",
329                Type="PP",
330                Project = "../Flowsheets/v2_2/Fluid_v2_2.vrtherm"
331        );
332        PPS as Plugin   (Brief = "External Physical Properties",
333                Type="PP",
334                Project = "../Flowsheets/v2_2/Solid_v2_2.vrtherm"
335        );
336       
337        NComp   as Integer (Brief = "Number of chemical components in the fluid phase");
338        NCompS  as Integer (Brief = "Number of chemical components in the solid phase");
339        flu as ConstituentFluid(Symbol = " ", Protected = true);
340        sol as ConstituentSolid(Symbol = " ", Protected = true);
341       
342#*-------------------------------------------------------------------
343* Define o valor dos parametros declarados no modelo
344*--------------------------------------------------------------------*#
345       
346        SET
347        NComp = PP.NumberOfComponents();
348        NCompS = PPS.NumberOfComponents();
349        S101.CompositionBasis = "Mass";
350        Ev101.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
351       
352#*-------------------------------------------------------------------
353* Condicoes iniciais e opcoes de Solver
354*--------------------------------------------------------------------*#
355
356        OPTIONS
357        Dynamic = false;
358        NLASolver(
359                File = "sundials",
360                RelativeAccuracy = 1e-3,
361                AbsoluteAccuracy = 1e-6,
362                MaxIterations = 100
363        );
364end
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