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var1_2_teste.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: 103.6 KB

Line
1	#*-------------------------------------------------------------------
2	* Biorrefinaria Virtual
3	*--------------------------------------------------------------------
4	* Nome do arquivo: var1_2_pinch_evap_econ.mso
5	* Projeto: producao de etanol 1G e 2G
6	* Conteudo: Maxima producao de etanol. Soh queimando o
7	* bagaco necessario para atender a demanda do processo
8	* (baixa carga de solidos). Sem turbina de condensacao no CHP.
9	* Etanol anidro do C12/C6/C5
10	* Integracao energetica atraves da analise pinch
11	* 5 evaporadores na etapa de concentracao do caldo
12	* 3 evaporadores na etapa de concentracao da xylose
13	--------------------------------------------------------------------#
14
15	#*-------------------------------------------------------------------
16	*
17	* versao 2.3
18	* Data: 11/2019
19	* Atualizada por: Andreza A. Longati, Andrew Elias
20	* Utiliza a versao 2.2 da biorrefinaria
21	*
22	*--------------------------------------------------------------------
23	*Descricao: simulacao da producao de E1G e E2G
24	--------------------------------------------------------------------
25
26	*--------------------------------------------------------------------
27	*Notas: Cada componente eh representado na simulacao por um Index number
28	* Abaixo segue o Index number para cada componente
29	-- fase fluida
30	* 1 - agua
31	* 2 - sacarose
32	* 3 - glicose
33	* 4 - xilose
34	* 5 - etanol
35	* 6 - CO2
36	* 7 - CO
37	* 8 - O2
38	* 9 - N2
39	* 10 - H2
40	* 11 - CH4
41	* 12 - amonia
42	* 13 - lignina
43	* 14 - xilana
44	* 15 - acido acetico
45	* 16 - furfural
46	* 17 - hidroximetilfurfural (HMF)
47	* 18 - glicerol
48	* 19 - Solunkn (acucares desconhecidos)
49	* 20 - MEG (monoetilenoglicol)
50	* 21 - H2SO4
51	* 22 - acido fosforico
52	* 23 - impurezas
53	* 24 - celobiose
54	* 25 - hidroxido de amonia
55
56	-- fase solida
57	* 1(26) - celulose
58	* 2(27) - xilana (hemicelulose)
59	* 3(28) - lignina
60	* 4(29) - cinzas
61	* 5(30) - enzima
62	* 6(31) - levedura
63	* 7(32) - hidroxido de calcio
64	* 8(33) - fosfato de calcio
65	* 9(34) - impurities
66	--------------------------------------------------------------------#
67
68	using "assumptions";
69	using "separators/dry_cleaning";
70	using "mixers_and_splitters/mixer_and_splitter_m";
71	using "separators/mill";
72	using "separators/sieve";
73	using "heat_exchangers/heater_m";
74	using "reactors/liming_tank";
75	using "pressure_changers/pump_m";
76	using "separators/flash_m";
77	using "separators/decanter";
78	using "separators/filter";
79	using "separators/evaporator";
80	using "mixers_and_splitters/mixer_and_splitter_w";
81	using "reactors/stoic_reactor";
82	using "reactors/fermenter";
83	using "separators/absorption_tower";
84	using "separators/centrifuge";
85	using "heat_exchangers/heater_w";
86	using "separators/column";
87	using "separators/separator";
88	using "reactors/boiler";
89	using "pressure_changers/turbine_w";
90	using "separators/flash_w";
91	using "pressure_changers/pump_w";
92	using "heat_exchangers/Modelo_pinch";
93	using "environmental_assumptions";
94	using "economic_assumptions";
95
96	FlowSheet var1_2_teste
97	#------------------------ Parte comum ---------------------------#
98	PARAMETERS
99	PP as Plugin (Brief = "External Physical Properties",
100	Type="PP",
101	Project = "../Flowsheets/v2_2/Fluid_v2_2.vrtherm"
102	);
103	PPS as Plugin (Brief = "External Physical Properties",
104	Type="PP",
105	Project = "../Flowsheets/v2_2/Solid_v2_2.vrtherm"
106	);
107
108	NComp as Integer;
109	NCompS as Integer;
110
111	ProPar as Assumptions (Brief = "Model With All the Assumptions Made");
112	flu as ConstituentFluid (Brief = "Indexes of All Compounds in the Fluid Phase", Symbol = " ", Protected = true);
113	sol as ConstituentSolid (Brief = "Indexes of All Compounds in the Solid Phase", Symbol = " ", Protected = true);
114
115	SET
116	#number of components in the liquid and solid phase
117	NComp = PP.NumberOfComponents();
118	NCompS = PPS.NumberOfComponents();
119
120	#---------------------- extracao -----------------------#
121	DEVICES
122	MSS101 as main_sourceR;# entrada de cana crua no processo
123	MSS102 as main_sourceR;#entrada de palha no processo
124	DCL101 as dry_cleaning; #limpeza a seco da cana
125
126	MSS103 as main_sourceL; #fonte de terra da palha enfardada
127
128	mSP102 as splitter_mL; #splitter da eficiencia de remocao da terra
129
130	MSS104 as main_sourceL; #fonte de palha enfardada
131
132	mMX103 as mixer2_mR; #misturador da palha enfardada e terra nao liberada
133	mMX104 as mixer2_mR; #misturador da palha enfardada e palha da impureza vegetal
134
135	MSS105 as main_sourceL;#agua que alimenta o primeiro terno (nulo)
136	MLL105 as mill; #primeiro terno da moenda
137
138	MLL106 as mill; #segundo terno da moenda
139
140	MLL107 as mill; #terceiro terno da moenda
141
142	MLL108 as mill; #quarto terno da moenda
143
144	MSS106 as main_sourceR;# agua que alimenta o quinto terno
145
146	MLL109 as mill; #quinto terno da moenda
147
148	mMX110 as mixer2_mR; #misturador para o caldo primario e secundario
149
150	SIE111 as sieve; #peneira para o caldo primario e secundario
151
152	mMX112 as mixer2_mR; #misturador para o bagaco do primeiro terno e torta da peneira
153
154	CONNECTIONS
155	MSS101.Outlet to DCL101.CrudeCane; #cana-de-acucar para limpeza a seco
156	MSS102.Outlet to DCL101.InletStraw; #palha para limpeza a seco
157
158	MSS103.Outlet to mSP102.Inlet; #terra para splitter da limpeza
159	#MSS104.Outlet to mMX103.Inlet1; #Fonte de palha enfardada
160
161	mSP102.Outlet1 to mMX103.Inlet2; #resto da terra para limpeza
162
163	mMX103.Outlet to mMX104.Inlet1; #palha enfardada para mixer da caldeira
164	DCL101.OutletStraw to mMX104.Inlet2; #palha (impureza vegetal) para mixer da caldeira
165
166	DCL101.SugarCane to MLL105.Cane; #cana limpa para primeiro terno
167	MSS105.Outlet to MLL105.Water; #agua (nula) para o primeiro terno
168
169	mMX112.Outlet to MLL106.Cane; #misturador para segundo terno da moenda
170	MLL107.MixedJuice to MLL106.Water; #caldo do terceiro para o segundo terno
171
172	MLL106.Bagasse to MLL107.Cane; #cana do segundo para o terceiro terno
173	MLL108.MixedJuice to MLL107.Water; #caldo do quarto pro terceiro terno
174
175	MLL107.Bagasse to MLL108.Cane; #cana do terceiro para o quarto terno
176	MLL109.MixedJuice to MLL108.Water; #caldo do quinto pro quarto terno
177
178	MLL108.Bagasse to MLL109.Cane; #cana do quarto para o quinto terno
179	MSS106.Outlet to MLL109.Water; #agua para o quinto terno
180
181	MLL105.MixedJuice to mMX110.Inlet1; #caldo primario para o mixer
182	MLL106.MixedJuice to mMX110.Inlet2; #caldo secundario para o mixer
183
184	mMX110.Outlet to SIE111.Inlet; #misturador dos caldos para peneira
185
186	SIE111.SieveCake to mMX112.Inlet1; #torta da peneira para misturador
187	MLL105.Bagasse to mMX112.Inlet2; #bagaco do primeiro terno para misturador
188
189	MLL109.Bagasse to mSP124.Inlet; #bagaco para splitter
190
191	mSP124.Outlet1 to mSP125.Inlet; #splitter para splitter
192
193	mSP125.Outlet1 to mSP126.Inlet; #splitter para splitter
194
195	SET
196	#entrada de cana-de-acucar
197	MSS101.ValidPhases = "Liquid-Only";
198	MSS101.CompositionBasis = "Mass";
199
200	#entrada de palha no processo
201	MSS102.ValidPhases = "Liquid-Only";
202	MSS102.CompositionBasis = "Mass";
203
204	#entrada de palha enfardada no processo
205	MSS103.ValidPhases = "Liquid-Only";
206	MSS103.CompositionBasis = "Mass";
207
208	#entrada de terra da palha enfardada no processo
209	MSS104.ValidPhases = "Liquid-Only";
210	MSS104.CompositionBasis = "Mass";
211
212	#agua para o primeiro terno
213	MSS105.ValidPhases = "Liquid-Only";
214	MSS105.CompositionBasis = "Mass";
215
216	#primeiro terno
217	MLL105.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
218	#segundo terno
219	MLL106.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
220	#terceiro terno
221	MLL107.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
222	#quarto terno
223	MLL108.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
224	#quinto terno
225	MLL109.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
226
227	#agua para o sexto terno
228	MSS106.ValidPhases = "Liquid-Only";
229	MSS106.CompositionBasis = "Mass";
230
231	SPECIFY
232	#entrada de cana-de-acucar
233	MSS101.CompositionOfFluid = ProPar.SugarcaneComposition;
234	MSS101.CompositionOfSolid = ProPar.SugarcaneCompositionSolid;
235	MSS101.T = ProPar.roomT;
236	MSS101.P = 1 * 'atm';
237
238	#entrada de palha no processo (impureza vegetal)
239	MSS102.CompositionOfFluid = ProPar.StrawComposition;
240	MSS102.CompositionOfSolid = ProPar.StrawCompositionSolid;
241	MSS102.T = ProPar.roomT;
242	MSS102.P = 1 * 'atm';
243
244	#limpeza a seco
245	DCL101.Cleaning_effVeg = 0.65;
246	DCL101.Cleaning_effMin = 0.70; #http://www.jacare.ind.br/Limpeza-de-Cana-Seco-por-Ventilacao.php
247	#DCL101.SugarLosses = 0.005;
248	DCL101.SugarLosses = 1e-6 ;
249	DCL101.Fiber_cane = ProPar.SugarcaneFiber;
250	DCL101.Duty = ProPar.DryCleaningDuty;
251
252	#terra da palha que entra enfardada
253	MSS103.CompositionOfFluid(1) = 1;
254	MSS103.CompositionOfFluid(2:NComp) = 0;
255	MSS103.CompositionOfSolid = [0, 0, 0, 0, 0, 0, 0, 0, 1];
256	MSS103.T = ProPar.roomT;
257	MSS103.P = 1 * 'atm';
258	MSS103.Fluid.Fw = 1e-6 * 'kg/h';
259	MSS103.Solid.Fw = 1e-6 * 'kg/h';
260
261	#Limpeza da palha enfardada
262	#mSP102.frac = 0.65;
263	mSP102.frac = 0.70;
264
265	#palha que entra enfardada
266	MSS104.CompositionOfFluid = ProPar.StrawComposition_baled;
267	MSS104.CompositionOfSolid = ProPar.StrawCompositionSolid_baled;
268	MSS104.T = ProPar.roomT;
269	MSS104.P = 1 * 'atm';
270
271	#agua para o primeiro terno
272	MSS105.CompositionOfFluid(1) = 1;
273	MSS105.CompositionOfFluid(2:NComp) = 0;
274	MSS105.CompositionOfSolid = [0.431, 0.252, 0.229, 0.028, 0, 0, 0, 0, 0];
275	#######
276	#MSS105.Solid.Fw = 1 * 'kg/h';
277	MSS105.Solid.Fw = 1e-6 * 'kg/h';
278	MSS105.T = ProPar.roomT;
279	MSS105.P = 1 * 'atm';
280
281	#primeiro terno
282	MLL105.WFPTC = 0;
283	MLL105.Duty = ProPar.MillDuty;
284	MLL105.humidity = 0.56;
285	MLL105.frac_sol = 0.9;
286
287	#segundo terno
288	MLL106.Duty = ProPar.MillDuty;
289	MLL106.humidity = 0.58;
290	MLL106.frac_sol = 0.9;
291	MLL106.Extract = 0.617;
292
293	#terceiro terno
294	MLL107.Duty = ProPar.MillDuty;
295	MLL107.humidity = 0.55;
296	MLL107.frac_sol = 0.9;
297	MLL107.Extract = 0.588;
298
299	#quarto terno
300	MLL108.Duty = ProPar.MillDuty;
301	MLL108.humidity = 0.53;
302	MLL108.frac_sol = 0.9;
303	MLL108.Extract = 0.554;
304
305	#quinto terno
306	MLL109.Duty = ProPar.MillDuty;
307	MLL109.humidity = 0.5;
308	MLL109.frac_sol = 0.9;
309	MLL109.Extract = 0.472;
310
311	#agua para o quinto terno
312	MSS106.CompositionOfFluid(1) = 1;
313	MSS106.CompositionOfFluid(2:NComp) = 0;
314	MSS106.CompositionOfSolid = [0.431, 0.252, 0.229, 0.028, 0, 0, 0, 0, 0];
315	MSS106.Solid.Fw = 1e-6 * 'kg/h';
316	#MSS106.T = 323.15 * 'K';
317	MSS106.T = (60 + 273.15) * 'K';
318	MSS106.P = 1 * 'atm';
319
320	#peneira
321	SIE111.frac_per = 0.88;
322	SIE111.humidity = 0.72;
323	SIE111.frac_insol = 0.92;
324
325	#splitter reserva de bagaco
326	mSP124.frac = 0.95;
327
328	VARIABLES
329	#frac_E2G as fraction (Brief = "E2G Mass Fraction for the Process", Default = 0.5);
330
331	EQUATIONS
332	#Quantidade de cana que entra na usina
333	MSS101.Outlet.Total.Fw = ProPar.SugarcaneFlow;
334
335	#Quantidade de palha que entra como impureza vegetal
336	MSS102.Outlet.Total.Fw = 0.048 * (MSS101.Outlet.Total.Fw + MSS102.Outlet.Total.Fw);
337
338	#Umidade da palha que entra como impureza vegetal
339	MSS102.Outlet.Total.zw(flu.Water) = ProPar.humidity_straw;
340
341	#Umidade da palha que entra como fardo
342	MSS104.Outlet.Total.zw(flu.Water) = ProPar.humidity_baled_straw;
343
344	#Vazao de palha que entra enfardada
345	#Vazao total * (1 - umidade da palha) = (fracao que eh trazida do campo) * (producao especifica) * vazao de cana - o que jah vem como impureza vegetal
346	MSS104.Outlet.Total.Fw * (1 - ProPar.humidity_baled_straw) = 0.5 * 140 * 'kg/t' * MSS101.Outlet.Total.Fw - MSS102.Outlet.Total.Fw * (1 - ProPar.humidity_straw);
347
348	#Recuperacao global dos acucares com base na quantidade que entra na primeira moenda
349	ProPar.SugarRecovery * MLL105.Cane.Fluid.Fw * (MLL105.Cane.Fluid.zw(flu.Sucrose) + MLL105.Cane.Fluid.zw(flu.Glucose)) =
350	SIE111.Permeate.Fluid.Fw * (SIE111.Permeate.Fluid.zw(flu.Sucrose) + SIE111.Permeate.Fluid.zw(flu.Glucose));
351
352	#Agua adicionada ao quinto terno (Com base no total de cana que eh moida)
353	ProPar.SoakingWater * ProPar.SugarcaneFlow = MSS106.Fluid.Fw;
354	#*
355	*#
356	#* A simulacao foi construida de forma a maximizar a producao de etanol 2G.
357	A fracao de bagaco que entra na caldeira eh a variavel controle.
358	Em situacoes onde todo o bagaco eh desviado para o 2G (mSP126.frac = 1)
359	a quantidade de palha enfardada eh calculada (atraves do balanco de energia)
360	*#
361
362	DEVICES
363	mSP103 as splitter_mL; #splitter para uso da palha
364
365	CONNECTIONS
366	MSS104.Outlet to mSP103.Inlet;
367	mSP103.Outlet1 to mMX103.Inlet1;
368
369	PARAMETERS
370	StrawSwitcher as Switcher (Valid = ["On", "Off"], Default = "Off");
371
372	EQUATIONS
373
374	switch StrawSwitcher
375	case "Off":
376	mSP103.Outlet2.Total.Fw = 1e-2 *'kg/h';
377	when mSP126.frac >= 1 switchto "On";
378
379	case "On":
380	mSP126.frac = 1;
381	when mSP103.frac >= 1 switchto "Off";
382	end
383	#*
384	*#
385	#------------------------- tratamento -----------------------------#
386	DEVICES
387	mMX113 as mixer2_mR; #misturador para o bagaco do primeiro terno e torta da peneira
388
389	LTS115 as liming_tank; #tanque de calagem
390	MSS107 as main_sourceR; #fonte de acido fosforico
391	MSS108 as main_sourceR; #fonte de hidroxido de calcio
392
393	mPP116 as pump_mL; #primeira bomba
394	PSS101 as power_sourceR; #potencia para a primeira bomba
395
396	mFL118 as exo_flash; #flash
397
398	MSS109 as main_sourceR;#polimero para o decantador
399
400	mMX119 as mixer2_mR; #misturador (caldo e polimero)
401
402	DEC120 as decanter3; #decantador
403
404	MSS110 as main_sourceL;#agua para filtracao na planta 1G
405	mMX121 as mixer2_mR; #misturador (lodo e agua)
406
407	mMX122 as mixer2_mR; #misturador (lodo+agua e bagacilho)
408
409	FLT123 as filter; #filtro de tambor rotativo
410
411	mSP124 as splitter_mL; #splitter do bagaco (reserva de bagaco)
412
413	mSP125 as splitter_mL; #splitter do bagaco (bagacilho para filtro)
414
415	mSP126 as splitter_mL; #splitter do bagaco (bagaco para 2G)
416	#*
417	*#
418	CONNECTIONS
419	SIE111.Permeate to mMX113.Inlet1; #filtrado da peneira misturador
420	FLT123.Filtrate to mMX113.Inlet2; #filtrado para misturador
421
422	#mMX113.Outlet to pinch to LTS115.Inlet; #misturador para o pinch para o tanque de calagem
423
424	MSS107.Outlet to LTS115.Acid; #fonte de acido fosforico para o tanque de calagem
425	MSS108.Outlet to LTS115.Lime; #fonte de hidroxido de calcio para o tanque de calagem
426
427	LTS115.Outlet to mPP116.Inlet; #caldo para primeira bomba
428	PSS101.Outlet_p to mPP116.Inlet_p; #potencia para a primeira bomba
429
430	#mPP116.Outlet to pinch to mFL118.Inlet ; #primeira bomba para o pinch para o flash
431
432	mFL118.OutletL to mMX119.Inlet1; #flash para misturador
433	MSS109.Outlet to mMX119.Inlet2; #polimero para misturador
434
435	mMX119.Outlet to DEC120.Inlet; #misturador para decantador
436
437	DEC120.Sludge to mMX121.Inlet1; #lodo do decantador para misturador
438	MSS110.Outlet to mMX121.Inlet2; #agua para misturador
439
440	mMX121.Outlet to mMX122.Inlet1; #agua+lodo para misturador
441	mSP125.Outlet2 to mMX122.Inlet2; #bagacilho para misturador
442
443	mMX122.Outlet to FLT123.Inlet; #misturador para filtro de tambor rotativo
444
445	SET
446
447	#fonte de acido fosforico
448	MSS107.ValidPhases = "Liquid-Only";
449	MSS107.CompositionBasis = "Mass";
450
451	#fonte de cal
452	MSS108.ValidPhases = "Liquid-Only";
453	MSS108.CompositionBasis = "Mass";
454
455	#tanque de calagem
456	LTS115.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
457	LTS115.NReac = 2;
458	LTS115.stoic (:,1) = [2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -2/3, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 1/3, 0]; # Reaction 1: 1.Ca(OH)2 + 2/3.H3PO4 --> 1/3Ca3(PO4)2 + 2H2O
459	LTS115.stoic (:,2) = [0, 0, 0, 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, 0, 0, 0, 0, 1]; # Reaction 1: Impurities(fluida) --> Impurities(solido)
460	LTS115.h = [0, 0] * 'kJ/kmol';
461	LTS115.density = 1000 * 'kg/m^3';
462	LTS115.SugarcaneFlow = ProPar.SugarcaneFlow;
463	LTS115.limit = [NComp+sol.CaOH2, flu.Impurities];
464
465	#primeira bomba
466	mPP116.density = 1000 * 'kg/m^3';
467
468	#polimero
469	MSS109.ValidPhases = "Liquid-Only";
470	MSS109.CompositionBasis = "Mass";
471
472
473	#decantador
474	DEC120.Brix = [0, 1, 1, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0];
475
476	#agua de lavagem do filtro
477	MSS110.ValidPhases = "Liquid-Only";
478	MSS110.CompositionBasis = "Mass";
479
480
481
482	SPECIFY
483
484	#fonte de acido fosforico
485	MSS107.CompositionOfFluid = [0.85, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0.15, 0, 0, 0];
486	MSS107.CompositionOfSolid = [0, 0, 0, 0, 0, 0, 1.0, 0, 0];
487	MSS107.Solid.Fw = 1e-6 * 'kg/h';
488	MSS107.T = (70 + 273.15) * 'K';
489	MSS107.P = 1 * 'atm';
490
491	#fonte de cal
492	MSS108.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, 0];
493	MSS108.CompositionOfSolid = [0, 0, 0, 0, 0, 0, 1.0, 0, 0];
494	MSS108.T = (70 + 273.15) * 'K';
495	MSS108.P = 1 * 'atm';
496
497	#tanque de calagem
498	LTS115.KCPTC = 1.057 * 'kg/t';
499	LTS115.LFPTJ = 17.6 * 'kg/t';
500	LTS115.Ex_Acid = 0;
501	LTS115.conv = [1.0, 1.0];
502	LTS115.T = (70 + 273.15) * 'K';
503	LTS115.reac_time = 48 * 'h';
504
505	#Bomba para garantir que nao vai evaporar nos trocadores
506	mPP116.PIn = 0.7 * 'atm';
507	mPP116.n = ProPar.PumpEff;
508
509	#Flash
510	mFL118.Pdrop = 0.7 * 'atm';
511	mFL118.OutletL.T = (98 + 273.15) * 'K';
512
513	#Fonte de polimero (soh considera agua)
514	MSS109.CompositionOfFluid(1) = 1;
515	MSS109.CompositionOfFluid(2:NComp) = 0;
516	MSS109.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
517	MSS109.Solid.Fw = 1e-6 * 'kg/h';
518	MSS109.T = (98 + 273.15) * 'K';
519	MSS109.P = 1 * 'atm';
520
521	#Decantador
522	DEC120.Clarified.Fluid.T = (97 + 273.15) * 'K';
523	DEC120.frac_dec = 0.9;
524	DEC120.Sludge.Total.zw(flu.Water) = 0.91;
525	DEC120.frac_insol = 0.997;
526	DEC120.reac_time = 0.1 * 'h';
527
528	#agua que lava o lodo
529	MSS110.CompositionOfFluid(1) = 1;
530	MSS110.CompositionOfFluid(2:NComp) = 0;
531	MSS110.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
532	MSS110.Solid.Fw = 1e-6 * 'kg/h';
533	MSS110.T = (75 + 273.15) * 'K';
534	MSS110.P = 1 * 'atm';
535
536	#Filtro de tambor rotativo
537	#FLT123.frac_insol = 0.9;
538	FLT123.frac_insol = 0.9394; #conferir se acha referencia desse valor, uma vez que ele \C3 de um ausina real
539	#FLT123.humidity = 0.75;
540	FLT123.humidity = 0.70;
541	FLT123.FilterCake.Total.zw(flu.Sucrose) = 0.018; #antes estava 0.02 - referencia \C3 de 1.8% a 2.0%
542
543	EQUATIONS
544
545	#Quantidade de polimero adicionado ao decantador
546	ProPar.PolymerFraction * mMX119.Outlet.Total.Fw = MSS109.Fluid.Fw;
547
548	#bagacilho para filtro
549	mSP125.Outlet2.Total.Fw = ProPar.Pith_proportion * ProPar.SugarcaneFlow;
550
551	#Quantidade de agua adicionada
552	MSS110.Outlet.Total.Fw = ProPar.Water_filter * ProPar.SugarcaneFlow;
553
554	# Custo operacional - tratamento
555	Input_Treat = EcoPar.WorkedHours * (MSS107.Outlet.Total.Fw * EcoPar.FosfCost +
556	MSS108.Outlet.Total.Fw * EcoPar.CalCost +
557	MSS109.Outlet.Total.Fw * EcoPar.PolCost +
558	MSS110.Outlet.Total.Fw * EcoPar.WaterCost);
559
560	VARIABLES
561	Input_Treat as currency (Brief = "Operational expenditure in the treatment");
562	#*
563	*#
564
565	#------------------ concentracao e fermentacao --------------------#
566	DEVICES
567
568	mPP201 as pump_mL; #bomba para o caldo
569	PSS201 as power_sourceR; #potencia para a bomba
570
571	WSS201 as water_sourceR; #Fonte de vapor de processo
572	EVP202 as evaporator3; # 1 evaporador
573	EVP203 as evaporator3; # 2 evaporador
574	EVP204 as evaporator3; # 3 evaporador
575	EVP205 as evaporator3; # 4 evaporador
576	EVP206 as evaporator3; # 5 evaporador
577
578	mPP204 as pump_mL; #bomba para o caldo concentrado
579	PSS204 as power_sourceR; #potencia para a bomba
580
581	MSS202 as main_sourceR; #Fonte de amonia
582	mMX205 as mixer2_mR; #misturador para a amonia
583
584	mMX206 as mixer_mR; #misturador de levedura
585
586	RTS207 as stoic_reactor; #"reator" que converte sacarose em glicose...
587
588	FMS208 as stoic_fermenter; #dornas de fermentacao
589
590	MSS203 as main_sourceR; #fonte de agua para a torre de absorcao
591	ABT209 as absorption_tower; #torre de absorcao
592
593	CFG210 as centrifuge; #centrifuga
594	PSS202 as power_sourceR; #potencia para a bomba
595
596	#sequencia de misturadores...
597	mMX211 as mixer_mR; #misturador levedura e agua da torre de absorcao
598
599	MSS204 as main_sourceR; #fonte de agua para diluicao da levedura
600	mMX212 as mixer_mR; #misturador levedura e agua de diluicao
601
602	MSS205 as main_sourceR; #fonte de acido sulfurico
603	mMX213 as mixer_mR; #misturador levedura e acido sulfurico
604
605	mSP214 as splitter_mR; #purga de levedura
606
607	mMX608 as mixer_mR; #misturador caldo 1G e 2G
608
609	#*
610	*#
611	CONNECTIONS
612	DEC120.Clarified to mPP201.Inlet; #caldo clarificado para a bomba
613	PSS201.Outlet_p to mPP201.Inlet_p; #potencia para a bomba
614
615	mPP201.Outlet to mMX608.Inlet1; #caldo para o misturador
616	mPP607.Outlet to mMX608.Inlet2; # caldo 2G para o misturador
617
618	mMX608.Outlet to EVP202.Inlet; #caldo da bomba para o evaporador
619	WSS201.Outlet to EVP202.InletS; #vapor para o evaporador
620
621	EVP202.OutletL to EVP203.Inlet; #caldo para o evaporador
622	EVP202.OutletV to EVP203.InletS; #vapor vegetal para o evaporador
623
624	EVP203.OutletL to EVP204.Inlet; #caldo para o evaporador
625	EVP203.OutletV to EVP204.InletS; #vapor vegetal para o evaporador
626
627	EVP204.OutletL to EVP205.Inlet;#caldo para o evaporador
628	EVP204.OutletV to EVP205.InletS;#vapor vegetal para o evaporador
629
630	EVP205.OutletL to EVP206.Inlet;#caldo para o evaporador
631	EVP205.OutletV to EVP206.InletS;#vapor vegetal para o evaporador
632
633	EVP206.OutletL to mPP204.Inlet; #caldo concetrado para a bomba
634	PSS204.Outlet_p to mPP204.Inlet_p; #potencia para a bomba
635
636	#mPP204.Outlet to pinch to mMX205.Inlet1; #caldo concentrado para o pinch para o misturador
637
638	MSS202.Outlet to mMX205.Inlet2; #amonia para misturador
639
640	mMX205.Outlet to mMX206.Inlet1; #misturador para misturador
641
642	mMX206.Outlet to RTS207.Inlet; #misturador para "reator"
643
644	RTS207.Outlet to FMS208.Inlet; #"reator" para fermentador
645
646	MSS203.Outlet to ABT209.InletL; #fonte de agua para torre de absorcao
647	FMS208.Gas to ABT209.InletG; #gases da fermentacao para torre de absorcao
648
649	FMS208.Outlet to CFG210.Inlet; #fermentador para centrifuga
650	PSS202.Outlet_p to CFG210.Inlet_p; #trabalho para a centrifuga
651
652	CFG210.FilterCake to mMX211.Inlet1; #leite de levedura para misturador
653	ABT209.OutletL to mMX211.Inlet2; #agua da torre de absorcao para misturador
654
655	mMX211.Outlet to mMX212.Inlet1; #misturador para misturador
656	MSS204.Outlet to mMX212.Inlet2; #agua de diluicao para misturador
657
658	mMX212.Outlet to mMX213.Inlet1; #misturador para misturador
659	MSS205.Outlet to mMX213.Inlet2; #acido sulfurico para misturador
660
661	mMX213.Outlet to mSP214.Inlet; #misturador para purga
662
663	mSP214.Outlet1 to mMX206.Inlet2; #reciclo real da levedura
664	#*
665	*#
666	SET
667
668	#Bomba
669	mPP201.density = 1000 * 'kg/m^3';
670
671	#Bomba caldo concentrado
672	mPP204.density = 1000 * 'kg/m^3';
673
674	#Fonte de vapor
675	WSS201.ValidPhases = "Vapour-Liquid";
676
677	#Evaporador
678	EVP202.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];
679	EVP203.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];
680	EVP204.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];
681	EVP205.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];
682	EVP206.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];
683
684	#Fonte de amonia
685	MSS202.ValidPhases = "Liquid-Only";
686	MSS202.CompositionBasis = "Mass";
687
688	#"reator"
689	RTS207.NReac = 1;
690	#Reacao 1: C12H22O11 + H2O -> 2 C6H12O6
691	RTS207.stoic(:,1) = [-1, -1, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0 ,0];
692	RTS207.h = [0] * 'kJ/kmol';
693	RTS207.density = 1000 * 'kg/m^3';
694	RTS207.limit = [flu.Sucrose];
695
696	#fermentador
697	#reacoes:
698	# C6H12O6 -> 2C2H6O + 2CO2 conv = 90.48 %
699	# C6H12O6 + 2H2O -> 2C2H4O + 2CO2 + 4H2 conv = 1.19 %
700	# C6H12O6 + 2H2 -> 2C3H8O3 conv = 2.67 %
701	# 0.174C6H12O6 + 0.12NH3 -> CH1.74O0.6N0.12 + 0.355H2O + 0.045CO2 conv = 1.37 %
702	FMS208.NReac = 4;
703	#glucose to ethanol
704	FMS208.stoic (:,1) = [0, 0, -1, 0, 2, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
705	#glucose to acetic acid
706	FMS208.stoic (:,2) = [-1.5524, 0, -1, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
707	#glucose to glycerol
708	FMS208.stoic (:,3) = [-0.2238, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
709	#glucose to yeast
710	FMS208.stoic (:,4) = [2.0355, 0, -1, 0, 0, 0.2586, 0, 0, 0, 0, 0, -0.6897, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 5.7471, 0, 0, 0];
711	FMS208.limit = [flu.Glucose, flu.Glucose, flu.Glucose, flu.Glucose];
712	FMS208.h = [0, 0, 0, 0] * 'kJ/mol';
713	FMS208.Outlet.Phase = "Liquid";
714	FMS208.fermentation = "glucose";
715	FMS208.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];
716
717	#agua para torre de absorcao
718	MSS203.ValidPhases = "Liquid-Only";
719	MSS203.CompositionBasis = "Mass";
720
721	#torre de absorcao
722	ABT209.Target = flu.Ethanol;
723
724	#agua de diluicao da levedura
725	MSS204.ValidPhases = "Liquid-Only";
726	MSS204.CompositionBasis = "Mass";
727
728	#acido sulfurico
729	MSS205.ValidPhases = "Liquid-Only";
730	MSS205.CompositionBasis = "Mass";
731
732	#*
733	*#
734	SPECIFY
735	#Bomba
736	mPP201.Outlet.P = 1.7 * 'atm';
737	mPP201.n = ProPar.PumpEff;
738
739	#Bomba para caldo concentrado
740	mPP204.Outlet.P = 1 * 'atm';
741	mPP204.n = ProPar.PumpEff;
742
743	#Fonte de vapor
744	WSS201.P = 2.5 * 'bar';
745	WSS201.v = 1;
746
747	#Pressao evaporadores
748	EVP202.OutletV.P = 1.69 * 'bar';
749	EVP203.OutletV.P = 1.31 * 'bar';
750	EVP204.OutletV.P = 0.93 * 'bar';
751	EVP205.OutletV.P = 0.54 * 'bar';
752	EVP206.OutletV.P = 0.16 * 'bar';
753
754	#Brix final
755	EVP206.Outlet_Brix = 0.20; #18 - 22 de acordo com o chandel. Este intervalo no 2G.
756
757	#Fonte de amonia
758	MSS202.T = ProPar.roomT;
759	MSS202.P = 1 * 'atm';
760	MSS202.Solid.Fw = 1e-6 * 'kg/h';
761	MSS202.CompositionOfFluid = [0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
762	MSS202.CompositionOfSolid = [0.431, 0.252, 0.229, 0.028, 0, 0, 0, 0, 0];
763
764	#"reator"
765	RTS207.conv = [1];
766	RTS207.T = (30 + 273.15) * 'K';
767	RTS207.reac_time = 1 * 'h';
768
769	#fermentador
770	#reacoes:
771	# C6H12O6 -> 2C2H6O + 2CO2 conv = 90.48 %
772	# C6H12O6 + 2H2O -> 2C2H4O + 2CO2 + 4H2 conv = 1.19 %
773	# C6H12O6 + 2H2 -> 2C3H8O3 conv = 2.67 %
774	# 0.174C6H12O6 + 0.12NH3 -> CH1.74O0.6N0.12 + 0.355H2O + 0.045CO2 conv = 1.37 %
775	#FMS208.conv = [0.9048, 0.0119, 0.0267, 0.0137];
776	FMS208.conv = [0.92, 0.0119, 0.0267, 0.0137];
777	FMS208.Outlet.T = (30 + 273.15) * 'K';
778	FMS208.Outlet.Total.z(flu.Ammonia) = 0.0001; #Soh amonia suficiente eh adicionada
779
780	#Fonte de agua
781	MSS203.CompositionOfFluid(1) = 1;
782	MSS203.CompositionOfFluid(2:NComp) = 0;
783	MSS203.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
784	MSS203.Solid.Fw = 1e-6 * 'kg/h';
785	MSS203.T = ProPar.roomT;
786	MSS203.P = 1 * 'atm';
787
788	#torre de absorcao
789	ABT209.R = 0.9996;
790	ABT209.f = 1.5;
791	ABT209.T = (30 + 273.15) * 'K';
792	ABT209.P = 1 * 'atm';
793	ABT209.m = 0.88;
794
795	#centrifuga
796	CFG210.humidity = 0.3;
797	CFG210.frac_sol = 0.999;
798	CFG210.Power = 100 * 'hp';
799
800	#agua de diluicao de levedura
801	MSS204.CompositionOfFluid(1) = 1;
802	MSS204.CompositionOfFluid(2:NComp) = 0;
803	MSS204.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
804	MSS204.Solid.Fw = 1e-6 * 'kg/h';
805	MSS204.T = (30 + 273.15) * 'K';
806	MSS204.P = 1 * 'atm';
807
808	#acido sulfurico
809	MSS205.CompositionOfFluid = [0.02, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0.98, 0, 0, 0, 0];
810	MSS205.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
811	MSS205.Solid.Fw = 1e-6 * 'kg/h';
812	MSS205.T = (30 + 273.15) * 'K';
813	MSS205.P = 1 * 'atm';
814
815	EQUATIONS
816	#Concentracao de leveduras depois da diluicao - Assumindo corrente solida somente com levedura
817	#apesar da fracao ser volumetrica,a utilizada eh massica pq a diferenca entre as densidades eh muito pequena
818	#o creme de leveduras eh diluido com agua da coluna de adsorcao
819	ProPar.yeastConcTreatment * mMX212.Outlet.Total.Fw = mMX212.Outlet.Solid.Fw;
820
821	#fracao de acido sulfurico adicionado com base na vazao volumetrica de levedura
822	####
823	ProPar.SulfurAcTreatment * (mMX213.Outlet.Solid.Fw / ProPar.density_solution)= (MSS205.Fluid.Fw / ProPar.SulfurAcDensity);
824
825	#concentracao de levedura no fermentador - Assumindo corrente solida somente com levedura
826	ProPar.yeastConcFermenter * mMX206.Outlet.Total.Fw = mMX206.Outlet.Solid.Fw;
827
828	# Custo operacional - etapas de concentracao e fermentacao
829
830	Input_ConcFerm = EcoPar.WorkedHours * (MSS202.Outlet.Total.Fw * EcoPar.AmmoniaCost +
831	MSS203.Outlet.Total.Fw * EcoPar.WaterCost +
832	MSS204.Outlet.Total.Fw * EcoPar.WaterCost +
833	MSS205.Outlet.Total.Fw * EcoPar.SulfCost);
834	VARIABLES
835	Input_ConcFerm as currency (Brief = "Operational expenditure in the concentration and fermentation steps");
836
837	#*
838	*#
839	#----------------- destilacao ---------------------#
840	DEVICES
841
842	mMX308 as mixer_mR; #misturador entre os vinhos do C6/C12 e do C5
843
844	mPP309 as pump_mR; #primeira bomba
845	PSS301 as power_sourceR; #potencia para bomba
846
847	QSS303 as heat_sourceR; #calor para o refervedor da coluna AA1
848	QSS304 as heat_sourceR; #calor para o refervedor da coluna BB1
849	COL303 as column; #trem de colunas de destilacao do hidratado
850
851	QSS305 as heat_sourceR; #calor para a coluna de desidratacao
852	QSS306 as heat_sourceR; #calor para a coluna de recuperacao
853	MSS301 as main_sourceR; #fonte de MEG (total)
854	DEH304 as dehydration; #trem de colunas de desidratacao
855
856	PSS302 as power_sourceR; #Trabalho para a bomba
857	mPP307 as pump_mR; #Bomba do MEG recuperado
858
859	#*
860	*#
861	CONNECTIONS
862
863	CFG210.Filtrate to mMX308.Inlet1; #filtrado para misturador
864	FMS706.Outlet to mMX308.Inlet2; #vinho delevedurado para primeiro trocador
865
866	mMX308.Outlet to mPP309.Inlet; #misturador para bomba
867	PSS301.Outlet_p to mPP309.Inlet_p; #potencia para bomba
868
869	#Na var12 base, ha dois trocadores de calor nesta etapa. Aqui, o valor da saida eh
870	#com base no valor da simulacao (362.63 K). O primeiro trocador atinge 70 C e o segundo 362.63 K
871	#mPP309.Outlet to pinch to COL303.Wine # vinho delevedurado para o pinch para o aquecido para coluna
872
873	QSS303.Outlet_q to COL303.QAA1; #calor para o refervedor AA1
874	QSS304.Outlet_q to COL303.QBB1; #calor para o refervedor BB1
875
876	QSS305.Outlet_q to DEH304.QREXT; #Calor para o refervedor da coluna extrativa
877	QSS306.Outlet_q to DEH304.QRREC; #Calor para o refervedor da coluna de recuperacao
878	MSS301.Outlet to DEH304.MEG; #MEG para a coluna extrativa
879	COL303.HydrEth to DEH304.HydrEth; #Etanol hidratado para a coluna extrativa
880
881	#COL303.Vinasse to pinch ; #vinhaca para segundo trocador
882
883	#DEH304.RecMEG to pinch to mPP307.Inlet; #MEG recuperado para o pinch para a bomba
884
885	PSS302.Outlet_p to mPP307.Inlet_p; #trabalho para bomba
886	#*
887	*#
888	SET
889
890	#primeira bomba
891	mPP309.density = 1000 * 'kg/m^3';
892
893	#coluna de destilacao - Liquid para etanol hidratado , Vapour para etanol anidro
894	COL303.HydrOutletPhase = "Vapour";
895
896	#MEG de reposicao
897	MSS301.ValidPhases = "Liquid-Only";
898	MSS301.CompositionBasis = "Mass";
899
900	#segunda bomba
901	mPP307.density = 1000 * 'kg/m^3';
902
903	#*
904	*#
905	SPECIFY
906	#primeira bomba
907	mPP309.Outlet.P = 136.3 * 'kPa';
908	mPP309.n = ProPar.PumpEff;
909
910
911	#Fonte de MEG (total)
912	MSS301.T = (80 + 273.15) * 'K';
913	MSS301.P = 1 * 'atm';
914	MSS301.Solid.Fw = 1e-6 * 'kg/h';
915	MSS301.CompositionOfFluid = [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];
916	MSS301.CompositionOfSolid = [0.25, 0.20, 0.55, 0, 0, 0, 0, 0, 0];
917
918	#Coluna de desidratacao
919	DEH304.SolventRatio = 0.5;
920
921	#bomba do retorno do MEG
922	mPP307.Outlet.P = 1 * 'atm';
923	mPP307.n = ProPar.PumpEff;
924
925	#*
926	*#
927	VARIABLES
928	F_MEG as flow_mass (Brief = "MEG Replacement Flow");
929
930	EQUATIONS
931	#vazao de reposicao do MEG
932	F_MEG = MSS301.Fluid.Fw * MSS301.Outlet.Fluid.zw(flu.MEG) - mPP307.Outlet.Fluid.Fw * mPP307.Outlet.Fluid.zw(flu.MEG);
933
934	# Custo Operacional - Etapa de purificacao
935	OpEx_Purif = 1e-6 * 'US$' * ((AnhyEthProd - EcoPar.Ethanol1GProduction) / AnhyEthProd);
936
937	VARIABLES
938	OpEx_Purif as currency (Brief = "Operational expenditure in the Purification stage");
939
940	#*
941	*#
942
943	#---------------------- CHP-NC -------------------------#
944	DEVICES
945
946	MSS401 as main_sourceR; #fonte de ar
947	QSS401 as heat_sourceR; #fonte de calor para a caldeira...
948	mMX401 as mixer_mR; #misturador para material lignocelulosico e bagaco
949	mMX402 as mixer_mR; #misturador para material lignicelulosico e palha
950	BLR403 as boiler; #caldeira
951
952	wTB404 as turbine_w; #turbina de alta
953
954	wSP405 as splitter_wL; #splitter pos turbina de alta
955
956	wMX406 as mixer_wL; #dessuper
957
958	Cwq407 as cooler_wLD; #trocador de calor de alta
959
960	wSP408 as splitter_wL; #splitter com as perdas do condensado de alta
961
962	wFL409 as flash_wR; #flash de agua
963
964	wTB410 as turbine_w; #turbina de media
965
966	wSP411 as splitter_wR; #splitter pos turbina de media
967
968	wMX412 as mixer_wL; #dessuper de media
969
970	wMX413 as mixer_wL;
971
972	Cwq414 as cooler_wLD; #trocador de calor de media
973
974	wSP415 as splitter_wR; #splitter com as perdas do condensado de media
975
976	wMX416 as mixer_wL;
977
978	wFL417 as flash_wR; #flash de agua
979
980	wTB418 as turbine_w; #turbina de baixa
981
982	wSP419 as splitter_wR; #vapor para o desaerador
983
984	wMX420 as mixer_wL; #dessuper de baixa
985
986	wMX421 as mixer_wL; #misturador (vapor do flash de media e dessuper de baixa)
987
988	Cwq422 as cooler_wLD; #trocador de calor baixa
989
990	wSP423 as splitter_wR; #Perdas de vapor do processo
991
992	wMX424 as mixer_wR; #misturador (liquido do flash de media e condensado de baixa)
993
994	WSS402 as water_sourceR; #agua de reposicao
995	wPP425 as pump_wR; #bomba da agua de reposicao
996	PSS401 as power_sourceR; #trabalho para a bomba da agua de reposicao
997
998	wMX426 as mixer_wR; #misturador (condensados e agua de reposicao)
999
1000	wMX427 as mixer_wR; #desaerador
1001
1002	wSP428 as splitter_wR; #agua para o dessuper de baixa
1003
1004	PSS402 as power_sourceR; #trabalho para a bomba do dessuper de baixa
1005	wPP429 as pump_wR; #agua para o dessuper de baixa
1006
1007	wSP430 as splitter_wR; #agua para o dessuper de media
1008
1009	PSS403 as power_sourceR; #trabalho para a bomba do dessuper de media
1010	wPP431 as pump_wR; #agua para o dessuper de media
1011
1012	wSP432 as splitter_wR; #agua para o dessuper de alta
1013
1014	PSS404 as power_sourceR; #potencia para a bomba do dessuper de alta
1015	wPP433 as pump_wR; #agua para o dessuper de alta
1016
1017	PSS405 as power_sourceR; #potencia para a bomba do retorno da caldeira
1018	wPP434 as pump_wR; #retorno da agua para a caldeira
1019
1020	#*
1021	*#
1022	CONNECTIONS
1023
1024	mSP126.Outlet2 to mMX401.Inlet1; #bagaco para misturador
1025	SEP606.OutletS to mMX401.Inlet2; #material lignocelulosico 2G para misturador
1026	mMX401.Outlet to mMX402.Inlet1; #material lignocelulosico (1G+2G) para misturador
1027	mMX104.Outlet to mMX402.Inlet2; #palha para misturador
1028	mMX402.Outlet to BLR403.Fuel; #combustiveis para caldeira
1029	MSS401.Outlet to BLR403.Air; #ar para a caldeira
1030	QSS401.Outlet_q to BLR403.Inlet_q; #calor para a caldeira
1031
1032	BLR403.Steam to wTB404.Inlet; #vapor para a turbina de alta
1033
1034	wTB404.Outlet to wSP405.Inlet; #turbina de alta para splitter
1035
1036	wSP405.Outlet1 to wMX406.Inlet1; #splitter para dessuper de alta
1037
1038	wMX406.Outlet to Cwq407.Inlet; #dessuper para trocador de alta
1039
1040	Cwq407.Outlet to wSP408.Inlet; #trocador de alta para splitter de perdas
1041
1042	wSP408.Outlet1 to wFL409.Inlet; #splitter para flash
1043
1044	wSP405.Outlet2 to wTB410.Inlet; #splitter de alta para turbina de media
1045
1046	wTB410.Outlet to wSP411.Inlet; #turbina de media para splitter de media
1047
1048	wSP411.Outlet1 to wMX412.Inlet1; #splitter de media para dessuper de media
1049
1050	wFL409.OutletV to wMX413.Inlet1;
1051	wFL417.OutletV to wMX413.Inlet2;
1052
1053	wMX412.Outlet to Cwq414.Inlet; #misturador de media para trocador de media
1054
1055	Cwq414.Outlet to wSP415.Inlet; #trocador de media para splitter de perdas
1056
1057	wFL409.OutletL to wMX416.Inlet1;
1058	wFL417.OutletL to wMX416.Inlet2;
1059
1060	wSP415.Outlet1 to wFL417.Inlet; #misturador para flash de media
1061
1062	wSP411.Outlet2 to wTB418.Inlet; #splitter de media para turbina de baixa
1063
1064	wTB418.Outlet to wSP419.Inlet; #turbina de baixa para splitter de baixa
1065
1066	wSP419.Outlet1 to wMX420.Inlet1; #splitter de baixa para dessuper de baixa
1067
1068	wMX420.Outlet to wMX421.Inlet1; #dessuper para misturador (vapor do flash de media e vapor saturado de baixa)
1069
1070	wMX413.Outlet to wMX421.Inlet2;
1071
1072	wMX421.Outlet to Cwq422.Inlet; #misturador de baixa para trocador de baixa
1073
1074	Cwq422.Outlet to wSP423.Inlet; #trocador de baixa para splitter de perdas
1075
1076	wSP423.Outlet1 to wMX424.Inlet1; #condensado de baixa para misturador (liquido do flash de media e condensado de baixa)
1077	wMX416.Outlet to wMX424.Inlet2;
1078
1079	WSS402.Outlet to wPP425.Inlet; #agua de reposicao para bomba
1080	PSS401.Outlet_p to wPP425.Inlet_p; #potencia para a bomba da agua de reposicao
1081
1082	wMX424.Outlet to wMX426.Inlet1; #condensados para misturador (condensados e agua de reposicao)
1083	wPP425.Outlet to wMX426.Inlet2; #agua de reposicao para misturador
1084
1085	wMX426.Outlet to wMX427.Inlet1; #agua para desaerador
1086	wSP419.Outlet2 to wMX427.Inlet2; #vapor para desaerador
1087
1088	wMX427.Outlet to wSP428.Inlet; #agua desaerada para splitter (dessuper de baixa)
1089
1090	wSP428.Outlet1 to wPP429.Inlet; #splitter para bomba (dessuper de baixa)
1091	PSS402.Outlet_p to wPP429.Inlet_p; #trabalho para bomba do dessuper de baixa
1092
1093	wPP429.Outlet to wMX420.Inlet2; #bomba para dessuper de baixa
1094
1095	wSP428.Outlet2 to wSP430.Inlet; #splitter (dessuper de baixa) para splitter (dessuper de media)
1096
1097	wSP430.Outlet1 to wPP431.Inlet; #splitter para bomba (dessuper de media)
1098	PSS403.Outlet_p to wPP431.Inlet_p; #trabalho para bomba do dessuper de media
1099
1100	wPP431.Outlet to wMX412.Inlet2; #bomba para dessuper de media
1101
1102	wSP430.Outlet2 to wSP432.Inlet; #splitter (dessuper de media) para splitter (dessuper de alta)
1103
1104	wSP432.Outlet1 to wPP433.Inlet; #splitter para bomba (dessuper de alta)
1105	PSS404.Outlet_p to wPP433.Inlet_p; #potencia para bomba do dessuper de alta
1106
1107	wPP433.Outlet to wMX406.Inlet2; #bomba para dessuper de alta
1108
1109	wSP432.Outlet2 to wPP434.Inlet; #splitter (dessuper de alta) para bomba (retorno da caldeira)
1110	PSS405.Outlet_p to wPP434.Inlet_p; #potencia para bomba do retorno da caldeira
1111
1112	wPP434.Outlet to BLR403.Water; #bomba para retorno da caldeira
1113	#*
1114	*#
1115	SET
1116
1117	#fonte de ar
1118	MSS401.CompositionBasis = "Molar";
1119	MSS401.ValidPhases = "Vapour-Only";
1120
1121	#boiler
1122	BLR403.NReac = 4;
1123	# Reaction 1:cellulose(C6H10O5) + 6O2 --> 5H2O + 6CO2
1124	BLR403.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];
1125	# Reaction 2:hemicellulose(C5H8O4) + 5O2 --> 4H2O + 5CO2
1126	BLR403.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];
1127	# Reaction 3:lignina(C10H11.6O3.9) + 10.95O2 --> 5.8H2O + 10CO2
1128	BLR403.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];
1129	# Reaction 4:CH4 + 2 O2 --> CO2 + 2 H2O
1130	BLR403.stoic (:,4) = [2, 0, 0, 0, 0, 1, 0, -2, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1131	BLR403.h = [-2804.2, -2170.9, -5243, -802.6] * 'kJ/mol';
1132	BLR403.limit = [NComp+sol.Cellulose, NComp+sol.Hemicell, NComp+sol.Lignin, flu.CH4];
1133
1134	#dessuper (alta)
1135	wMX406.Outlet.ValidPhases = "Vapour-Liquid";
1136
1137	#condensador alta
1138	Cwq407.Outlet.ValidPhases = "Liquid-Only";
1139
1140	#Dessuper de media
1141	wMX412.Outlet.ValidPhases = "Vapour-Liquid";
1142
1143	#misturador
1144	wMX413.Outlet.ValidPhases = "Vapour-Liquid";
1145
1146	#condensador media
1147	Cwq414.Outlet.ValidPhases = "Liquid-Only";
1148
1149	#misturador
1150	wMX416.Outlet.ValidPhases = "Vapour-Liquid";
1151
1152	#Dessuper de baixa
1153	wMX420.Outlet.ValidPhases = "Vapour-Liquid";
1154
1155	#misturador (vapor do flash e dessuper baixa)
1156	wMX421.Outlet.ValidPhases = "Vapour-Liquid";
1157
1158	#condensador baixa
1159	Cwq422.Outlet.ValidPhases = "Liquid-Only";
1160
1161	#misturador (liquido do flash de media e condensado de baixa)
1162	wMX424.Outlet.ValidPhases = "Liquid-Only";
1163
1164	#agua de reposicao
1165	WSS402.ValidPhases = "Liquid-Only";
1166
1167	#bomba
1168	wPP425.density = 1000 * 'kg/m^3';
1169
1170	#primeiro mixer (desaerador)
1171	wMX426.Outlet.ValidPhases = "Liquid-Only";
1172
1173	#segundo mixer (desaerador)
1174	wMX427.Outlet.ValidPhases = "Vapour-Liquid";
1175
1176	#bomba (dessuper baixa)
1177	wPP429.density = 1000 * 'kg/m^3';
1178
1179	#bomba (dessuper media)
1180	wPP431.density = 1000 * 'kg/m^3';
1181
1182	#bomba (dessuper alta)
1183	wPP433.density = 1000 * 'kg/m^3';
1184
1185	#bomba (retorno da caldeira)
1186	wPP434.density = 1000 * 'kg/m^3';
1187	#*
1188	*#
1189	SPECIFY
1190
1191	#fonte de ar
1192	MSS401.Solid.Fw = 1e-6 * 'kg/h';
1193	MSS401.T = (50 + 273.15) * 'K';
1194	MSS401.P = 1 * 'atm';
1195	MSS401.CompositionOfSolid = [0.455992, 0.278661, 0.241138, 0.0242091, 0, 0, 0, 0, 0];
1196	MSS401.CompositionOfFluid = [0, 0, 0, 0, 0, 0, 0, 0.21, 0.79, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1197
1198	#boiler
1199	#BLR403.f_losses = 0.01;
1200	BLR403.Gas.T = (190 + 273.15) * 'K'; #usina Alta Mogiana
1201	BLR403.Efficiency_LHV = 0.88; #comunicacao pessoal
1202	BLR403.T = (485 + 273.15) * 'K';
1203	BLR403.Pdrop = 0 * 'bar';
1204	BLR403.conv = [1, 1, 1, 1];
1205	BLR403.Ex_Air = 0.3;
1206	BLR403.Inlet_q.Q = 0 * 'kW';
1207
1208	#turbina de alta
1209	wTB404.Outlet.P = 17.4 * 'bar';
1210	wTB404.EF_T = ProPar.TurbineEff;
1211	wTB404.EF_ME = ProPar.MechanicalEff;
1212
1213	#dessuper de alta
1214	wMX406.Outlet.v = 1;
1215
1216	#trocador representando demanda de vapor de alta do processo
1217	Cwq407.Outlet.P = 17.4 * 'bar';
1218	Cwq407.Outlet.T = (200 + 273.15) * 'K';
1219	Cwq407.U = ProPar.U;
1220	Cwq407.lmtd = 10 * 'K';
1221
1222	#perdas do processo (alta)
1223	wSP408.frac = 0.96;
1224
1225	#flash (alta)
1226	#wFL409.P = 6 * 'bar';
1227	wFL409.P = 2.5 * 'bar';
1228	wFL409.v = 0.145390044; #valor especificado para que 'Q' seja aproximadamente 0
1229
1230	#turbina de media
1231	wTB410.Outlet.P = 6 * 'bar';
1232	wTB410.EF_T = ProPar.TurbineEff;
1233	wTB410.EF_ME = ProPar.MechanicalEff;
1234
1235	#dessuper de media
1236	wMX412.Outlet.v = 1;
1237
1238	#trocador representando demanda de vapor de media do processo
1239	Cwq414.Pdrop = 0 * 'bar';
1240	Cwq414.Outlet.T = (154 + 273.15) * 'K';
1241	Cwq414.U = ProPar.U;
1242	Cwq414.lmtd = 10 * 'K';
1243
1244	#perdas do processo (media)
1245	wSP415.frac = 0.96;
1246
1247	#flash (media)
1248	wFL417.P = 2.5 * 'bar';
1249	wFL417.v = 0.0523755; #valor especificado para que 'Q' seja aproximadamente 0
1250
1251	#turbina de baixa
1252	wTB418.Outlet.P = 2.5 * 'bar';
1253	wTB418.EF_T = ProPar.TurbineEff;
1254	wTB418.EF_ME = ProPar.MechanicalEff;
1255
1256	#dessuper de baixa
1257	wMX420.Outlet.v = 1;
1258
1259	#trocador representando demanda de vapor de baixa do processo
1260	Cwq422.Outlet.P = 2.092 * 'bar';
1261	Cwq422.Outlet.T = (102 + 273.15) * 'K';
1262	Cwq422.U = ProPar.U;
1263	Cwq422.lmtd = 10 * 'K';
1264
1265	#perdas do processo (baixa)
1266	wSP423.frac = 0.96;
1267
1268	#agua de reposicao
1269	WSS402.T = ProPar.roomT;
1270	WSS402.P = 1 * 'atm';
1271
1272	#bomba reposicao
1273	wPP425.PIn = 1.65 * 'bar';
1274	wPP425.n = ProPar.PumpEff;
1275
1276	#desaerador
1277	wMX427.Outlet.v = 0;
1278
1279	#bomba dessuper baixa
1280	wPP429.Outlet.P = 2.5 * 'bar';
1281	wPP429.n = ProPar.PumpEff;
1282
1283	#bomba dessuper media
1284	wPP431.Outlet.P = 6 * 'bar';
1285	wPP431.n = ProPar.PumpEff;
1286
1287	#bomba dessuper alta
1288	wPP433.Outlet.P = 17.4 * 'bar';
1289	wPP433.n = ProPar.PumpEff;
1290
1291	#bomba retrno a caldeira
1292	wPP434.Outlet.P = 65 * 'bar';
1293	wPP434.n = ProPar.PumpEff;
1294
1295	# Custo operacional - Cogeracao
1296	VARIABLES
1297	EnergyProduction as positive (Unit = 'kW/h');
1298
1299	EQUATIONS
1300	# Vapor produzido
1301	EnergyProduction = wTB404.Outlet.Fw / (11.92 * 'kg/kW') * 0.001
1302	+ wTB410.Outlet.Fw / (18.06 * 'kg/kW') * 0.001
1303	+ wTB418.Outlet.Fw / (26.13 * 'kg/kW') * 0.001;
1304
1305	#*
1306	*#
1307	#-------------------- pretratamento ----------------------#
1308	DEVICES
1309	PSS501 as power_sourceR; #trabalho para a bomba
1310	mPP501 as pump_mL; #"bomba" que pressuriza o bagaco
1311
1312	mMX502 as mixer_mR; #misturador bagaco-agua
1313
1314	RTS504 as stoic_reactor; #reator de pre-tratamento
1315
1316	MSS501 as main_sourceR; #fonte de agua de diluicao
1317	mPP505 as pump_mL; #bomba que pressuriza a agua de diluicao
1318	PSS502 as power_sourceR; #trabalho para a bomba
1319
1320	mFL508 as exo_flash; #flash para abaixar a pressao da mistura
1321
1322	MSS502 as main_sourceR; #fonte de amonia para neutralizacao da mistura
1323	mMX509 as mixer_mR; #misturador
1324
1325	MSS503 as main_sourceR; #fonte de agua de diluicao
1326	mMX510 as mixer_mR; #misturador bagaco tratado - agua de diluicao
1327
1328	SEP511 as sepR; #filtro
1329	#*
1330	*#
1331	CONNECTIONS
1332	mSP126.Outlet1 to mPP501.Inlet; #bagaco
1333	PSS501.Outlet_p to mPP501.Inlet_p; #potencia para bomba
1334
1335	mPP501.Outlet to mMX502.Inlet1; #bomba para misturador
1336
1337	#mMX502.Outlet to pinch to RTS504.Inlet; #misturador para o pinch para o reator de pre-tratamento
1338
1339	MSS501.Outlet to mPP505.Inlet; #fonte de agua para bomba
1340	PSS502.Outlet_p to mPP505.Inlet_p; #trabalho para bomba
1341
1342	#mPP505.Outlet to pinch to mMX502.Inlet2; #agua de diluicao para aquecedor
1343
1344	#RTS504.Outlet to pinch to mFL508.Inlet; #bagaco pre-tratado para o pinch para o flash
1345
1346	mFL508.OutletL to mMX509.Inlet1; #flash (liquido) para misturador
1347	MSS502.Outlet to mMX509.Inlet2; #amonia para misturador
1348
1349	mMX509.Outlet to mMX510.Inlet1; #misturador para misturador
1350	MSS503.Outlet to mMX510.Inlet2; #agua de diluicao para misturador
1351
1352	mMX510.Outlet to SEP511.Inlet; #misturador para filtro
1353	#*
1354	*#
1355	SET
1356
1357	#pretreatment reactor
1358	#reactions:
1359	# C6H10O5(limit) + H2O -> C6H12O6 conv = 8.12 %
1360	# C6H10O5(limit) -> C6H6O3 + 2H2O conv = 0.07 %
1361	# C6H10O5(limit) + H2O -> 12C0.5HO0.5 conv = 5.28 %
1362	# C5H8O5(limit) + H2O -> C5H10O5 conv = 46.53 %
1363	# C5H8O5(limit) + H2O -> 10C0.5HO0.5 conv = 25.77 % This represents the arabinose reaction + unknowns produced
1364	# C5H8O5(limit) -> C5H4O2 + 2H2O conv = 3.89 %
1365	# C5H8O5(limit) + H2O -> 5/2C2H4O2 conv = 7.39 %
1366	# C10H11.6O2.9(limit) -> C10H11.6O2.9(liq) conv = 17.2 %
1367
1368	RTS504.NReac = 8;
1369	#cellulose to glucose
1370	RTS504.stoic (:,1) = [-1, 0, 1, 0, 0, 0, 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, 0, 0];
1371	#cellulose to 5-HMF
1372	RTS504.stoic (:,2) = [2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0];
1373	#cellulose to solunkn
1374	RTS504.stoic (:,3) = [-1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 12, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0];
1375	#hemicellulose to xylose
1376	RTS504.stoic (:,4) = [-1, 0, 0, 1, 0, 0, 0, 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, 0];
1377	#hemicellulose to solunkn
1378	RTS504.stoic (:,5) = [-1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 10, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0];
1379	#hemicellulose to furfural
1380	RTS504.stoic (:,6) = [2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0];
1381	#hemicellulose to acetic acid
1382	RTS504.stoic (:,7) = [-1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 2.5, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0];
1383	#lignin to solunkn
1384	RTS504.stoic (:,8) = [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, 0, -1, 0, 0, 0, 0, 0, 0];
1385	RTS504.limit = [NComp+sol.Cellulose, NComp+sol.Cellulose, NComp+sol.Cellulose, NComp+sol.Hemicell, NComp+sol.Hemicell, NComp+sol.Hemicell, NComp+sol.Hemicell, NComp+sol.Lignin];
1386	RTS504.h = [0, 0, 0, 0, 0, 0, 0, 0] * 'kJ/mol';
1387
1388	#entrada de agua
1389	MSS501.ValidPhases = "Liquid-Only";
1390	MSS501.CompositionBasis = "Mass";
1391
1392	#entrada de amonia
1393	MSS502.ValidPhases = "Liquid-Only";
1394	MSS502.CompositionBasis = "Mass";
1395
1396	#entrada de agua
1397	MSS503.ValidPhases = "Liquid-Only";
1398	MSS503.CompositionBasis = "Mass";
1399	#*
1400	*#
1401	SPECIFY
1402
1403	#bomba para o bagaco
1404	mPP501.PIn = 14.1 * 'atm';
1405	mPP501.n = ProPar.PumpEff;
1406
1407	#reator de pre-tratamento
1408	#reactions:
1409	# C6H10O5(limit) + H2O -> C6H12O6 conv = 8.12 %
1410	# C6H10O5(limit) -> C6H6O3 + 2H2O conv = 0.07 %
1411	# C6H10O5(limit) + H2O -> 12C0.5HO0.5 conv = 5.28 %
1412	# C5H8O5(limit) + H2O -> C5H10O5 conv = 46.53 %
1413	# C5H8O5(limit) + H2O -> 10C0.5HO0.5 conv = 25.77 % This represents the arabinose reaction + unknowns produced
1414	# C5H8O5(limit) -> C5H4O2 + 2H2O conv = 3.89 %
1415	# C5H8O5(limit) + H2O -> 5/2C2H4O2 conv = 7.39 %
1416	# C10H11.6O2.9(limit) -> C10H11.6O2.9(liq) conv = 17.2 %
1417	#RTS504.conv = [0.0812, 0.0007, 0.0528, 0.4653, 0.2577, 0.0389, 0.0739, 0.172];
1418	#RTS504.Outlet.T = (195 + 273.15) * 'K';
1419	RTS504.reac_time = 600 * 's'; #10 min
1420
1421	#fonte de agua
1422	MSS501.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];
1423	MSS501.Solid.Fw = 1e-6 * 'kg/h';
1424	MSS501.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
1425	MSS501.T = 303.15 * 'K';
1426	MSS501.P = 1 * 'atm';
1427
1428	#bomba da agua de diluicao
1429	mPP505.PIn = 14.1 * 'atm';
1430	mPP505.n = ProPar.PumpEff;
1431
1432	#flash
1433	mFL508.Pdrop = 14.1 * 'atm';
1434	mFL508.OutletV.T = (80 + 273.15) * 'K';
1435
1436	#fonte de amonia
1437	MSS502.CompositionOfFluid = [0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1438	MSS502.Solid.Fw = 1e-6 * 'kg/h';
1439	MSS502.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
1440	MSS502.T = ProPar.roomT;
1441	MSS502.P = 1 * 'atm';
1442
1443	#fonte de agua de diluicao
1444	MSS503.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];
1445	MSS503.Fluid.Fw = 1e-6 * 'kg/h';
1446	MSS503.Solid.Fw = 1e-6 * 'kg/h';
1447	MSS503.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
1448	MSS503.T = ProPar.roomT;
1449	MSS503.P = 1 * 'atm';
1450
1451	#filtro
1452	SEP511.humidity = 0.5;
1453	SEP511.frac_sol = 0.995;
1454
1455	#fracao de solidos
1456	#SolMassFracPre = 0.15;
1457	#SolMassFracPre = 0.2;
1458
1459	VARIABLES
1460	SolMassFracPre as fraction (Brief = "Solid Mass Fraction in the Pretreatment Reactor", Default = 0.15);
1461
1462	EQUATIONS
1463	#fracao de solidos no reator de pre-tratamento
1464	mMX502.Outlet.Solid.Fw = SolMassFracPre * mMX502.Outlet.Total.Fw;
1465
1466	#amonia neutraliza metade do acido acetico produzido no reator de pre-tratamento
1467	MSS502.Fluid.Fw = 0.5 * mFL508.OutletL.Fluid.Fw * mFL508.OutletL.Fluid.zw(flu.AceticAcid);
1468
1469	# Custo operacional - Etapa de pretratamento
1470	Input_PreTreat = EcoPar.WorkedHours * (MSS501.Outlet.Total.Fw * EcoPar.WaterCost +
1471	MSS502.Outlet.Total.Fw * EcoPar.AmmoniaCost +
1472	MSS503.Outlet.Total.Fw * EcoPar.WaterCost);
1473
1474	VARIABLES
1475	Input_PreTreat as currency (Brief = "Operational expenditure in the pretreatment stage");
1476
1477	#*
1478	*#
1479	#---------------------- hidrolise ------------------------#
1480	DEVICES
1481	MSS601 as main_sourceR; #fonte de agua de diluicao
1482	mMX601 as mixer_mR; #misturador
1483
1484	MSS602 as main_sourceR; #fonte de enzimas
1485	mMX603 as mixer_mR; #misturador
1486
1487	HLS604 as stoic_reactor; #reator de hidrolise
1488
1489	MSS603 as main_sourceR; #fonte de agua de diluicao
1490	mMX605 as mixer_mR; #misturador
1491
1492	SEP606 as sepR; #filtro
1493
1494	mPP607 as pump_mR; #bomba do hidrolisado
1495	PSS601 as power_sourceR; #trabalho para bomba
1496	#*
1497	*#
1498	CONNECTIONS
1499	SEP511.OutletS to mMX601.Inlet1; #bagaco pre-tratado para misturador
1500	MSS601.Outlet to mMX601.Inlet2; #agua de diluicao para misturador
1501
1502	#mMX601.Outlet to pinch to mMX603.Inlet1; #misturador para pinch para misturador
1503
1504	MSS602.Outlet to mMX603.Inlet2; #enzima para misturador
1505
1506	mMX603.Outlet to HLS604.Inlet; #misturador para reator
1507
1508	HLS604.Outlet to mMX605.Inlet1; #reator para misturador
1509	MSS603.Outlet to mMX605.Inlet2; #agua de diluicao para misturador
1510
1511	mMX605.Outlet to SEP606.Inlet; #misturador para filtro
1512
1513	SEP606.OutletL to mPP607.Inlet; #filtrado para bomba
1514	PSS601.Outlet_p to mPP607.Inlet_p; #trabalho para bomba
1515	#*
1516	*#
1517	SET
1518	#entrada de agua de diluicao
1519	MSS601.ValidPhases = "Liquid-Only";
1520	MSS601.CompositionBasis = "Mass";
1521
1522	#fonte de enzima
1523	MSS602.ValidPhases = "Liquid-Only";
1524	MSS602.CompositionBasis = "Mass";
1525
1526	#hydrolysis reactor
1527	#reactions:
1528	# C6H10O5(limit) + H2O -> C6H12O6
1529	HLS604.NReac = 1;
1530	#cellulose to glucose
1531	HLS604.stoic (:,1) = [-1, 0, 1, 0, 0, 0, 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, 0, 0];
1532	HLS604.limit = [NComp+sol.Cellulose];
1533	HLS604.h = [0] * 'kJ/mol';
1534	HLS604.density = 1000 * 'kg/m^3';
1535
1536	#entrada de bagaco agua de diluicao
1537	MSS603.ValidPhases = "Liquid-Only";
1538	MSS603.CompositionBasis = "Mass";
1539
1540	#Bomba
1541	mPP607.density = 1000 * 'kg/m^3';
1542
1543
1544	#*
1545	*#
1546	SPECIFY
1547
1548	#fonte de agua
1549	MSS601.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];
1550	MSS601.Solid.Fw = 1e-6 * 'kg/h';
1551	MSS601.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
1552	MSS601.T = ProPar.roomT;
1553	MSS601.P = 1 * 'atm';
1554
1555	#fonte de enzima
1556	MSS602.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];
1557	MSS602.CompositionOfSolid = [0, 0, 0, 0, 1, 0, 0, 0, 0];
1558	MSS602.T = 303.15 * 'K';
1559	MSS602.P = 1 * 'atm';
1560
1561	#reator de hidrolise
1562	#reactions:
1563	# C6H10O5(limit) + H2O -> C6H12O6
1564	#HLS604.conv = [0.59];
1565	#HLS604.Outlet.T = (50 + 273.15) * 'K';
1566	#HLS604.reac_time = 48 * 'h';
1567
1568	#fonte de agua
1569	MSS603.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];
1570	MSS603.Fluid.Fw = 1e-6 * 'kg/h';
1571	MSS603.Solid.Fw = 1e-6 * 'kg/h';
1572	MSS603.CompositionOfSolid = [1, 0, 0, 0, 0, 0, 0, 0, 0];
1573	MSS603.T = 303.15 * 'K';
1574	MSS603.P = 1 * 'atm';
1575
1576	#filtro
1577	SEP606.humidity = 0.5;
1578	SEP606.frac_sol = 0.99;
1579
1580	#bomba
1581	mPP607.Outlet.P = 1.7 * 'atm';
1582	mPP607.n = ProPar.PumpEff;
1583
1584	#principais condicoes operacionais hidrolise
1585	#EnzymeConc = 150 * 'g/l';
1586	#SolMassFracHydro = 0.15;
1587	#SolMassFracHydro = 0.10;
1588	#EnzymeLoad = 10;
1589
1590	#*
1591	*#
1592	VARIABLES
1593	EnzymeConc as Real (Brief = "Enzyme Concentration", Unit='g/l', Default = 150);
1594	SolMassFracHydro as fraction (Brief = "Solid Mass Fraction in the Hydrolysis Reactor", Default = 0.10);
1595	EnzymeLoad as positive (Brief = "Enzyme Load in FPU/g of cellulose", Default = 10);
1596
1597	PARAMETERS
1598	EnzymeActivity as positive (Brief = "Complex enzyme activity in U/g", Default = 500);
1599
1600	SET
1601	EnzymeActivity = 500;
1602
1603	EQUATIONS
1604
1605	#Enzyme concentration
1606	#1000 * 'kg/m^3' * MSS602.Outlet.Solid.zw(sol.Enzyme) * MSS602.Outlet.Solid.Fw = EnzymeConc * MSS602.Outlet.Total.Fw;
1607	#assumindo densidade da mistura de 1000 * 'kg/m^3'
1608	1150 * 'kg/m^3' * MSS602.Outlet.Solid.zw(sol.Enzyme) * MSS602.Outlet.Solid.Fw = EnzymeConc * MSS602.Outlet.Total.Fw;
1609	#assumindo densidade da mistura de 1.15 g/mL - Cellic CTec2 - Sigma-Aldrich
1610
1611	#amount of enzyme in the hydrolysis reactor
1612	EnzymeLoad * HLS604.Inlet.Solid.zw(sol.Cellulose) = EnzymeActivity * HLS604.Inlet.Solid.zw(sol.Enzyme);
1613
1614	#Solid mass fraction in the hydrolysis reactor
1615	HLS604.Inlet.Solid.Fw = SolMassFracHydro * HLS604.Inlet.Total.Fw;
1616
1617	# Custo operacional - Etapa de hidrolise e da producao de enzima
1618	Input_Hydr = EcoPar.WorkedHours * (MSS601.Outlet.Total.Fw * EcoPar.WaterCost +
1619	MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * EnzymecostFinal +
1620	MSS603.Outlet.Total.Fw * EcoPar.WaterCost);
1621
1622	Input_Enzyme = EcoPar.WorkedHours * MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * EnzymecostFinal;
1623
1624
1625	VARIABLES
1626	Input_Hydr as currency (Brief = "Operational expenditure in the Hydrolisis stage");
1627	Input_Enzyme as currency (Brief = "Operational expenditure in the enzyme in Hydrolisis stage");
1628
1629	#*
1630	*#
1631	#----------------- fermentacao xilose ---------------------#
1632	DEVICES
1633
1634	PSS701 as power_sourceR; #potencia para bomba
1635	mPP701 as pump_mL; #bomba para licor de C5
1636
1637	WSS701 as water_sourceR; #vapor de aquecimento para o evaporador
1638	EVP702 as evaporator3; # 1 evaporador
1639	EVP703 as evaporator3; # 2 evaporador
1640	EVP704 as evaporator3; # 3 evaporador
1641
1642	PSS702 as power_sourceR; #potencia para segunda bomba
1643	mPP704 as pump_mL; #segunda bomba
1644
1645	FMS706 as stoic_fermenter; #fermentador C5 e C6
1646
1647	#*
1648	*#
1649	CONNECTIONS
1650
1651	SEP511.OutletL to mPP701.Inlet; #licor C5 para bomba
1652	PSS701.Outlet_p to mPP701.Inlet_p; #potencia para bomba
1653
1654	mPP701.Outlet to EVP702.Inlet; #licor C5 para evaporador
1655	WSS701.Outlet to EVP702.InletS; #vapor para o 2 evaporador
1656
1657	EVP702.OutletL to EVP703.Inlet; #licor C5 concentrado para 2 evaporador
1658	EVP702.OutletV to EVP703.InletS; #vapor para o 3 evaporador
1659
1660	EVP703.OutletL to EVP704.Inlet; #licor C5 concentrado para 3 evaporador
1661	EVP703.OutletV to EVP704.InletS;
1662
1663	EVP704.OutletL to mPP704.Inlet; #licor C5 concentrado para segunda bomba
1664
1665	PSS702.Outlet_p to mPP704.Inlet_p; #potencia para segunda bomba
1666
1667	#mPP704.Outlet to pinch to FMS706.Inlet; #licor C5 para o resfriador para o fermentador
1668
1669	#*
1670	*#
1671	SET
1672
1673	#bomba da agua de diluicao
1674	mPP701.density = 1000 * 'kg/m^3';
1675
1676	#Fonte de vapor
1677	WSS701.ValidPhases = "Vapour-Liquid";
1678
1679	#Evaporador
1680	EVP702.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];
1681	EVP703.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];
1682	EVP704.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];
1683
1684	#bomba para licor concetrado
1685	mPP704.density = 1000 * 'kg/m^3';
1686
1687	#C5 fermentor
1688	#reactions:
1689	# C6H12O6 -> 2C2H6O + 2CO2 conv = 90.48 %
1690	# C6H12O6 + 2H2O -> 2C2H4O + 2CO2 + 4H2 conv = 1.19 %
1691	# C6H12O6 + 2H2 -> 2C3H8O3 conv = 2.67 %
1692	# C5H10O5 -> 5/3C2H6O + 5/3CO2 conv = 91.7742%
1693	# C5H10O5 -> 5/2C2H4O2 conv = 1.5 %
1694	# C5H10O5 + 5/3H2 -> 5/3C3H8O3 conv = 2.8 %
1695	FMS706.NReac = 6;
1696	#glucose to ethanol
1697	FMS706.stoic (:,1) = [0, 0, -1, 0, 2, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1698	#glucose to acetic acid
1699	FMS706.stoic (:,2) = [-1.5524, 0, -1, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1700	#glucose to glycerol
1701	FMS706.stoic (:,3) = [-0.2238, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 2, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1702	#xylose to ethanol
1703	FMS706.stoic (:,4) = [0, 0, 0, -1, 5/3, 5/3, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1704	#xylose to acetic acid
1705	FMS706.stoic (:,5) = [0, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 2.5, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1706	#xylose to glycerol
1707	FMS706.stoic (:,6) = [-0.1865, 0, 0, -1, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 5/3, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0];
1708	FMS706.limit = [flu.Glucose, flu.Glucose, flu.Glucose, flu.Xylose, flu.Xylose, flu.Xylose];
1709	FMS706.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];
1710	FMS706.fermentation = "glucose-xylose";
1711
1712	#*
1713	*#
1714	SPECIFY
1715
1716	#bomba do licor de pentoses
1717	mPP701.Outlet.P = 1.7 * 'atm';
1718	mPP701.n = ProPar.PumpEff;
1719
1720	#segunda bomba
1721	mPP704.Outlet.P = 1.2 * 'atm';
1722	mPP704.n = ProPar.PumpEff;
1723
1724	#vapor de aquecimento para concentracao do caldo C5
1725	WSS701.v = 1;
1726	WSS701.P = 2.5 * 'bar';
1727
1728	#evaporadores
1729	EVP702.OutletV.P = 1.69 * 'bar';
1730	EVP703.OutletV.P = 1.31 * 'bar';
1731	EVP704.OutletV.P = 0.93 * 'bar';
1732
1733	#C5 fermentor
1734	#reactions:
1735	# C6H12O6 -> 2C2H6O + 2CO2 conv = 90.48 %
1736	# C6H12O6 + 2H2O -> 2C2H4O + 2CO2 + 4H2 conv = 1.19 %
1737	# C6H12O6 + 2H2 -> 2C3H8O3 conv = 2.67 %
1738	# C5H10O5 -> 5/3C2H6O + 5/3CO2 conv = 91.7742%
1739	# C5H10O5 -> 5/2C2H4O2 conv = 1.5 %
1740	# C5H10O5 + 5/3H2 -> 5/3C3H8O3 conv = 2.8 %
1741	#FMS706.conv = [0.9048, 0.0119, 0.0267, (0.95-1/31), 0.015, 0.028];
1742	FMS706.conv(1:3) = [0.9048, 0.0119, 0.0267];
1743	FMS706.conv(5:6) = [0.015, 0.028];
1744	#FMS706.conv(4) = 0.917742;
1745
1746	FMS706.Outlet.T = (35 + 273.15) * 'K';
1747
1748	#Conc_xylose = 60 * 'g/l';
1749
1750	VARIABLES
1751	Conc_xylose as Real (Brief = "Xylose Concentration", Unit='g/l', Lower = 1e-6);
1752	RT_Fermenter as time_h (Brief = "Residence Time", Default = 5.4);
1753	Pr_xylose as Real (Brief = "C5 ethanol global volumetric productivity", Unit = 'g/l/h', Lower = 1e-6);
1754
1755	EQUATIONS
1756	#concentracao de acucares no evaporador
1757	Conc_xylose * EVP704.OutletL.Total.Fw = 1000 * 'kg/m^3' * EVP704.OutletL.Fluid.zw(flu.Xylose) * EVP704.OutletL.Fluid.Fw;
1758
1759	RT_Fermenter / (994.01 * 'kg/m^3') = FMS706.Outlet.Total.zw(flu.Ethanol) / Pr_xylose;
1760	#RT_Fermenter * Pr_xylose = FMS706.Outlet.Total.Fw * FMS706.Outlet.Total.zw(flu.Ethanol) / (FMS706.Outlet.Total.Fw / (994.01 * 'kg/m^3'));
1761
1762	SPECIFY
1763	RT_Fermenter = 5.4 * 'h';
1764	#*
1765	*#
1766
1767	PARAMETERS
1768	C5FermRaw as Real (Brief = "Raw material Costs", Unit = 'US$ / kg');
1769
1770	SET
1771	C5FermRaw = (0.84 /EcoPar.ExchangeRate) * 'US$'/ 12 / 0.98 * '1/kg' #KH2PO4 - xylose base - (preco / qde usada por g de xylose / pureza)
1772	+ (0.168/EcoPar.ExchangeRate) * 'US$' / 30 / 0.99 * '1/kg' #MgSO4 - xylose base - (preco / qde usada por g de xylose / pureza)
1773	+ (0.42/EcoPar.ExchangeRate) * 'US$'/ 40 / 0.99 * '1/kg' #Ureia - xylose base - (preco / qde usada por g de xylose / pureza)
1774	+ (0.21/EcoPar.ExchangeRate) * 'US$'/ 30 / 0.94 * '1/kg'; #CaCl2 - xylose base - (preco / qde usada por g de xylose / pureza)
1775
1776	VARIABLES
1777	Input_C5Ferm as currency (Brief = "Operational expenditure in the Xylose Fermentation stage");
1778
1779	EQUATIONS
1780	Input_C5Ferm = FMS706.Inlet.Total.Fw * FMS706.Inlet.Total.zw(flu.Xylose) * C5FermRaw * EcoPar.WorkedHours;
1781	#*
1782	*#
1783
1784	#------------------- Calculos extras ----------------------#
1785	VARIABLES
1786	HydrEthProd as flow_vol (Brief = "Hydrous Ethanol Volumetric Production @ 35 C");
1787	HydrEthSpecProd as Real (Brief = "Hydrous Ethanol Specific Production @ 35 C", Unit = 'l/t');
1788
1789	AnhyEthProd as flow_vol (Brief = "Anhydrous Ethanol Volumetric Production @ 35 C");
1790	AnhyEthSpecProd as Real (Brief = "Anhydrous Ethanol Specific Production @ 35 C", Unit = 'l/t');
1791
1792	VinasseProd as flow_vol (Brief = "Vinasse Volumetric Production @ 75 C");
1793	VinSpecProd as Real (Brief = "Vinasse Specific Production @ 75 C");
1794
1795	SteamCons(3) as flow_mass (Brief = "Steam Consumption by the Several Process Stages");
1796	SteamCons_total as flow_mass (Brief = "Steam Consumption");
1797	SteamSpecCons(3) as Real (Brief = "Steam Specific Consumption by the process", Unit = 'kg/t');
1798	SteamSpecConsEtOH(3) as Real (Brief = "Steam Specific Consumption by the Several Process Stages (Etanol Base)", Unit = 'kg/l');
1799
1800	Wtotal as potency (Brief = "Total Electric Energy Produced", Upper = 1e10);
1801	WCons(3) as potency (Brief = "Power Consumption by the Several Process Stages", Upper = 1e10);
1802	Wnet as potency (Brief = "Electric Energy Surplus Produced", Upper = 1e10);
1803
1804	EQUATIONS
1805	HydrEthProd = COL303.HydrEth.Fluid.Fw / (790.5 * 'kg/m^3');
1806
1807	HydrEthSpecProd = HydrEthProd / ProPar.SugarcaneFlow;
1808
1809	AnhyEthProd = DEH304.AnhyEth.Fluid.Fw / (778.24 * 'kg/m^3');
1810
1811	AnhyEthSpecProd = AnhyEthProd / ProPar.SugarcaneFlow;
1812
1813	VinasseProd = COL303.Vinasse.Fluid.Fw / (974.850 * 'kg/m^3'); #considerando a densidade da agua a 75 C
1814
1815	VinSpecProd = VinasseProd / AnhyEthProd;
1816
1817	SteamCons(1) = Cwq422.Inlet.Fw; #vapor de escape a 2.5 bar
1818	SteamCons(2) = Cwq414.Inlet.Fw; #vapor de 6 bar
1819	SteamCons(3) = Cwq407.Inlet.Fw; #vapor de 17.4 bar
1820	SteamCons_total = sum(SteamCons);
1821
1822	SteamSpecCons = SteamCons / ProPar.SugarcaneFlow;
1823
1824	SteamSpecConsEtOH = SteamCons / AnhyEthProd;
1825
1826	Wtotal = wTB404.Outlet_p.W + wTB410.Outlet_p.W + wTB418.Outlet_p.W;
1827
1828	WCons(1) = 16 * 'kW * h/t' * ProPar.SugarcaneFlow; #consumo da moenda Cortez rodrigues (2017) e pina (2017)
1829	WCons(2) = 12 * 'kW * h/t' * ProPar.SugarcaneFlow; #consumo do processo Cortez rodrigues (2017) e pina (2017)
1830	WCons(3) = 0 * 'kW';
1831
1832	Wnet = Wtotal - sum(WCons);
1833	#*
1834	*#
1835	#*--------------------------------------------
1836	* Pinch
1837	---------------------------------------------*#
1838
1839	PARAMETERS
1840	Pinch as Plugin (Type = "Pinch", numCorrentes = 15, numUtilQuente = 3, numUtilFria = 1);
1841
1842	DEVICES
1843	INT101 as heat_source_int;
1844	INT102 as heat_source_int;
1845	INT103 as heat_source_int;
1846	INT104 as heat_source_int;
1847
1848	SS101 as water_sourceR;
1849
1850	SS102 as water_sourceR;
1851	SS103 as water_sourceR;
1852	SS104 as water_sourceR;
1853
1854	PinchPoint as PinchPointInt;
1855
1856	TAC_HEN as TAC_HEN;
1857
1858
1859	#------Fonte de agua e vapor do pinch-------------#
1860
1861	CONNECTIONS
1862	# Fonte de agua de resfriamento
1863	SS101.Outlet to PinchPoint.Inlet_f(1);
1864
1865	#Fonte de baixa, media e alta
1866	SS102.Outlet to PinchPoint.Inlet_q(1);
1867	SS103.Outlet to PinchPoint.Inlet_q(2);
1868	SS104.Outlet to PinchPoint.Inlet_q(3);
1869
1870	SET
1871	SS101.ValidPhases = "Liquid-Only";
1872
1873	SS102.ValidPhases = "Vapour-Liquid";
1874	SS103.ValidPhases = "Vapour-Liquid";
1875	SS104.ValidPhases = "Vapour-Liquid";
1876
1877	PinchPoint.NCorrentes = 11; #numero de correntes de processo que trocam calor
1878	PinchPoint.NCorrentesInt = 4;#Numero de correntes que entram ou saem do interpolador
1879	PinchPoint.NUtilQuente = 3; #Numero de utilidades quentes
1880	PinchPoint.NUtilFria = 1; #Numero de utilidades frias
1881	PinchPoint.method = "h";
1882
1883	#Parametros para a estimativa do TAC da HEN
1884	TAC_HEN.a_annu = 4897 * 'US$/yr';
1885	TAC_HEN.b_annu = 33.0 * 'US$/(m^1.56)/yr';
1886	TAC_HEN.c_annu = 0.78;
1887	TAC_HEN.Cost_Hot_Util = 96 * 'US$/kW/yr';
1888	TAC_HEN.Cost_Cold_Util = 50 * 'US$/kW/yr';
1889
1890	SPECIFY
1891	#Temperatura minima de aproximacao
1892	PinchPoint.DTmin = 10 * 'K';
1893
1894	#Fonte de agua de resfriamento
1895	SS101.T = 303.15 * 'K';
1896	SS101.P = 1 * 'bar';
1897	PinchPoint.Outlet_f(1).T = 333.15 * 'K';
1898	PinchPoint.heat_trans_cold(1) = 1.38 * 'kW/m^2/K';
1899
1900	#Fonte de vapor
1901	SS102.P = 2.5 * 'bar';
1902	SS102.v = 1;
1903	PinchPoint.heat_trans_hot(1) = 1.38 * 'kW/m^2/K' ;
1904
1905	SS103.P = 6 * 'bar';
1906	SS103.v = 1;
1907	PinchPoint.heat_trans_hot(2) = 1.38 * 'kW/m^2/K' ;
1908
1909	SS104.P = 17.5 * 'bar';
1910	SS104.v = 1;
1911	PinchPoint.heat_trans_hot(3) = 1.38 * 'kW/m^2/K' ;
1912
1913	EQUATIONS
1914
1915	TAC_HEN.Area_HEN = PinchPoint.Area_HEN;
1916	TAC_HEN.Demand_Hot = Cwq422.Outlet_q.Q + Cwq414.Outlet_q.Q + Cwq407.Outlet_q.Q;
1917	TAC_HEN.Demand_Cold = PinchPoint.QC_total;
1918	TAC_HEN.num_util = PinchPoint.N_Troca;
1919
1920	#*----------Integracao correntes (aquecer ou resfriar) ------
1921	Os trocadores foram retirados e todas as correntes entram no pinch e
1922	retornam para o processo.
1923	*#
1924	CONNECTIONS
1925
1926	#Etapa de extracao e tratamento
1927	mMX113.Outlet to PinchPoint.Inlet(1);
1928	PinchPoint.Outlet(1) to LTS115.Inlet;
1929
1930	mPP116.Outlet to PinchPoint.Inlet(2);
1931	PinchPoint.Outlet(2) to mFL118.Inlet;
1932
1933	#Concentracao e fermentacao c6/c12
1934	mPP204.Outlet to PinchPoint.Inlet(3);
1935	PinchPoint.Outlet(3) to mMX205.Inlet1;
1936
1937	#destilacao
1938	mPP309.Outlet to PinchPoint.Inlet(4);
1939	PinchPoint.Outlet(4) to COL303.Wine;
1940
1941	COL303.Vinasse to PinchPoint.Inlet(5);
1942
1943	DEH304.RecMEG to PinchPoint.Inlet(6);
1944	PinchPoint.Outlet(6) to mPP307.Inlet;
1945
1946	#Pre-tratamento e hidrolise
1947	mMX502.Outlet to PinchPoint.Inlet(7);
1948	PinchPoint.Outlet(7) to RTS504.Inlet;
1949
1950	mPP505.Outlet to PinchPoint.Inlet(8);
1951	PinchPoint.Outlet(8)to mMX502.Inlet2;
1952
1953	RTS504.Outlet to PinchPoint.Inlet(9);
1954	PinchPoint.Outlet(9)to mFL508.Inlet;
1955
1956	mMX601.Outlet to PinchPoint.Inlet(10);
1957	PinchPoint.Outlet(10) to mMX603.Inlet1;
1958
1959	#Fermentacao Xilose
1960	mPP704.Outlet to PinchPoint.Inlet(11);
1961	PinchPoint.Outlet(11) to FMS706.Inlet;
1962
1963	SPECIFY
1964	#Temperatura que deve ser atendida na saida do "pinch"
1965	PinchPoint.Outlet(1).T = (70 + 273.15) * 'K';
1966	PinchPoint.Outlet(2).T = (105 + 273.15) * 'K';
1967	PinchPoint.Outlet(3).T = (33 + 273.15) * 'K';
1968	#PinchPoint.Outlet(4).T = (70 + 273.15) * 'K';
1969	PinchPoint.Outlet(4).T = (90 + 273.15) * 'K';
1970	PinchPoint.Outlet(5).T = (90 + 273.15) * 'K';
1971	PinchPoint.Outlet(6).T = (80 + 273.15) * 'K';
1972	PinchPoint.Outlet(7).T = (195 + 273.15) * 'K';
1973	PinchPoint.Outlet(8).T = (185 + 273.15) * 'K';
1974	PinchPoint.Outlet(9).T = (80 + 273.15) * 'K';
1975	PinchPoint.Outlet(10).T = (50 + 273.15) * 'K';
1976	PinchPoint.Outlet(11).T = (35 + 273.15) * 'K';
1977
1978	#Coeficiente de transferencia de calor para as correntes de calor: Calculo da HEN
1979	PinchPoint.heat_trans_corr(1:11) = 1.38 * 'kW/m^2/K';
1980
1981
1982	#------Pinch no trem de colunas de destilacao (interpolador) ----#
1983
1984	#* A etapa de destilacao conta com um interpolador
1985	Para contornar a falta de acessibilidade da informacao no black box
1986	foi criada uma nova energy stream que contem apenas informacoes de T e Q
1987	*#
1988	CONNECTIONS
1989	INT101.Outlet to PinchPoint.Inlet_Int(1);
1990	INT102.Outlet to PinchPoint.Inlet_Int(2);
1991	INT103.Outlet to PinchPoint.Inlet_Int(3);
1992	INT104.Outlet to PinchPoint.Inlet_Int(4);
1993
1994	SPECIFY
1995	#Coeficiente de transferencia de calor para as correntes de calor: Calculo da HEN
1996	PinchPoint.heat_trans_corr(12:15) = 1.38 * 'kW/m^2/K';
1997
1998	EQUATIONS
1999
2000	INT101.Outlet.T = COL303.SecGrad.T;
2001	INT102.Outlet.T = COL303.HydrEth.T;
2002
2003	INT101.Outlet.Q = -COL303.CD.Q;
2004	INT102.Outlet.Q = -COL303.CBB1.Q;
2005
2006	INT103.Outlet.Q = -DEH304.QCEXT.Q;
2007	INT104.Outlet.Q = -DEH304.QCREC.Q;
2008
2009	INT103.Outlet.T = DEH304.AnhyEth.T;
2010	INT104.Outlet.T = DEH304.Water.T;
2011
2012	#*
2013	*#
2014	#--------------------- integracoes -----------------------#
2015	#Integracao entre a cogeracao e as demandas do processo (pinch e outros equipamentos)
2016	EQUATIONS
2017
2018	#Vapor de 2.5 consumido
2019	Cwq422.Outlet_q.Q = PinchPoint.QH(1) +
2020	EVP202.Q +
2021	EVP702.Q +
2022	COL303.QAA1.Q +
2023	COL303.QBB1.Q;
2024
2025	#Vapor de 6 bar consumido
2026	Cwq414.Outlet_q.Q = PinchPoint.QH(2) +
2027	DEH304.QREXT.Q +
2028	DEH304.QRREC.Q;
2029
2030	#Vapor de 17.4 bar consumido
2031	Cwq407.Outlet_q.Q = PinchPoint.QH(3);
2032	#*
2033	*#
2034	#*
2035	-----------------------Analise economica-----------
2036	*#
2037
2038	DEVICES
2039	EcoPar as EconomicParameters (Brief = "Model With All the Assumptions Made");
2040
2041	VARIABLES
2042	RecExtCost as currency (Brief = "Investment in the Reception and Extration stage");
2043	EvapCost as currency (Brief = "Investment in the Evaporation stage");
2044	EtOHprodCost as currency (Brief = "Investment in the fermentation, distillation and dehydration stage (molecular sieve)");
2045	CHPCost as currency (Brief = "Investment in the Combined Heat and Power stage - steam and electricity");
2046	InfrastrutureCost as currency (Brief = "Investment in the Infrastruture, engineering and utilities");
2047	ReceptionCost as currency (Brief = "Investment in the Dust collection system and straw gathering stage");
2048
2049	IG_InstalledEquipment as currency; #1G custos diretos e indiretos, exceto contigencia
2050
2051	EQUATIONS
2052	#Alguns parametros das equacoes de estimacao foram obtidos por comunicacao pessoaL
2053	RecExtCost = ((139.15E6 / EcoPar.ExchangeRate) * 'US$' - EvapCost - ReceptionCost) *
2054	((ProPar.SugarcaneFlow * EcoPar.WorkedHours /(4E9 * 'kg'))^0.6); #fator de escala NREL, Humbird 2011
2055
2056	#Evaporador do tipo Roberts de inox - 4 milhoes de reais com 6000 m2 de area de troca termica
2057	EvapCost = (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP202.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2058	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP203.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2059	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP204.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2060	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP205.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2061	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP206.A /(6000 * 'm^2'))^0.54); #fator de escala peters
2062
2063	#uma usina que produziu 340milhoes m3 de etanol em uma safra com titulo de etanol de 70g/L
2064	EtOHprodCost = (173.0E6 / EcoPar.ExchangeRate) * 'US$' *
2065	(abs( FMS208.Inlet.Total.Fw * FMS208.Inlet.Total.zw (5) * EcoPar.WorkedHours /(340E3 * 'm^3' * 70 * 'g / l'))^0.6); #fator de escala NREL, Humbird 2011
2066
2067	CHPCost = (140.0E6 / EcoPar.ExchangeRate) * 'US$' * #400
2068	(abs((BLR403.Steam.Fw)/(200000 * 'kg/h'))^0.6); #fator de escala NREL, Humbird 2011
2069
2070	ReceptionCost = (6.9E5 / EcoPar.ExchangeRate )* 'US$' * 1.7 *
2071	(abs((ProPar.SugarcaneFlow + MSS102.Outlet.Total.Fw + MSS103.Outlet.Total.Fw)/(94967 * 'kg/h'))^0.6) +
2072	(1500000 / EcoPar.ExchangeRate) * 'US$' * (abs((MSS102.Outlet.Total.Fw + MSS104.Outlet.Total.Fw)/(15000 * 'kg/h'))^0.6) ; #fator de escala NREL, Humbird 2011
2073	#1.5 milhoes eh o custo total do recolhimento de palha
2074	#desde as modificacoes no campo para enfardar a palha,
2075	#modificacoes para receber os caminhoes
2076	#esteiras transportadoras e adaptacoes na caldeira.
2077	#(preco de 2016, atualiza???)
2078
2079	#instalacao de 25% nesse caso
2080	InfrastrutureCost = 0.25 * (RecExtCost + EvapCost + EtOHprodCost + CHPCost + ReceptionCost );
2081
2082	IG_InstalledEquipment = InfrastrutureCost + RecExtCost + EvapCost + EtOHprodCost + CHPCost + ReceptionCost;
2083
2084	VARIABLES
2085	OpEx_IG as currency (Brief = "Operational expenditure in the plant");
2086
2087	EQUATIONS
2088	#O custo para producao do etanol anidro eh um valor fechado - inclui todas as etapas
2089	#####
2090	OpEx_IG = 87.0 * 'US$/m^3' * AnhyEthProd * EcoPar.WorkedHours ; #Custo para producao do etanol anidro, jah em dolar
2091
2092	VARIABLES
2093	n_Enzymeprice as Real (Brief = "Price multiplicator");
2094	EnzymecostFinal as positive (Brief = "Enzyme final cost", Unit = 'US$ / kg'); #preco final da enzima comprada
2095
2096	EQUATIONS
2097	#Preco final da enzima ( utilizado para estudo do impacto do preco da enzima)
2098	EnzymecostFinal = EcoPar.EnzymeCost * n_Enzymeprice;
2099
2100	VARIABLES
2101	HEArea as positive ( Brief = "Mean area of Heat Exchanger Network", Unit = 'm^2');
2102	TDH_equalization as time_h;
2103
2104	SPECIFY
2105	TDH_equalization = 7.2 *'h';
2106
2107	EQUATIONS
2108	#Area media com base no numero de trocadores de calor
2109	PinchPoint.N_Troca * HEArea = PinchPoint.Area_HEN;
2110
2111	# ----- Etapa de pretratamento-------
2112
2113	VARIABLES
2114	TDH_mix as time_h;
2115	ConveyorBeltPretreatCost as currency;
2116	TankPretreatCost as currency;
2117	PumpPretreatCost as currency;
2118	TCPretreatCost as currency;
2119	ReactorCost as currency;
2120	FlashCost as currency;
2121	V_Flash as positive (Unit = 'm^3');
2122	Mass_Flash as positive (Unit = 'kg');
2123	BeltFilterPretreatCost as currency (Brief = "Investment in the belt filter vaccum press");
2124
2125	PreTreatSectorCost as currency (Brief = "Investment in the pre treatment stage");
2126
2127	SPECIFY
2128	TDH_mix = 1 *'h';
2129
2130	EQUATIONS
2131	#Os custos dos equipamentos consideram a instalacao no local
2132
2133	ConveyorBeltPretreatCost = 50 * 'm' * EcoPar.ConveyorBeltCost;
2134
2135	TankPretreatCost = EcoPar.ConcreteCost * TDH_mix *
2136	(mMX502.Inlet2.Total.Fw / (120 * 'kg/m^3') +
2137	mMX502.Inlet1.Total.Fw / (957 * 'kg/m^3')) ;
2138
2139	# 2 bombas - Considenrando somente bagaco na fase solida ro -> 120 kg/m^3
2140	PumpPretreatCost = (mPP501.Inlet.Total.Fw / (120 * 'kg/m^3') +
2141	mPP505.Inlet.Total.Fw / (1000 * 'kg/m^3')) *
2142	EcoPar.HighPumpCost;
2143
2144	# 2 trocadores
2145	TCPretreatCost = 2 * (350000) * 'US$' * (abs(HEArea/(150 * 'm^2'))^0.54) / EcoPar.ExchangeRate ; #TC placas titanio, agua e mosto (mesmo CP) s´o calor sensivel, FQ entra 95C e sai 32C e FF entra 28C, alto U
2146
2147	#60% de enchimento - maior custo da etapa!
2148	ReactorCost = (80E6 / EcoPar.ExchangeRate) * 'US$' *
2149	(abs( RTS504.Inlet.Total.Fw / 0.6 /(360000 * 'kg/h'))^0.56) ;
2150
2151	FlashCost = Mass_Flash * EcoPar.InoxCost;
2152
2153	V_Flash = (mFL508.Inlet.Solid.Fw / (120 * 'kg/m^3') +
2154	mFL508.Inlet.Fluid.Fw / (973 * 'kg/m^3')) * TDH_mix;
2155
2156	Mass_Flash = 2 * ProPar.pi * 6 * 'm' *
2157	(abs(2 * V_Flash / ProPar.pi / (6 'm')) ^ 0.5) 0.95 'cm' 7.85 * 'g/cm^3';
2158
2159	BeltFilterPretreatCost = (1300000 / EcoPar.ExchangeRate) * 'US$' *
2160	(abs( SEP511.Inlet.Total.Fw /(500000 * 'kg/h'))^ 0.8); #0.8 fator de escala do NREL,Humbird 2011
2161
2162	PreTreatSectorCost = EcoPar.PretreatmentInstalationFactor *
2163	(ConveyorBeltPretreatCost +
2164	TankPretreatCost +
2165	PumpPretreatCost +
2166	TCPretreatCost +
2167	ReactorCost +
2168	0.3 * ReactorCost + #acessorios do reator
2169	FlashCost +
2170	BeltFilterPretreatCost +
2171	(EcoPar.pHmetroCost / EcoPar.ExchangeRate ) * 'US$')
2172	;
2173
2174	# --------------Etapa de hidrolise ----------------------
2175	PARAMETERS
2176	n_ReactorHydrolysis as positive (Brief = "Number of hydrolysis reactor", Default = 1);
2177
2178	SET
2179	n_ReactorHydrolysis = 12;
2180	#foi setado em 12 baseado nas capacidades do NREL
2181
2182	VARIABLES
2183	ConveyorBeltHydrolysisCost as currency;
2184
2185	TankMixHydrolysisCost as currency (Brief = "Investment in the mix tank in the sector of hydrolisis");
2186	V_TankMixHydrolysis as positive (Brief = "Volume of the emix tank in the sector of hydrolisis", Unit = 'm^3');
2187	TCHydrolysisCost as currency (Brief = "Investment in the TC in the sector of hydrolisis");
2188	ReactorHydrolysisCost as currency (Brief = "Investment in the tank in the sector of hydrolisis");
2189
2190	V_ReactorHydrolysis as positive (Brief = "Volume of the tank in the sector of hydrolisis", Unit = 'm^3');
2191	H_ReactorHydrolysis as positive (Brief = "H of the tank in the sector of hydrolisis", Unit = 'm');
2192	D_ReactorHydrolysis as positive (Brief = "Diameter of the tank in the sector of hydrolisis", Unit = 'm');
2193	Vmaterial_ReactorHydrolysis as positive (Brief = "Volume of the material used in the construction of the reactor in the sector of hydrolisis", Unit = 'm^3');
2194
2195	PumpHydrolysisRecCost as currency;
2196	PumpDosingCost as currency;
2197	BeltFilterHydrolysisCost as currency (Brief = "Investment in the belt filter vaccun press in the sector of hydrolisis");
2198	PumpHydrolysisCost as currency;
2199	TankC6WineCost as currency;
2200
2201	HydrolysisSectorCost as currency (Brief = "Investment in the hydrolisis stage");
2202
2203	TDH_fermenter as time_h (Default = 5.4);
2204
2205
2206
2207	SPECIFY
2208	#TDH_fermenter = 5.4 * 'h';
2209
2210	EQUATIONS
2211	#correia transportadora do bagaco pretratado
2212	ConveyorBeltHydrolysisCost = 30 * 'm' * EcoPar.ConveyorBeltCost;
2213
2214	TankMixHydrolysisCost = EcoPar.ConcreteCost * V_TankMixHydrolysis;
2215
2216	PumpDosingCost = 5000 / EcoPar.ExchangeRate * 'US$';
2217
2218	V_TankMixHydrolysis = TDH_equalization *
2219	(SEP511.OutletS.Total.Fw / (120 * 'kg/m^3') + #densidade do bagaco a 50% umidade
2220	MSS601.Outlet.Total.Fw / (1000 * 'kg/m^3') + #densidade da agua
2221	MSS602.Outlet.Total.Fw / (1150 * 'kg/m^3')); #densidade da enzima de acordo Sigma
2222
2223	TCHydrolysisCost = (350000) * 'US$' (abs( HEArea /(150 'm^2'))^0.54) / EcoPar.ExchangeRate ;
2224
2225	ReactorHydrolysisCost = Vmaterial_ReactorHydrolysis * 7850 'kg/m^3' EcoPar.CarbonSteelCost;
2226	#densidade do aco carbono 7850
2227
2228	V_ReactorHydrolysis = HLS604.reac_time *
2229	(HLS604.Inlet.Solid.Fw / (120 * 'kg/m^3') +
2230	HLS604.Inlet.Fluid.Fw / (989 * 'kg/m^3')) *
2231	1.428571429/n_ReactorHydrolysis;
2232
2233	V_ReactorHydrolysis = 16 * ProPar.pi * (H_ReactorHydrolysis ^3)/9;
2234
2235	D_ReactorHydrolysis = (8/3) * H_ReactorHydrolysis;
2236
2237	Vmaterial_ReactorHydrolysis = ProPar.pi * (D_ReactorHydrolysis^2)0.0191'm'/4 + #0.191 e a espessura da base e
2238	ProPar.pi * (D_ReactorHydrolysis^2)0.0127'm'/(4*0.96592582628) + #0.0127 e a espessura da tampa do reator
2239	ProPar.pi * (D_ReactorHydrolysis)H_ReactorHydrolysis'm'*
2240	(0.38640.0191+0.07890.0159 +
2241	0.07890.0127 + 0.12630.0095 +
2242	0.12630.0079 + 0.20320.0064);
2243
2244	PumpHydrolysisRecCost = n_ReactorHydrolysis * (V_ReactorHydrolysis/HLS604.reac_time ) * EcoPar.HighPumpCost;
2245
2246	BeltFilterHydrolysisCost = (1300000 / EcoPar.ExchangeRate) * 'US$' *
2247	(( SEP606.Inlet.Total.Fw /(500000 * 'kg/h'))^0.8) ; #0.8 fator de escala do NREL
2248
2249	PumpHydrolysisCost = SEP606.OutletL.Total.Fw / (972.087 * 'kg/m^3') *
2250	EcoPar.HighPumpCost;
2251
2252	TankC6WineCost = EcoPar.ConcreteCost *
2253	mPP607.Outlet.Total.Fw * TDH_equalization / (ProPar.density_solution) ;
2254
2255	HydrolysisSectorCost = EcoPar.HydrolysisInstalationFactor *
2256	(ConveyorBeltHydrolysisCost +
2257	TankMixHydrolysisCost +
2258	PumpDosingCost +
2259	TCHydrolysisCost +
2260	n_ReactorHydrolysis * ReactorHydrolysisCost +
2261	0.3 * n_ReactorHydrolysis * ReactorHydrolysisCost + #acessorios dos reatores
2262	n_ReactorHydrolysis * 68000 * 'US$'+ #agitator of each reactor
2263	PumpHydrolysisRecCost +
2264	BeltFilterHydrolysisCost +
2265	ConveyorBeltHydrolysisCost +
2266	n_ReactorHydrolysis * PumpHydrolysisCost +
2267	TankC6WineCost)
2268	;
2269
2270	#-------- Etapa de fermentacao da C5 -------
2271	VARIABLES
2272	TankC5Cost as currency (Brief = "Investment in the equalization tank in the sector of C5 fermentation");
2273	V_TankC5Cost as positive (Brief = "Volume of the equalization tank in the sector of C5 fermentation", Unit = 'm^3');
2274	PumpFeedEvapC5Cost as currency (Brief = "Investment in the pump of evapotor feeding in the sector of C5 fermentation");
2275	EvaporatorC5Cost as currency (Brief = "Investment in the evaporator in the sector of C5 fermentation");
2276	PumpFeedReactorC5Cost as currency (Brief = "Investment in the pump of reactor feeding in the sector of C5 fermentationin");
2277	TCC5Cost as currency (Brief = "Investment in the TC in the sector of C5 fermentation");
2278	VolumeC5ferm as positive (Brief = "Volume of C5 fermenter", Unit = 'm^3');
2279	FermenterC5Cost as currency (Brief = "Investment in the fermenter of C5 fraction");
2280	C5FermSectorCost as currency (Brief = "Investment in the c5 fermentation stage");
2281
2282	EQUATIONS
2283	TankC5Cost = EcoPar.ConcreteCost * V_TankC5Cost ;
2284
2285	V_TankC5Cost = SEP511.OutletL.Total.Fw * TDH_equalization / (972.052 * 'kg/m^3') ;
2286
2287	PumpFeedEvapC5Cost = SEP511.OutletL.Total.Fw / (972.087 * 'kg/m^3') *
2288	EcoPar.HighPumpCost ;
2289
2290	EvaporatorC5Cost = (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP702.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2291	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP703.A /(6000 * 'm^2'))^0.54) #fator de escala peters
2292	+ (4E6 / EcoPar.ExchangeRate) * 'US$' * (abs( EVP704.A /(6000 * 'm^2'))^0.54); #fator de escala peters
2293
2294	PumpFeedReactorC5Cost =2 * EVP704.OutletL.Total.Fw / (947.179 * 'kg/m^3') *
2295	EcoPar.HighPumpCost;
2296
2297	TCC5Cost = (350000) * 'US$' (abs( HEArea /(150 'm^2'))^0.54) / EcoPar.ExchangeRate ;#area de troca termica de 4000 m2, TC
2298
2299	VolumeC5ferm = FMS706.Outlet.Total.Fw * TDH_fermenter / (994.01 * 'kg/m^3')/0.6;
2300
2301	FermenterC5Cost = (4.2E6 / EcoPar.ExchangeRate) * 'US$' *
2302	(abs( VolumeC5ferm /(1E3 * 'm^3'))^0.6) ; #pressao turn key
2303
2304	C5FermSectorCost = EcoPar.C5InstalationFactor *
2305	(TankC5Cost +
2306	PumpFeedEvapC5Cost +
2307	EvaporatorC5Cost +
2308	PumpFeedReactorC5Cost +
2309	TCC5Cost +
2310	FermenterC5Cost +
2311	1.3 * FermenterC5Cost) #acessorios do reator - reator continuo, mais controle que o convencional, leito recheado... (Milessi 2017)
2312	;
2313
2314	VARIABLES
2315	IIG_InstalledEquipment as currency; #2G custos diretos e indiretos, exceto contigencia
2316	TotalInstalledEquipment as currency; #1G2G custos diretos e indiretos, exceto contigencia
2317	TotalFixedCapital as currency;
2318	Contingency as currency;
2319	WorkingCapital as currency;
2320	Capex as currency;
2321
2322	EQUATIONS
2323	IIG_InstalledEquipment = PreTreatSectorCost + C5FermSectorCost + HydrolysisSectorCost;
2324	TotalInstalledEquipment = IIG_InstalledEquipment + IG_InstalledEquipment;
2325	TotalFixedCapital = IIG_InstalledEquipment + IG_InstalledEquipment + Contingency;
2326	Contingency = 0.08 * TotalFixedCapital;
2327	WorkingCapital = 0.1 * Capex;
2328
2329	Capex = TotalFixedCapital + WorkingCapital;
2330
2331	#total product cost estimation
2332	VARIABLES
2333	TotalInput as currency (Brief = "All inputs of the biorefinery - raw materials");
2334
2335	EQUATIONS
2336	#Agua esta sendo contabilizada nesta parte
2337	TotalInput =
2338	(EcoPar.SugarcaneCost/EcoPar.ExchangeRate) * ProPar.SugarcaneFlow * EcoPar.WorkedHours + #sugarcane costs
2339	(EcoPar.StrawCost/EcoPar.ExchangeRate) * MSS102.Outlet.Total.Fw * EcoPar.WorkedHours + #straw sugarcane costs
2340	Input_Treat+
2341	Input_ConcFerm +
2342	Input_C5Ferm +
2343	Input_Hydr +
2344	Input_PreTreat
2345	;
2346
2347	#utilities
2348	#custo da agua tratada 0.05 reais/m^3 - preco de 2018 de uma usina real
2349	#custo da agua desmi 2.44 reais/m^3 - preco de 2018 de uma usina real
2350	VARIABLES
2351	HotUtilitie_price as Real (Unit = 'US$/kW/h');
2352	HotUtilitie_cost as currency;
2353	ColdUtilitie_price as Real (Unit = 'US$/kW/h');
2354	ColdUtilitie_cost as currency;
2355	Utilities as currency;
2356
2357	SPECIFY
2358	ColdUtilitie_price = (174.363/EcoPar.ExchangeRate/(5760'h')) 'US$/kW'; #Oliveira 2017 #tempo de trabalho qe a Cassia considerou foi 5760 h
2359	HotUtilitie_price = (334.80/EcoPar.ExchangeRate/(5760'h')) 'US$/kW'; #Oliveira 2017 - idem
2360
2361	EQUATIONS
2362	HotUtilitie_cost = HotUtilitie_price * EcoPar.WorkedHours *
2363	(PinchPoint.QH(1) + #2.5 bar
2364	PinchPoint.QH(2) + #6 bar
2365	PinchPoint.QH(3)); #17 bar
2366
2367	ColdUtilitie_cost = ColdUtilitie_price * EcoPar.WorkedHours * PinchPoint.QC(1); # agua de resfriamento
2368
2369	Utilities = HotUtilitie_cost +
2370	ColdUtilitie_cost;
2371
2372	VARIABLES
2373	Revenue as currency;
2374	OperatingLabor as currency (Brief = "Costs with skilled and unskilled labor");
2375	OperatingSupervision as currency (Brief = "Costs with direct supervisory and clerical labor");
2376	MaintenanceCost as currency;
2377	OperatingSupplies as currency;
2378	LaboratoryCharges as currency (Brief = "Costs with tests for control of operations and for product-quality control");
2379	PatentsRoyalts as currency;
2380	DirectProductionCosts as currency (Brief = "Costs directly associated with the manufacturing operation");
2381
2382	PlantOverheadCost as currency (Brief = "Safety services - not vary widely with changes in production rate");
2383	ManufacteringCosts as currency;
2384
2385	AdmCosts as currency (Brief = "Costs for executive, office supplies, engineering...");
2386	ResearchDevelopmentCost as currency (Brief = "Costs with research and development");
2387	DistribuitionMarketing as currency;
2388	GeneralExpenses as currency (Brief = "General expenses involved in company operations - addition to the manufacturing costs");
2389
2390	TotalProductCost as currency;
2391
2392	EQUATIONS
2393	Revenue = (AnhyEthProd * EcoPar.EthanolPrice + Wnet * EcoPar.EnergyPrice ) * EcoPar.WorkedHours;
2394
2395	OperatingLabor = EcoPar.WorkedHours *
2396	(49.55/EcoPar.ExchangeRate * 'US$/m^3' * EcoPar.Ethanol1GProduction + # Mao de obra do 1G - Pecege 2011
2397	(AnhyEthProd - EcoPar.Ethanol1GProduction ) * 11 * 'US$/m^3' ); # Mao de obra 2G - material suplementar Jonker et 2015
2398
2399	#MaintenanceCost = 3 / 100 * TotalFixedCapital; #baseado em Milanez et al 2015, Jonker 2015, junqueira et al. 2017
2400	MaintenanceCost = EcoPar.WorkedHours * (65.52/EcoPar.ExchangeRate) * 'US$/m^3' * EcoPar.Ethanol1GProduction + #pecege 2011
2401	0.03 * IIG_InstalledEquipment; #jonker 2015
2402
2403	OperatingSupervision = 0.1 * OperatingLabor;
2404	#varia de 10% a 20%, pegamos o menor valor pq nesse caso eh soh do 2g
2405	#e nao precisaria de aumentar uma estrutura completa, pois jah
2406	#tem da planta 1G
2407
2408	OperatingSupplies = 0.15 * MaintenanceCost; #peters 2002
2409
2410	LaboratoryCharges = 0.15 * OperatingLabor; #peters 2002
2411
2412	#PatentsRoyalts = 0.01 * TotalProductCost; #peters 2002
2413	PatentsRoyalts = 0.01 * DirectProductionCosts; #peters 2002
2414	#de 0 a 6% do custo total de producao,pegamos
2415	#valor baixo pq seria patente apenas do processo 2G
2416
2417	DirectProductionCosts = TotalInput +
2418	Utilities +
2419	OperatingLabor +
2420	OperatingSupervision +
2421	MaintenanceCost +
2422	OperatingSupplies +
2423	PatentsRoyalts +
2424	LaboratoryCharges;
2425
2426	PlantOverheadCost = 0.6 * (OperatingLabor +
2427	OperatingSupervision +
2428	MaintenanceCost); #peters 2002, valor intermediario entre 0.5 e 0.7
2429
2430	ManufacteringCosts =
2431	DirectProductionCosts +
2432	#FixedCharges +
2433	PlantOverheadCost;
2434
2435	AdmCosts = 0.20 * (OperatingLabor +
2436	OperatingSupervision +
2437	MaintenanceCost); #peters 2002, valor intermediario entre 0.15 e 0.25
2438
2439	ResearchDevelopmentCost = 2/100 * Revenue;
2440
2441	DistribuitionMarketing = 0.05 * TotalProductCost;
2442
2443	GeneralExpenses = AdmCosts + DistribuitionMarketing + ResearchDevelopmentCost;
2444
2445	TotalProductCost = GeneralExpenses + ManufacteringCosts;
2446
2447	VARIABLES
2448	Depreciation as currency (Brief = "Decrease in value throughout the usual life of the material");
2449	Tax(3) as currency;
2450	CashFlow(28) as currency;
2451	CF(28) as currency;
2452	NPV as currency;
2453
2454	EQUATIONS
2455	Depreciation = 0.1 * TotalFixedCapital;
2456
2457	if (Revenue - TotalProductCost - Depreciation) > 0 * 'US$' then
2458	Tax(1) = (Revenue - TotalProductCost - Depreciation) * 0.34;
2459	else
2460	Tax(1) = 0 * 'US$';
2461	end
2462
2463	if (Revenue - TotalProductCost) > 0 * 'US$' then
2464	Tax(2) = (Revenue - TotalProductCost)*0.34;
2465	else
2466	Tax(2) = 0 * 'US$';
2467	end
2468
2469	if (Revenue - TotalProductCost + WorkingCapital) > 0 * 'US$' then
2470	Tax(3) = (Revenue - TotalProductCost + WorkingCapital) * 0.34;
2471	else
2472	Tax(3) = 0 * 'US$';
2473	end
2474
2475	CashFlow(1:2) = -TotalFixedCapital/2;
2476	CashFlow(3) = -WorkingCapital;
2477	CashFlow(4:13) = Revenue - TotalProductCost - Tax(1);
2478	CashFlow(14:27) = Revenue - TotalProductCost - Tax(2);
2479	CashFlow(28) = Revenue - TotalProductCost - Tax(3) + WorkingCapital;
2480
2481	for i in [1:28] do
2482	CF(i) * (1 + EcoPar.r)^(i-1) = CashFlow(i);
2483	end
2484
2485	NPV = sum(CF);
2486
2487	SPECIFY
2488	#NPV = 0 * 'US$';
2489
2490	#*
2491	*#
2492
2493	#----------------------Analise de Ciclo de vida -----------------#
2494	PARAMETERS
2495	gwp as Renovabio (Brief = "Parametros de acordo com a planilha RenovaCalc");
2496	ad as AD_SimaPro;
2497	odp as ODP_SimaPro;
2498	ht as HT_SimaPro;
2499	fwaet as FWAET_SimaPro;
2500	maet as MAET_SimaPro;
2501	tet as TET_SimaPro;
2502	po as PO_SimaPro;
2503	ac as AC_SimaPro;
2504	eu as EU_SimaPro;
2505
2506	PCI as PCI (Brief = "Poder de combustao inferior");
2507
2508	#Emissao Campo
2509	VARIABLES
2510	GWP100_cana as positive (Unit = 'kg/h');
2511	AD_cana as positive (Unit = 'kg/h');
2512	ODP_cana as positive (Unit = 'kg/h');
2513	HT_cana as positive (Unit = 'kg/h');
2514	FWAET_cana as positive (Unit = 'kg/h');
2515	MAET_cana as positive (Unit = 'kg/h');
2516	TET_cana as positive (Unit = 'kg/h');
2517	PO_cana as positive (Unit = 'kg/h');
2518	AC_cana as positive (Unit = 'kg/h');
2519	EU_cana as positive (Unit = 'kg/h');
2520
2521	EQUATIONS
2522	GWP100_cana = ProPar.SugarcaneFlow * gwp.cana_de_acucar_B9;
2523	AD_cana = ProPar.SugarcaneFlow * ad.cana_de_acucar_B9;
2524	ODP_cana = ProPar.SugarcaneFlow * odp.cana_de_acucar_B9;
2525	HT_cana = ProPar.SugarcaneFlow * ht.cana_de_acucar_B9;
2526	FWAET_cana = ProPar.SugarcaneFlow * fwaet.cana_de_acucar_B9;
2527	MAET_cana = ProPar.SugarcaneFlow * maet.cana_de_acucar_B9;
2528	TET_cana = ProPar.SugarcaneFlow * tet.cana_de_acucar_B9;
2529	PO_cana = ProPar.SugarcaneFlow * po.cana_de_acucar_B9;
2530	AC_cana = ProPar.SugarcaneFlow * ac.cana_de_acucar_B9;
2531	EU_cana = ProPar.SugarcaneFlow * eu.cana_de_acucar_B9;
2532
2533	#Emissao agua
2534	VARIABLES
2535	total_water_inlet as flow_mass;
2536	GWP100_agua as positive (Unit = 'kg/h');
2537	AD_agua as positive (Unit = 'kg/h');
2538	ODP_agua as positive (Unit = 'kg/h');
2539	HT_agua as positive (Unit = 'kg/h');
2540	FWAET_agua as positive (Unit = 'kg/h');
2541	MAET_agua as positive (Unit = 'kg/h');
2542	TET_agua as positive (Unit = 'kg/h');
2543	PO_agua as positive (Unit = 'kg/h');
2544	AC_agua as positive (Unit = 'kg/h');
2545	EU_agua as positive (Unit = 'kg/h');
2546
2547	EQUATIONS
2548	total_water_inlet =
2549	MSS106.Outlet.Fluid.Fw + # Agua que entra no 5 terno
2550	MSS108.Outlet.Fluid.Fw + # Agua utilizada na diluicao da cal
2551	MSS109.Outlet.Fluid.Fw + # Agua utilizada na diluicao do polimero
2552	MSS110.Outlet.Fluid.Fw + # Agua para filtracao do 1G
2553	MSS203.Outlet.Fluid.Fw + # Agua para a adsorcao
2554	MSS204.Outlet.Fluid.Fw + # Agua para diluicao da levedura/acido sulfurico
2555	#WSS402.Outlet.Fw + # Agua de reposicao da cogeracao - outra especificao... agua desmi
2556	MSS501.Outlet.Fluid.Fw + # Agua para diluicao do pretratamento
2557	MSS503.Outlet.Fluid.Fw + # Agua para diluicao do pretratamento(nula)
2558	MSS601.Outlet.Fluid.Fw + # Agua para diluicao da hidrolise
2559	MSS603.Outlet.Fluid.Fw # Agua para diluicao da hidrolise (nula)
2560	;
2561
2562	GWP100_agua = total_water_inlet * gwp.agua;
2563	AD_agua = total_water_inlet * ad.agua;
2564	ODP_agua = total_water_inlet * odp.agua;
2565	HT_agua = total_water_inlet * ht.agua;
2566	FWAET_agua = total_water_inlet * fwaet.agua;
2567	MAET_agua = total_water_inlet * maet.agua;
2568	TET_agua = total_water_inlet * tet.agua;
2569	PO_agua = total_water_inlet * po.agua;
2570	AC_agua = total_water_inlet * ac.agua;
2571	EU_agua = total_water_inlet * eu.agua;
2572
2573	#Emissao caldeira
2574	VARIABLES
2575	palha as flow_mass;
2576	bagaco as flow_mass;
2577	efluente_2G as flow_mass;
2578
2579	GWP100_caldeira as positive (Unit = 'kg/h');
2580	AD_caldeira as positive (Unit = 'kg/h');
2581	ODP_caldeira as positive (Unit = 'kg/h');
2582	HT_caldeira as positive (Unit = 'kg/h');
2583	FWAET_caldeira as positive (Unit = 'kg/h');
2584	MAET_caldeira as positive (Unit = 'kg/h');
2585	TET_caldeira as positive (Unit = 'kg/h');
2586	PO_caldeira as positive (Unit = 'kg/h');
2587	AC_caldeira as positive (Unit = 'kg/h');
2588	EU_caldeira as positive (Unit = 'kg/h');
2589
2590	EQUATIONS
2591	#Total de palha que entra no misturador da caldeira, em base seca
2592	palha = mMX104.Outlet.Total.Fw - mMX104.Outlet.Total.Fw * mMX104.Outlet.Total.zw(flu.Water);
2593
2594	#Total de bagaco que entra no misturador da caldeira, em base seca
2595	bagaco = mSP126.Outlet2.Total.Fw - mSP126.Outlet2.Total.Fw * mSP126.Outlet2.Total.zw(flu.Water);
2596
2597	#Total de material lignocelulosico que entra no misturador da caldeira, em base seca
2598	efluente_2G = SEP606.OutletS.Total.Fw - SEP606.OutletS.Total.Fw * SEP606.OutletS.Total.zw(flu.Water);
2599
2600	GWP100_caldeira =
2601	bagaco * gwp.bagaco +
2602	palha * gwp.palha +
2603	efluente_2G * gwp.bagaco # assumido igual bagaco
2604	;
2605	AD_caldeira =
2606	bagaco * ad.bagaco +
2607	palha * ad.palha +
2608	efluente_2G * ad.bagaco # assumido igual bagaco
2609	;
2610	ODP_caldeira =
2611	bagaco * odp.bagaco +
2612	palha * odp.palha +
2613	efluente_2G * odp.bagaco # assumido igual bagaco
2614	;
2615	HT_caldeira =
2616	bagaco * ht.bagaco +
2617	palha * ht.palha +
2618	efluente_2G * ht.bagaco # assumido igual bagaco
2619	;
2620	FWAET_caldeira =
2621	bagaco * fwaet.bagaco +
2622	palha * fwaet.palha +
2623	efluente_2G * fwaet.bagaco # assumido igual bagaco
2624	;
2625	MAET_caldeira =
2626	bagaco * maet.bagaco +
2627	palha * maet.palha +
2628	efluente_2G * maet.bagaco # assumido igual bagaco
2629	;
2630	TET_caldeira =
2631	bagaco * tet.bagaco +
2632	palha * tet.palha +
2633	efluente_2G * tet.bagaco # assumido igual bagaco
2634	;
2635	PO_caldeira =
2636	bagaco * po.bagaco +
2637	palha * po.palha +
2638	efluente_2G * po.bagaco # assumido igual bagaco
2639	;
2640	AC_caldeira =
2641	bagaco * ac.bagaco +
2642	palha * ac.palha +
2643	efluente_2G * ac.bagaco # assumido igual bagaco
2644	;
2645	EU_caldeira =
2646	bagaco * eu.bagaco +
2647	palha * eu.palha +
2648	efluente_2G * eu.bagaco # assumido igual bagaco
2649	;
2650	#Emissao outros insumos
2651	VARIABLES
2652	GWP100_insumos as positive (Unit = 'kg/h');
2653	AD_insumos as positive (Unit = 'kg/h');
2654	ODP_insumos as positive (Unit = 'kg/h');
2655	HT_insumos as positive (Unit = 'kg/h');
2656	FWAET_insumos as positive (Unit = 'kg/h');
2657	MAET_insumos as positive (Unit = 'kg/h');
2658	TET_insumos as positive (Unit = 'kg/h');
2659	PO_insumos as positive (Unit = 'kg/h');
2660	AC_insumos as positive (Unit = 'kg/h');
2661	EU_insumos as positive (Unit = 'kg/h');
2662
2663	GWP100_enzima as positive (Unit = 'kg/h');
2664	AD_enzima as positive (Unit = 'kg/h');
2665	ODP_enzima as positive (Unit = 'kg/h');
2666	HT_enzima as positive (Unit = 'kg/h');
2667	FWAET_enzima as positive (Unit = 'kg/h');
2668	MAET_enzima as positive (Unit = 'kg/h');
2669	TET_enzima as positive (Unit = 'kg/h');
2670	PO_enzima as positive (Unit = 'kg/h');
2671	AC_enzima as positive (Unit = 'kg/h');
2672	EU_enzima as positive (Unit = 'kg/h');
2673
2674	EQUATIONS
2675	GWP100_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * gwp.enzima_celulase;
2676	AD_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * ad.enzima_celulase;
2677	ODP_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * odp.enzima_celulase;
2678	HT_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * ht.enzima_celulase;
2679	FWAET_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * fwaet.enzima_celulase;
2680	MAET_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * maet.enzima_celulase;
2681	TET_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * tet.enzima_celulase;
2682	PO_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * po.enzima_celulase;
2683	AC_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * ac.enzima_celulase;
2684	EU_enzima = MSS602.Outlet.Total.Fw * MSS602.Outlet.Total.zw(NComp + sol.Enzyme) * eu.enzima_celulase;
2685
2686	GWP100_insumos =
2687	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * gwp.acido_fosforico +
2688	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * gwp.cal +
2689	MSS109.Fluid.Fw * gwp.floculante +
2690	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * gwp.amonia +
2691	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * gwp.acido_sulfurico +
2692	F_MEG * gwp.etileno_glicol +
2693	GWP100_enzima
2694	;
2695	AD_insumos =
2696	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * ad.acido_fosforico +
2697	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * ad.cal +
2698	MSS109.Fluid.Fw * ad.floculante +
2699	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * ad.amonia +
2700	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * ad.acido_sulfurico +
2701	F_MEG * ad.etileno_glicol +
2702	AD_enzima
2703	;
2704	ODP_insumos =
2705	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * odp.acido_fosforico +
2706	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * odp.cal +
2707	MSS109.Fluid.Fw * odp.floculante +
2708	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * odp.amonia +
2709	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * odp.acido_sulfurico +
2710	F_MEG * odp.etileno_glicol +
2711	ODP_enzima
2712	;
2713	HT_insumos =
2714	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * ht.acido_fosforico +
2715	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * ht.cal +
2716	MSS109.Fluid.Fw * ht.floculante +
2717	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * ht.amonia +
2718	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * ht.acido_sulfurico +
2719	F_MEG * ht.etileno_glicol +
2720	HT_enzima
2721	;
2722	FWAET_insumos =
2723	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * fwaet.acido_fosforico +
2724	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * fwaet.cal +
2725	MSS109.Fluid.Fw * fwaet.floculante +
2726	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * fwaet.amonia +
2727	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * fwaet.acido_sulfurico +
2728	F_MEG * fwaet.etileno_glicol +
2729	FWAET_enzima
2730	;
2731	MAET_insumos =
2732	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * maet.acido_fosforico +
2733	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * maet.cal +
2734	MSS109.Fluid.Fw * maet.floculante +
2735	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * maet.amonia +
2736	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * maet.acido_sulfurico +
2737	F_MEG * maet.etileno_glicol +
2738	MAET_enzima
2739	;
2740	TET_insumos =
2741	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * tet.acido_fosforico +
2742	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * tet.cal +
2743	MSS109.Fluid.Fw * tet.floculante +
2744	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * tet.amonia +
2745	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * tet.acido_sulfurico +
2746	F_MEG * tet.etileno_glicol +
2747	TET_enzima
2748	;
2749	PO_insumos =
2750	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * po.acido_fosforico +
2751	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * po.cal +
2752	MSS109.Fluid.Fw * po.floculante +
2753	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * po.amonia +
2754	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * po.acido_sulfurico +
2755	F_MEG * po.etileno_glicol +
2756	PO_enzima
2757	;
2758	AC_insumos =
2759	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * ac.acido_fosforico +
2760	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * ac.cal +
2761	MSS109.Fluid.Fw * ac.floculante +
2762	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * ac.amonia +
2763	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * ac.acido_sulfurico +
2764	F_MEG * ac.etileno_glicol +
2765	AC_enzima
2766	;
2767	EU_insumos =
2768	MSS107.Outlet.Total.Fw * MSS107.Outlet.Total.zw(flu.PhosphoricAcid) * eu.acido_fosforico +
2769	MSS108.Outlet.Total.Fw * MSS108.Outlet.Total.zw(NComp + sol.CaOH2) * eu.cal +
2770	MSS109.Fluid.Fw * eu.floculante +
2771	MSS202.Outlet.Total.Fw * MSS202.Outlet.Total.zw(flu.Ammonia) * eu.amonia +
2772	MSS205.Outlet.Total.Fw * MSS205.Outlet.Total.zw(flu.H2SO4) * eu.acido_sulfurico +
2773	F_MEG * eu.etileno_glicol +
2774	EU_enzima
2775	;
2776
2777	#Emissao total
2778	VARIABLES
2779	GWP100_total as positive (Unit = 'kg/h');
2780	AD_total as positive (Unit = 'kg/h');
2781	ODP_total as positive (Unit = 'kg/h');
2782	HT_total as positive (Unit = 'kg/h');
2783	FWAET_total as positive (Unit = 'kg/h');
2784	MAET_total as positive (Unit = 'kg/h');
2785	TET_total as positive (Unit = 'kg/h');
2786	PO_total as positive (Unit = 'kg/h');
2787	AC_total as positive (Unit = 'kg/h');
2788	EU_total as positive (Unit = 'kg/h');
2789
2790	GWP100_total_enzima as positive (Brief = " kg CO2 eq/h ");
2791
2792	EQUATIONS
2793	GWP100_total_enzima = GWP100_enzima / GWP100_total;
2794
2795	GWP100_total = GWP100_cana +
2796	GWP100_agua +
2797	GWP100_caldeira +
2798	GWP100_insumos
2799	;
2800	AD_total = AD_cana +
2801	AD_agua +
2802	AD_caldeira +
2803	AD_insumos
2804	;
2805	ODP_total = ODP_cana +
2806	ODP_agua +
2807	ODP_caldeira +
2808	ODP_insumos
2809	;
2810	HT_total = HT_cana +
2811	HT_agua +
2812	HT_caldeira +
2813	HT_insumos
2814	;
2815	FWAET_total = FWAET_cana +
2816	FWAET_agua +
2817	FWAET_caldeira +
2818	FWAET_insumos
2819	;
2820	MAET_total = MAET_cana +
2821	MAET_agua +
2822	MAET_caldeira +
2823	MAET_insumos
2824	;
2825	TET_total = TET_cana +
2826	TET_agua +
2827	TET_caldeira +
2828	TET_insumos
2829	;
2830	PO_total = PO_cana +
2831	PO_agua +
2832	PO_caldeira +
2833	PO_insumos
2834	;
2835	AC_total = AC_cana +
2836	AC_agua +
2837	AC_caldeira +
2838	AC_insumos
2839	;
2840	EU_total = EU_cana +
2841	EU_agua +
2842	EU_caldeira +
2843	EU_insumos
2844	;
2845	#Emissao total por MJ de etanol anidro
2846	VARIABLES
2847	GWP100 as Real (Brief = " kg CO2 eq/MJ ethanol", Unit = 'kg/MJ');
2848	AD as Real (Brief = " kg Sb eq /MJ ethanol", Unit = 'kg/MJ');
2849	ODP as Real (Brief = " kg CFC-11 eq/MJ ethanol", Unit = 'kg/MJ');
2850	HT as Real (Brief = " kg 1,4DB eq/MJ ethanol", Unit = 'kg/MJ');
2851	FWAET as Real (Brief = " kg 1,4DB eq/MJ ethanol", Unit = 'kg/MJ');
2852	MAET as Real (Brief = " kg 1,4DB eq/MJ ethanol", Unit = 'kg/MJ');
2853	TET as Real (Brief = " kg 1,4DB eq/MJ ethanol", Unit = 'kg/MJ');
2854	PO as Real (Brief = " kg C2H4 eq/MJ ethanol", Unit = 'kg/MJ');
2855	AC as Real (Brief = " kg SO2 eq/MJ ethanol", Unit = 'kg/MJ');
2856	EU as Real (Brief = " kg PO4-3 eq/MJ ethanol", Unit = 'kg/MJ');
2857
2858	EQUATIONS
2859	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * GWP100 = GWP100_total;
2860	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * AD = AD_total;
2861	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * ODP = ODP_total;
2862	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * HT = HT_total;
2863	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * FWAET = FWAET_total;
2864	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * MAET = MAET_total;
2865	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * TET = TET_total;
2866	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * PO = PO_total;
2867	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * AC = AC_total;
2868	DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro * EU = EU_total;
2869
2870	#*
2871	*#
2872	#*--------------------------- Alocacao Energetica ---------------------#
2873	* A alocacao energetica foi realizada levando em consideracao apenas etanol e energia
2874	* eletrica como produtos da biorrefinaria
2875	*#
2876	VARIABLES
2877	frac_allo(2) as fraction (Brief = "Energy allocation fraction ");
2878	frac_allo_eco(2) as fraction (Brief = "Energy allocation fraction ");
2879	total_energy_coproducts as Real (Brief = "Total energy produced" , Unit = 'MJ/h');
2880
2881	GWP100_Allo_eco as Real (Brief = " kg CO2 eq/MJ ethanol after ECONOMIC allocation ", Unit = 'g/MJ');
2882
2883	GWP100_Allo as Real (Brief = " kg CO2 eq/MJ ethanol after energy allocation ", Unit = 'g/MJ');
2884	AD_Allo as Real (Brief = " kg Sb eq /MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2885	ODP_Allo as Real (Brief = " kg CFC-11 eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2886	HT_Allo as Real (Brief = " kg 1,4DB eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2887	FWAET_Allo as Real (Brief = " kg 1,4DB eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2888	MAET_Allo as Real (Brief = " kg 1,4DB eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2889	TET_Allo as Real (Brief = " kg 1,4DB eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2890	PO_Allo as Real (Brief = " kg C2H4 eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2891	AC_Allo as Real (Brief = " kg SO2 eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2892	EU_Allo as Real (Brief = " kg PO4-3 eq/MJ ethanol after energy allocation ", Unit = 'kg/MJ');
2893
2894	EQUATIONS
2895	total_energy_coproducts = DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro + Wnet ;
2896	frac_allo(1) * total_energy_coproducts = DEH304.AnhyEth.Total.Fw * PCI.etanol_anidro; #Ethanol
2897	frac_allo(2) = 1 - frac_allo(1); #Electricity
2898
2899	GWP100_Allo = GWP100 * frac_allo(1);
2900	AD_Allo = AD * frac_allo(1);
2901	ODP_Allo = ODP * frac_allo(1);
2902	HT_Allo = HT * frac_allo(1);
2903	FWAET_Allo = FWAET * frac_allo(1);
2904	MAET_Allo = MAET * frac_allo(1);
2905	TET_Allo = TET * frac_allo(1);
2906	PO_Allo = PO * frac_allo(1);
2907	AC_Allo = AC * frac_allo(1);
2908	EU_Allo = EU * frac_allo(1);
2909
2910	frac_allo_eco(1) * Revenue = AnhyEthProd * EcoPar.EthanolPrice * EcoPar.WorkedHours; #Ethanol
2911	frac_allo_eco(2) = 1 - frac_allo_eco(1); #Electricity
2912	GWP100_Allo_eco = GWP100 * frac_allo_eco(1);
2913
2914	#*
2915	*#
2916
2917	#----------------------- Variaveis estudadas-----------------------#
2918	SPECIFY
2919	#principais condicoes operacionais fermentador de C5
2920	#Produtividade = 4.78 * 'g/l/h';
2921	Conc_xylose = 60 * 'g/l';
2922	#Conc_ethanol = 28 * 'g/l';
2923	#Yps_fermenter = 0.46;
2924	TDH_fermenter = 5.4 * 'h';# default
2925
2926	FMS706.conv(4) = 0.917742;# default
2927
2928	#FMS706.conv(4) = 0.957; # Limite da conversao da xilose para etanol
2929	#FMS706.conv(4) = 0.7656; # Conversao de 80% da xilose para etanol
2930	#FMS706.conv(4) = 0.5742; # Conversao de 60% da xilose para etanol
2931	#FMS706.conv(4) = 0.3828; # Conversao de 40% da xilose para etanol
2932
2933	#principais condicoes operacionais hidrolise
2934	EnzymeConc = 150 * 'g/l';
2935
2936	n_Enzymeprice = 1;
2937
2938	#Para a analise retro
2939	#SolMassFracHydro = 0.10;# default
2940	SolMassFracHydro = 0.14;
2941
2942	#HLS604.reac_time = 96 * 'h';# default
2943	HLS604.reac_time = 76 * 'h';
2944
2945	HLS604.Outlet.T = (50 + 273.15) * 'K';# default
2946
2947	EnzymeLoad = 10;# default
2948	#EnzymeLoad = 10;
2949	#EnzymeLoad = 20;
2950
2951	HLS604.conv = [0.756]; # default
2952	#HLS604.conv = [0.55716];
2953
2954	#Principais variaveis pretratamento
2955
2956	#SolMassFracPre = 0.2;
2957	SolMassFracPre = 0.10; # default
2958
2959	RTS504.conv(1) = [0.0812];# default
2960	#RTS504.conv(1) = [0.05];
2961	#RTS504.conv(1) = [0.15];
2962
2963	RTS504.conv(2:3) = [0.0007, 0.0528];
2964
2965	RTS504.conv(4) = [0.4653];# default
2966	#RTS504.conv(4) = [0.45];
2967	#RTS504.conv(4) = [0.55];
2968
2969	RTS504.conv(5:8)= [0.2577, 0.0389, 0.0739, 0.172];
2970
2971	RTS504.Outlet.T = (195 + 273.15) * 'K'; # default
2972	#RTS504.Outlet.T = (458.15) * 'K';
2973	#RTS504.Outlet.T = (468.15) * 'K';
2974
2975	#*
2976	*#
2977	OPTIONS
2978	Dynamic = false;
2979	GuessFile = "var1_2_teste.rlt";
2980
2981	NLASolver(
2982	File = "nlasolver",
2983	#File = "sundials",
2984	RelativeAccuracy = 1e-3,
2985	AbsoluteAccuracy = 1e-6,
2986	MaxIterations = 100
2987	);
2988
2989	end

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