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boiler.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.
File size: 20.9 KB

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1	#*-------------------------------------------------------------------
2	* Biorrefinaria Petrobras
3	*--------------------------------------------------------------------
4	* Nome do arquivo: boiler.mso
5	* Projeto: Modelo integrado de producao de etanol 1G/2G
6	* Conteudo: caldeira
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 da caldeira que sera empregada na biorrefinaria
17	*--------------------------------------------------------------------
18
19	*--------------------------------------------------------------------
20	*Hipoteses assumidas: 1 - equilibrio termico
21	* 2 - equilibrio mecanico
22	* 3 - geracao somente de CO2 e H2O
23	*--------------------------------------------------------------------
24
25	*--------------------------------------------------------------------
26	*Notas: Foram feitos 2 flowsheets para averiguar os modelos
27	--------------------------------------------------------------------#
28
29	using "main_stream";
30	using "water_stream";
31	using "energy_stream";
32	using "assumptions";
33
34	Model boiler
35
36	ATTRIBUTES
37	Pallete = true;
38	Icon = "icon/boiler";
39	Brief = "Simplified Boiler Model";
40	Info =
41	"== GENERAL ==
42	Modeling of a boiler based on a stoichiometric approach.
43	The conversion of the reactions should be specified based on the
44	liminting compound. Also, the limiting compound should have a
45	stoichiometric coefficient equal to minus one. The model also
46	regards some process variables such as the excess of air, the
47	lower and the higher heating values, the boiler efficiency related
48	to both of them, the specific steam production and the heat lost to
49	the surroundings (based on the higher heating value).
50
51	Note that the higher heating value (HHV) is defined here as the heat
52	of combustion at 298.15 K, as defined by the American Petroleum
53	Institute. The lower heating value (LHV), on the other hand, is
54	defined here as commonly used in the sugar and ethanol industry. This
55	definition assumes that all combustion products (water and carbon
56	dioxide) are present as gases at 298.15 K. It is impontant to note
57	that this definition considers not only the water produced by the
58	combustion but also the one present in the inlet streams (Fuel and
59	Air streams).
60
61	== ASSUMPTIONS ==
62	* All three-phases can be involved;
63	* Steady-state;
64	* Only carbon dioxide and water are produced in the combustion.
65
66	== SPECIFY ==
67	* The Fuel and Air stream;
68	flow rate
69	temperature
70	pressure
71	stream composition;
72	* The water steam stream:
73	temperature
74	pressure;
75	* Conversion for each reaction based on the limiting compound;
76	* Temperature of the outlet steam;
77	* The boiler HHV or LHV efficiency;
78	* The excess of air;
79	* The pressure drop in the water/steam side;
80	* The fraction of heat that is lost to the surroundings.
81
82	== SET ==
83	* Number of stream components(Ncomp/NcompS);
84	* Phase of the stream feed;
85	* Number of reactions;
86	* Stoichiometric matrix;
87	* Limiting compound for each reaction;
88	* Heat of reaction;
89	* The position in the compound vector of the water (NWater) and
90	the oxygen (NO2).
91
92	== ADITIONAL INFORMATION ==
93	* Specific steam production (based on inlet fuel mass);
94	* Dry and wet higher heating values;
95	* Lower heating value;
96	* Air humidity;
97	* Boiler efficiency (based on both HHV and LHV).
98	";
99
100	#*-------------------------------------------------------------------
101	#Parametros
102	--------------------------------------------------------------------#
103
104	PARAMETERS
105
106	propterm as Plugin (Brief = "IAPWS 97 properties of water",Type = "water");
107	outer PP as Plugin (Brief = "External Physical Properties (Fluid Phase)", Type="PP");
108	outer PPS as Plugin (Brief = "External Physical Properties (Solid Phase)", Type="PP");
109	outer NComp as Integer (Brief = "Number Of Chemical Components");
110	outer NCompS as Integer (Brief = "Number Of Chemical Components for the Solid Phase");
111	NReac as Integer (Brief = "Number Of Reactions", Default = 1);
112	stoic(NComp + NCompS, NReac) as Real (Brief = "Stoichiometric Matrix, Matrix Size = NComp+NCompS, NReac");
113	limit(NReac) as Integer (Brief = "Limiting Component Index Number, Vector Size = NReac", Lower = 1);
114	h(NReac) as heat_reaction (Brief = "Molar Heat of Reaction Based on Limiting Component, Vector Size = NReac");
115	M(NComp) as molweight (Brief = "Component Mol Weight", Protected=true);
116	MS(NCompS) as molweight (Brief = "Component Mol Weight", Protected=true);
117	outer flu as ConstituentFluid(Symbol = " ", Protected = true);
118
119	#*-------------------------------------------------------------------
120	* Define o valor dos parametros declarados no modelo
121	--------------------------------------------------------------------#
122
123	SET
124
125	M = PP.MolecularWeight();
126	MS = PPS.MolecularWeight();
127
128	#*-------------------------------------------------------------------
129	* Declaracao de variaveis
130	--------------------------------------------------------------------#
131
132	VARIABLES
133	in Fuel as main_stream (Brief = "Inlet Mass Flow", PosX=0, PosY=0.65, Symbol="_{Fuel}", Protected = false);
134	in Air as main_stream (Brief = "Inlet Air Flow", PosX=0, PosY=0.5, Symbol="_{Air}", Protected = false);
135	in Water as water_stream (Brief = "Inlet Water Mass Flow", PosX=0, PosY=0.02, Symbol="_{Water}", Protected = false);
136	in Inlet_q as heat_stream (Brief = "Imported Energy", PosX=0, PosY=0.81, Protected =true,Symbol="_{in}");
137	out Steam as water_stream_vapfrac (Brief = "Vapour Outlet Flow", PosX=0.833, PosY=0.0, Symbol="_{Steam}", Protected = false);
138	out Gas as main_stream_eq (Brief = "Outlet Gas", PosX=0.95, PosY=0, Symbol="_{Gas}", Protected = false);
139	out Ash as main_stream_eq (Brief = "Outlet Ash", PosX=1, PosY=0.5, Symbol="_{Ash}", Protected = false);
140
141	FGas as flow_mol (Brief = "Stoichiometric Oxygen Molar Flow", Hidden = true, Symbol = "F_{stoichGas}");
142	zGas(NComp) as fraction (Brief = "Stoichiometric Oxygen Molar Fraction, Vector Size = NComp", Hidden = true, Symbol = "z_{stoichGas}");
143	F as flow_mol (Brief = "Total Inlet Stream Flow", Hidden = true);
144	z(NComp + NCompS) as fraction (Brief = "Total Inlet Composition, Vector Size = NComp+NCompS", Hidden = true);
145	Pdrop as press_delta (Brief = "Pressure Drop in the Water/Steam Side", Symbol = "\Delta P");
146	T as temperature (Brief = "Outlet Steam Temperature");
147	Efficiency_HHV as fraction (Brief = "Heat Transfer Efficiency (Higher Heating Value)", Symbol = "\eta_{HHV}");
148	Efficiency_LHV as fraction (Brief = "Heat Transfer Efficiency (Lower Heating Value)", Symbol = "\eta_{LHV}");
149	q_losses as heat_rate (Brief = "Heat Losses", Symbol = "q_{loss}");
150	f_losses as fraction (Brief = "Heat Fraction Losses", Symbol = "f_{loss}");
151	q_ex as heat_rate (Brief = "Heat Exchanged", Symbol = "q_{ex}");
152	q_HHV as heat_rate (Brief = "Higher Heating Value (Heat)", Symbol = "q_{HHV}", Hidden = true);
153	q_LHV as heat_rate (Brief = "Lower Heating Value (Heat)", Symbol = "q_{LHV}", Hidden = true);
154	q_comb as heat_rate (Brief = "Heat of Combustion at the Operational Temperature", Symbol = "q_{comb}", Hidden = true);
155	v_specific as Real (Brief = "Specific Production of Kilogram of Steam/Kilogram of Wet Bagasse", Symbol = "v_{specific}", Unit = 'kg/kg', Protected = true);
156	HHV_dry as Real (Brief = "Higher Heating Value - Dry Basis", Symbol = "HHV_{dry}", Default=500, Lower=-1e8, Upper=1e8, final Unit = 'kJ/kg');
157	HHV_wet as Real (Brief = "Higher Heating Value - Wet Basis", Symbol = "HHV_{wet}", Default=500, Lower=-1e8, Upper=1e8, final Unit = 'kJ/kg');
158	LHV as Real (Brief = "Lower Heating Value - Wet Basis", Default=500, Lower=-1e8, Upper=1e8, final Unit = 'kJ/kg');
159	r(NComp + NCompS, NReac) as Real (Brief = "Ratio between component (i) production/consumption for the limiting component, Matrix Size = NComp+NCompS, NReac");
160	conv(NReac) as fraction (Brief = "Reaction Conversion Based on Limiting Component, Vector Size = NReac");
161	Ex_Air as fraction (Brief = "Excess Air fraction", Symbol = "Ex_{Air}");
162	humidity as fraction (Brief = "Fraction of Water in Air", Protected = true);
163	h_gas as enth_mol (Brief = "Molar Enthalpy of Gas", Symbol = "h_{gas}", Hidden = true);
164	h_ash as enth_mol (Brief = "Molar Enthalpy of Ash", Symbol = "h_{ash}", Hidden = true);
165	h_air as enth_mol (Brief = "Molar Enthalpy of Air", Symbol = "h_{air}", Hidden = true);
166	h_bag_sol as enth_mol (Brief = "Molar Enthalpy of Bagasse (Solid)", Symbol = "h_{bagsol}", Hidden = true);
167	h_bag_fluid as enth_mol (Brief = "Molar Enthalpy of Bagasse (Fluid)",Symbol = "h_{bagfluid}", Hidden = true);
168	x_gas_1(NComp) as fraction (Brief = "Fraction of Liquids in Gas", Symbol = "x_{gas1}", Hidden = true);
169	y_gas_1(NComp) as fraction (Brief = "Fraction of Vapour in Gas", Symbol = "y_{gas1}", Hidden = true);
170	v_gas_1 as fraction (Brief = "Fraction of Vapour in Mixture_Gas", Symbol = "v_{gas1}", Hidden = true);
171	x_gas_2(NComp) as fraction (Brief = "Fraction of Liquids in Gas", Symbol = "x_{gas2}", Hidden = true);
172	y_gas_2(NComp) as fraction (Brief = "Fraction of Vapour in Gas", Symbol = "y_{gas2}", Hidden = true);
173	v_gas_2 as fraction (Brief = "Fraction of Vapour in Mixture_Gas", Symbol = "v_{gas2}", Hidden = true);
174	x_air_1(NComp) as fraction (Brief = "Fraction of Liquids in Air", Symbol = "x_{air1}", Hidden = true);
175	y_air_1(NComp) as fraction (Brief = "Fraction of Vapour in Air", Symbol = "y_{air1}", Hidden = true);
176	v_air_1 as fraction (Brief = "Fraction of Vapour in Mixture_Air", Symbol = "v_{air1}", Hidden = true);
177	x_air_2(NComp) as fraction (Brief = "Fraction of Liquids in Air", Symbol = "x_{air2}", Hidden = true);
178	y_air_2(NComp) as fraction (Brief = "Fraction of Vapour in Air", Symbol = "y_{air2}", Hidden = true);
179	v_air_2 as fraction (Brief = "Fraction of Vapour in Mixture_Air", Symbol = "v_{air2}", Hidden = true);
180
181	SET
182	Gas.Phase = "Vapour";
183	Ash.Phase = "Vapour";
184
185	#*-------------------------------------------------------------------
186	* Equacoes do modelo
187	--------------------------------------------------------------------#
188
189	EQUATIONS
190
191	"Global Molar Balance for Water/Steam Side"
192	Water.Fw = Steam.Fw;
193
194	"Steam Outlet Temperature"
195	Steam.T = T;
196
197	"Thermal Equilibrium Fuel Side"
198	Gas.T = Ash.T;
199
200	"Mechanical Equilibrium Water/Steam Side"
201	Steam.P = Water.P - Pdrop;
202
203	"Mechanical Equilibrium Fuel Side 1, array = [Air.P, Fuel.P]"
204	Gas.P = min([Air.P, Fuel.P]);
205
206	"Mechanical Equilibrium Fuel Side 2"
207	Gas.P = Ash.P;
208
209	"Enthalpy of Steam , array = [Steam.S, Steam.H]"
210	[Steam.S, Steam.H] = propterm.propPTv(Steam.P, Steam.T);
211
212	"Heat Exchanged"
213	(Steam.H - Water.H) * Water.Fw = q_ex + Inlet_q.Q;
214
215	"Ratio between component (i) production/consumption for the limiting component"
216	r(1:NComp+NCompS,:) = stoic(1:NComp+NCompS,:) * conv * z(limit);
217
218	if (NReac equal 1) then
219	"Component Molar Balance (Fluid Phase)"
220	Gas.Fluid.F * Gas.Fluid.z(1:NComp) = Fuel.Fluid.F * Fuel.Fluid.z(1:NComp) + Air.Fluid.F * Air.Fluid.z(1:NComp) + F * r(1:NComp,1);
221
222	"Component Molar Balance (Stoichiometric oxygen)"
223	FGas * zGas(1:NComp) = Fuel.Fluid.F * Fuel.Fluid.z(1:NComp) + Air.Fluid.F Air.Fluid.z(1:NComp) / (1+Ex_Air) + F r(1:NComp,1);
224
225	"Component Molar Balance (Solid Phase)"
226	Ash.Solid.F * Ash.Solid.z(1:NCompS) = Fuel.Solid.F * Fuel.Solid.z(1:NCompS) + Air.Solid.F * Air.Solid.z(1:NCompS) + F * r(NComp+1:NComp+NCompS,1);
227	else
228	"Component Molar Balance (Fluid Phase)"
229	Gas.Fluid.F * Gas.Fluid.z(1:NComp) = Fuel.Fluid.F * Fuel.Fluid.z(1:NComp) + Air.Fluid.F * Air.Fluid.z(1:NComp) + F * sumt(r(1:NComp,:));
230
231	"Component Molar Balance (Stoichiometric oxygen)"
232	FGas * zGas(1:NComp) = Fuel.Fluid.F * Fuel.Fluid.z(1:NComp) + Air.Fluid.F * Air.Fluid.z(1:NComp) / (1+Ex_Air) + F * sumt(r(1:NComp,:));
233
234	"Component Molar Balance (Solid Phase)"
235	Ash.Solid.F * Ash.Solid.z(1:NCompS) = Fuel.Solid.F * Fuel.Solid.z(1:NCompS) + Air.Solid.F * Air.Solid.z(1:NCompS) + F * sumt(r(NComp+1:NComp+NCompS, :));
236	end
237
238	"Sum of Molar Fractions for the Outlet Gas"
239	sum(Gas.Fluid.z) = 1;
240
241	"Sum of Molar Fractions for the Outlet Ash"
242	sum(Ash.Solid.z) = 1;
243
244	"Sum of Molar Fractions (Stoichiometric oxygen)"
245	sum(zGas) = 1;
246
247	"Stoichiometric oxygen"
248	zGas(flu.O2) = 0;
249
250	"Molar Enthalpy of Gas at 298.15 K"
251	[v_gas_1, x_gas_1, y_gas_1] = PP.Flash(298.15 * 'K', 1 * 'atm', Gas.Fluid.z);
252
253	"Molar Enthalpy of Gas at Outlet Gas Temperature"
254	[v_gas_2, x_gas_2, y_gas_2] = PP.Flash(Gas.T, Gas.P, Gas.Fluid.z);
255
256	"Molar Enthalpy Delta for the Gas Between 298.15 K and the Outlet Gas Temperature"
257	h_gas = (v_gas_2 * PP.VapourEnthalpy(Gas.T, Gas.P, y_gas_2) + (1 - v_gas_2) * PP.LiquidEnthalpy(Gas.T, Gas.P, x_gas_2))
258	- (v_gas_1 * PP.VapourEnthalpy(298.15 * 'K', 1 * 'atm', y_gas_1) + (1 - v_gas_1) * PP.LiquidEnthalpy(298.15 * 'K', 1 * 'atm', x_gas_1))
259	;
260
261	"Molar Enthalpy of Air at 298.15 K"
262	[v_air_1, x_air_1, y_air_1] = PP.Flash(298.15 * 'K', 1 * 'atm', Air.Fluid.z);
263
264	"Molar Enthalpy of Gas at Inlet Air Temperature"
265	[v_air_2, x_air_2, y_air_2] = PP.Flash(Air.T, Air.P, Air.Fluid.z);
266
267	"Molar Enthalpy Delta for the Air Between 298.15 K and the Inlet Air Temperature"
268	h_air = (v_air_1 * PP.VapourEnthalpy(298.15 * 'K', 1 * 'atm', y_air_1) + (1 - v_air_1) * PP.LiquidEnthalpy(298.15 * 'K', 1 * 'atm', x_air_1))
269	- (v_air_2 * PP.VapourEnthalpy(Air.T, Air.P, y_air_2) + (1 - v_air_2) * PP.LiquidEnthalpy(Air.T, Air.P, x_air_2))
270	;
271
272	"Molar Enthalpy Delta for the Ash Between 298.15 K and the Outlet Ash Temperature"
273	h_ash = PPS.VapourEnthalpy(Ash.T, Ash.P, Ash.Solid.z) - PPS.VapourEnthalpy(298.15 * 'K', Ash.P, Ash.Solid.z);
274
275	"Molar Enthalpy Delta for the Fuel Between 298.15 K and the Inlet Fuel Temperature (Solid Phase)"
276	h_bag_sol = PPS.VapourEnthalpy(298.15 * 'K', Fuel.P, Fuel.Solid.z) - PPS.VapourEnthalpy(Fuel.T, Fuel.P, Fuel.Solid.z);
277
278	"Molar Enthalpy Delta for the Fuel Between 298.15 K and the Inlet Fuel Temperature (Fluid Phase)"
279	h_bag_fluid = PP.LiquidEnthalpy(298.15 * 'K', Fuel.P, Fuel.Fluid.z) - PP.LiquidEnthalpy(Fuel.T, Fuel.P, Fuel.Fluid.z);
280
281	"Energy Balance"
282	q_comb = q_ex + q_losses;
283
284	"Heat Losses"
285	q_losses = q_HHV * f_losses;
286
287	"Heat of Combustion at the Operational Temperature"
288	-q_comb = Air.Fluid.F * h_air + Fuel.Solid.F * h_bag_sol + F * sum(h conv z(limit)) + Fuel.Fluid.F * h_bag_fluid
289	+ Gas.Fluid.F * h_gas + Ash.Solid.F * h_ash;
290
291	"Higher Heating Value (Heat)"
292	-q_HHV = F * sum(h conv z(limit));
293
294	"Lower Heating Value (Heat)"
295	#q_LHV = q_HHV - (Outlet_Gas.F * Outlet_Gas.z(1) * M(1) - Inlet_Mass.F * Inlet_Mass.z(1) * M(1)) * 2464.67 * 'kJ/kg';#(API)
296	#q_LHV = q_HHV - Outlet_Gas.F * Outlet_Gas.z(1) * M(1) * 2464.67 * 'kJ/kg'; #(calor de vaporizacao a 15.15 graus celsius)
297	q_LHV = q_HHV - Gas.Fluid.Fw * Gas.Fluid.zw(flu.Water) * 2442.1 * 'kJ/kg'; #(calor de vaporizacao a 25 graus celsius)
298
299	"Higher Heating Value - Wet Basis"
300	HHV_wet * Fuel.Total.Fw = q_HHV;
301
302	"Higher Heating Value - Dry Basis"
303	HHV_dry * (Fuel.Total.Fw - Fuel.Fluid.Fw * Fuel.Fluid.z(flu.Water))= q_HHV;
304
305	"Lower Heating Value - Wet Basis"
306	LHV * Fuel.Total.Fw = q_LHV;
307
308	"Specific Production of Steam"
309	v_specific * Fuel.Total.Fw = Steam.Fw;
310
311	"Heat Transfer Efficiency (Lower Heating Value)"
312	Efficiency_LHV * q_LHV = q_ex;
313
314	"Heat Transfer Efficiency (Higher Heating Value)"
315	Efficiency_HHV * q_HHV = q_ex;
316
317	"Air Humidity"
318	humidity * (Air.Fluid.Fw - Air.Fluid.Fw * Air.Fluid.zw(flu.Water)) = Air.Fluid.Fw * Air.Fluid.zw(flu.Water);
319
320	"Total Inlet Composition (Fluid Phase)"
321	F * z(1:NComp) = Fuel.Fluid.F * Fuel.Fluid.z + Air.Fluid.F * Air.Fluid.z;
322
323	"Total Inlet Composition (Solid Phase)"
324	F * z(NComp + 1: NComp + NCompS) = Fuel.Solid.F * Fuel.Solid.z + Air.Solid.F * Air.Solid.z;
325
326	"Total Inlet Stream Flow"
327	F = Fuel.Fluid.F + Fuel.Solid.F + Air.Fluid.F + Air.Solid.F;
328
329	"Outlet Composition (Fluid Phase)"
330	Gas.Fluid.z = Ash.Fluid.z;
331
332	"Outlet Composition (Solid Phase)"
333	Gas.Solid.z = Ash.Solid.z;
334
335	"Solids in Gas Outlet"
336	Gas.Solid.F = 1e-6 * 'kmol/h';
337
338	"Gases in Solid Outlet"
339	Ash.Fluid.F = 1e-6 * 'kmol/h';
340
341	end
342
343
344	FlowSheet teste_boiler
345
346	#*-------------------------------------------------------------------
347	* Declaracao de dispositivos (ou blocos contendo o modelo)
348	--------------------------------------------------------------------#
349
350	DEVICES
351	S101 as main_sourceR;
352	S102 as water_sourceR;
353	S103 as main_sourceR;
354	B101 as boiler;
355	E101 as heat_sourceR;
356
357	#*-------------------------------------------------------------------
358	* Especifica as conexoes entre os modelos
359	--------------------------------------------------------------------#
360
361	CONNECTIONS
362	S103.Outlet to B101.Air;
363	S101.Outlet to B101.Fuel;
364	S102.Outlet to B101.Water;
365	E101.Outlet_q to B101.Inlet_q;
366
367	#*-------------------------------------------------------------------
368	* Define o valor dos parametros declarados no modelo
369	--------------------------------------------------------------------#
370
371	SET
372	S101.ValidPhases = "Liquid-Only";
373	S102.ValidPhases = "Liquid-Only";
374	S103.ValidPhases = "Vapour-Only";
375	NComp = PP.NumberOfComponents();
376	NCompS = PPS.NumberOfComponents();
377	B101.NReac = 3;
378
379	B101.stoic (:,1) = [5, 0, 0, 0, 0, 6, 0, -6, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0]; # Reaction 1:cellulose(C6H10O5) + 6O2 --> 5H2O + 6CO2
380	B101.stoic (:,2) = [4, 0, 0, 0, 0, 5, 0, -5, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0]; # Reaction 2:hemicellulose(C5H8O4) + 5O2 --> 4H2O + 5CO2
381	B101.stoic (:,3) = [5.8, 0, 0, 0, 0, 10, 0, -10.95, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0]; # Reaction 3:lignina(C10H11.6O3.9) + 10.95O2 --> 5.8H2O + 10CO2
382	B101.h = [-2575, -1954, -4401] * 'kJ/mol';
383	B101.limit = [NComp+sol.Cellulose,NComp+sol.Hemicell, NComp+sol.Lignin];
384
385
386	#*-------------------------------------------------------------------
387	* Especifica variaveis definidas no modelo
388	--------------------------------------------------------------------#
389
390	SPECIFY
391	S101.Fluid.Fw = 50000 * 'kg/h';
392	S101.Solid.Fw = 50000 * 'kg/h';
393	S101.T = 338.15 * 'K';
394	S101.P = 1 * 'atm';
395	S101.CompositionOfSolid = [0.4385, 0.2564, 0.233, 0.0285, 0, 0, 0, 0.043, 0];
396	S101.CompositionOfFluid = [1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
397
398	S102.T = 383.15 * 'K';
399	S102.P = 67 * 'bar';
400
401	S103.Solid.F = 1e-6 * 'kmol/h';
402	S103.T = 303.15 * 'K';
403	S103.P = 1 * 'atm';
404	S103.CompositionOfSolid = [0.25, 0.20, 0.55, 0, 0, 0, 0, 0, 0];
405	S103.CompositionOfFluid = [0.013, 0, 0, 0, 0, 0, 0, 0.31, 0.677, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];#(massico-ar umido)
406
407	B101.Efficiency_LHV = 0.85;
408	B101.Gas.T = 423.15 * 'K'; #150C
409	B101.T = 763.15 * 'K';
410	B101.Pdrop = 0 * 'bar';
411	B101.conv = [1, 1, 1];
412	B101.Ex_Air = 0.5;
413	B101.Inlet_q.Q = 0 * 'kW';
414
415	#*-------------------------------------------------------------------
416	#Parametros
417	--------------------------------------------------------------------#
418
419	PARAMETERS
420	PP as Plugin (Brief = "External Physical Properties",
421	Type="PP",
422	Project = "../Flowsheets/v2_2/Fluid_v2_2.vrtherm"
423	);
424	PPS as Plugin (Brief = "External Physical Properties",
425	Type="PP",
426	Project = "../Flowsheets/v2_2/Solid_v2_2.vrtherm"
427	);
428
429	NComp as Integer (Brief = "Number of chemical components in the fluid phase");
430	NCompS as Integer (Brief = "Number of chemical components in the solid phase");
431	flu as ConstituentFluid(Symbol = " ", Protected = true);
432	sol as ConstituentSolid(Symbol = " ", Protected = true);
433	#*-------------------------------------------------------------------
434	* Define o valor dos parametros declarados no modelo
435	--------------------------------------------------------------------#
436
437	SET
438	NComp = PP.NumberOfComponents();
439	NCompS = PPS.NumberOfComponents();
440	S101.CompositionBasis = "Mass";
441	S103.CompositionBasis = "Mass";
442
443	#*-------------------------------------------------------------------
444	* Condicoes iniciais e opcoes de Solver
445	--------------------------------------------------------------------#
446
447	OPTIONS
448	Dynamic = false;
449	Integration = "original";
450	NLASolver(
451	File = "sundials",
452	RelativeAccuracy = 1e-3,
453	AbsoluteAccuracy = 1e-6,
454	MaxIterations = 100
455	);
456	DAESolver(
457	File = "dassl",
458	RelativeAccuracy = 1e-3,
459	AbsoluteAccuracy = 1e-6,
460	EventAccuracy = 1e-2
461	);
462	end
463

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