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column.mso @ 102

Last change on this file since 102 was 102, checked in by Paula Bettio Staudt, 15 years ago
updated Distillation_thermosyphon_subcooling model in column.mso
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[72]	1	#*-------------------------------------------------------------------
	2	* EMSO Model Library (EML) Copyright (C) 2004 - 2007 ALSOC.
	3	*
	4	* This LIBRARY is free software; you can distribute it and/or modify
	5	* it under the therms of the ALSOC FREE LICENSE as available at
	6	* http://www.enq.ufrgs.br/alsoc.
	7	*
	8	* EMSO Copyright (C) 2004 - 2007 ALSOC, original code
	9	* from http://www.rps.eng.br Copyright (C) 2002-2004.
	10	* All rights reserved.
	11	*
	12	* EMSO is distributed under the therms of the ALSOC LICENSE as
	13	* available at http://www.enq.ufrgs.br/alsoc.
	14	*
	15	*----------------------------------------------------------------------
[1]	16	* File containg models of columns: distillation, stripping, absorbers
	17	* rectifier, ....
	18	*
	19	* The default nomenclature is:
	20	* Type_Column_reboilertype_condensertyper
	21	*
	22	* where:
	23	* Type = refluxed or reboiled or section
	24	* Column = Stripping, Absorption, Rectifier, Distillation
	25	* Reboiler type (if exists) = kettle or thermosyphon
	26	* Condenser type (if exists) = with subccoling or without subcooling
	27	*
	28	*-----------------------------------------------------------------------
	29	* Author: Paula B. Staudt
	30	* $Id: column.mso 102 2007-01-09 16:06:00Z paula $
	31	---------------------------------------------------------------------#
	32
	33	using "tray";
	34	using "reboiler";
	35	using "condenser";
	36	using "mixers_splitters/splitter";
[6]	37	using "mixers_splitters/mixer";
[1]	38	using "tank";
	39	using "pressure_changers/pump";
	40
	41	#*----------------------------------------------------------------------
	42	* Model of a column section with:
	43	* - NTrays=number of trays trays.
	44	*
	45	---------------------------------------------------------------------#
	46	Model Section_Column
	47	PARAMETERS
	48	ext PP as CalcObject;
	49	ext NComp as Integer;
	50	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	51	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	52	top as Integer(Brief="Number of top tray");
	53	bot as Integer(Brief="Number of bottom tray");
	54
	55	SET
	56	top = (NTrays-1)*(1-topdown)/2+1;
	57	bot = NTrays/top;
[1]	58
	59	VARIABLES
	60	trays(NTrays) as tray;
	61
	62	EQUATIONS
	63	"Pressure Drop through the tray"
[6]	64	trays([top:topdown:bot]).OutletV.F = (1 + tanh(1 *
	65	(trays([top:topdown:bot]).OutletV.P -
[37]	66	trays([top:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	67	trays([top:topdown:bot]).Ah/trays([top:topdown:bot]).vV *
	68	sqrt(2*(trays([top:topdown:bot]).OutletV.P -
	69	trays([top:topdown:bot]).InletL.P + 1e-8 * "atm") /
	70	(trays([top:topdown:bot]).alfa*trays([top:topdown:bot]).rhoV));
	71
[1]	72	CONNECTIONS
[6]	73	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	74	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	75	end
	76
	77
	78	#*----------------------------------------------------------------------
	79	* Model of a distillation column containing:
	80	* - NTrays like tray;
	81	* - a kettle reboiler;
	82	* - dymamic condenser;
	83	* - a splitter which separate reflux and distillate;
	84	* - a pump in reflux stream;
	85	---------------------------------------------------------------------#
	86	Model Distillation_kettle_cond
	87	PARAMETERS
	88	ext PP as CalcObject;
	89	ext NComp as Integer;
	90	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	91	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	92	top as Integer(Brief="Number of top tray");
	93	bot as Integer(Brief="Number of bottom tray");
	94
	95	SET
	96	top = (NTrays-1)*(1-topdown)/2+1;
	97	bot = NTrays/top;
[1]	98
	99	VARIABLES
	100	trays(NTrays) as tray;
	101	cond as condenser;
	102	reb as reboiler;
[6]	103	sptop as splitter;
[1]	104	pump1 as pump;
	105
	106	EQUATIONS
	107	if (reb.OutletV.P > reb.InletL.P) then
[6]	108	"Pressure Drop through the reboiler"
	109	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
	110	/ (trays(bot).beta*reb.rhoV) );
[1]	111	else
[6]	112	"No flow in reboiler"
[1]	113	reb.OutletV.F = 0.0 * "mol/s";
	114	end
	115
	116	"Pressure Drop through the tray"
[37]	117	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - cond.OutletL.P)/"Pa"))/2 *
[6]	118	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	119	cond.OutletL.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	120
[6]	121	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	122	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	123	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	124	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	125	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	126	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	127	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
	128
[1]	129	CONNECTIONS
	130	#vapor
[6]	131	reb.OutletV to trays(bot).InletV;
	132	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	133	trays(top).OutletV to cond.InletV;
	134
[1]	135	#liquid
[6]	136	cond.OutletL to sptop.Inlet;
	137	sptop.Outlet2 to pump1.Inlet;
	138	pump1.Outlet to trays(top).InletL;
	139	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	140	trays(bot).OutletL to reb.InletL;
[1]	141	end
	142
	143
	144	#* -------------------------------------------------------------------
	145	* Distillation Column model with:
	146	*
	147	* - NTrays like tray;
	148	* - a vessel in the bottom of column;
	149	* - a splitter who separate the bottom product and the stream to reboiler;
	150	* - steady state reboiler (thermosyphon);
	151	* - a steady state condenser with subcooling;
	152	* - a vessel drum (layed cilinder);
	153	* - a splitter which separate reflux and distillate;
	154	* - a pump in reflux stream.
	155	*
	156	* ------------------------------------------------------------------*#
	157	Model Distillation_thermosyphon_subcooling
	158	PARAMETERS
	159	ext PP as CalcObject;
	160	ext NComp as Integer;
	161	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	162	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	163	top as Integer(Brief="Number of top tray");
	164	bot as Integer(Brief="Number of bottom tray");
	165
	166	SET
	167	top = (NTrays-1)*(1-topdown)/2+1;
	168	bot = NTrays/top;
[1]	169
	170	VARIABLES
	171	trays(NTrays) as tray;
	172	cond as condenserSteady;
	173	reb as reboilerSteady;
	174	tbottom as tank;
	175	ttop as tank_cylindrical;
	176	spbottom as splitter;
	177	sptop as splitter;
	178	pump1 as pump;
	179
	180	EQUATIONS
[102]	181	if (reb.OutletV.P > reb.InletL.P) then
	182	"Pressure Drop through the reboiler"
	183	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
	184	/ (trays(bot).alfa*reb.rhoV) );
	185	else
	186	"No flow in reboiler"
	187	reb.OutletV.F = 0.0 * "mol/s";
	188	end
	189
[1]	190	"Pressure Drop through the tray"
[37]	191	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - ttop.Outlet.P)/"Pa"))/2 *
[46]	192	trays(top).Ah/trays(top).vV /2* sqrt(2*(trays(top).OutletV.P -
[6]	193	ttop.Outlet.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	194
[6]	195	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	196	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	197	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[46]	198	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV /2*
[6]	199	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	200	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	201	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	202
	203	CONNECTIONS
	204	#vapor
[6]	205	reb.OutletV to trays(bot).InletV;
	206	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	207	trays(top).OutletV to cond.InletV;
[1]	208
	209	#liquid
[6]	210	cond.OutletL to ttop.Inlet;
	211	ttop.Outlet to sptop.Inlet;
	212	sptop.Outlet2 to pump1.Inlet;
	213	pump1.Outlet to trays(top).InletL;
	214	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	215	trays(bot).OutletL to tbottom.Inlet;
[1]	216	tbottom.Outlet to spbottom.Inlet;
	217	spbottom.Outlet2 to reb.InletL;
	218	end
	219
	220
	221	#* -------------------------------------------------------------------
	222	* Distillation Column model with:
	223	*
	224	* - NTrays like tray;
	225	* - a vessel in the bottom of column;
	226	* - a splitter who separate the bottom product and the stream to reboiler;
	227	* - steady state reboiler (thermosyphon);
	228	* - a dynamic condenser without subcooling;
	229	* - a splitter which separate reflux and distillate;
	230	* - a pump in reflux stream.
	231	*
	232	* ------------------------------------------------------------------*#
	233	Model Distillation_thermosyphon_cond
	234	PARAMETERS
	235	ext PP as CalcObject;
	236	ext NComp as Integer;
	237	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	238	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	239	top as Integer(Brief="Number of top tray");
	240	bot as Integer(Brief="Number of bottom tray");
	241
	242	SET
	243	top = (NTrays-1)*(1-topdown)/2+1;
	244	bot = NTrays/top;
[1]	245
	246	VARIABLES
	247	trays(NTrays) as tray;
	248	cond as condenser;
	249	reb as reboilerSteady;
	250	tbottom as tank;
	251	spbottom as splitter;
	252	sptop as splitter;
	253	pump1 as pump;
	254
	255	EQUATIONS
	256	if (reb.OutletV.P > reb.InletL.P) then
[6]	257	"Pressure Drop through the reboiler"
	258	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
[99]	259	/ (trays(bot).alfa*reb.rhoV) );
[1]	260	else
[6]	261	"No flow in reboiler"
[1]	262	reb.OutletV.F = 0.0 * "mol/s";
	263	end
	264
	265	"Pressure Drop through the tray"
[37]	266	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - cond.OutletL.P)/"Pa"))/2 *
[6]	267	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	268	cond.OutletL.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	269
[6]	270	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	271	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	272	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	273	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	274	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	275	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	276	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	277
	278	CONNECTIONS
	279	#vapor
[6]	280	reb.OutletV to trays(bot).InletV;
	281	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	282	trays(top).OutletV to cond.InletV;
[1]	283
	284	#liquid
	285	cond.OutletL to sptop.Inlet;
	286	sptop.Outlet2 to pump1.Inlet;
[6]	287	pump1.Outlet to trays(top).InletL;
	288	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	289	trays(bot).OutletL to tbottom.Inlet;
[1]	290	tbottom.Outlet to spbottom.Inlet;
	291	spbottom.Outlet2 to reb.InletL;
	292	end
	293
	294	#* -------------------------------------------------------------------
	295	* Distillation Column model with:
	296	*
	297	* - NTrays like tray;
	298	* - a kettle reboiler;
	299	* - a steady state condenser with subcooling;
	300	* - a vessel drum (layed cilinder);
	301	* - a splitter which separate reflux and distillate;
	302	* - a pump in reflux stream.
	303	*
	304	* ------------------------------------------------------------------*#
	305	Model Distillation_kettle_subcooling
	306	PARAMETERS
	307	ext PP as CalcObject;
	308	ext NComp as Integer;
	309	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	310	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	311	top as Integer(Brief="Number of top tray");
	312	bot as Integer(Brief="Number of bottom tray");
	313
	314	SET
	315	top = (NTrays-1)*(1-topdown)/2+1;
	316	bot = NTrays/top;
[1]	317
	318	VARIABLES
	319	trays(NTrays) as tray;
	320	cond as condenserSteady;
	321	reb as reboiler;
	322	ttop as tank_cylindrical;
	323	sptop as splitter;
	324	pump1 as pump;
	325
	326	EQUATIONS
	327	if (reb.OutletV.P > reb.InletL.P) then
[6]	328	"Pressure Drop through the reboiler"
	329	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
	330	/ (trays(bot).beta*reb.rhoV) );
[1]	331	else
[6]	332	"No flow in reboiler"
[1]	333	reb.OutletV.F = 0.0 * "mol/s";
	334	end
	335
	336	"Pressure Drop through the tray"
[37]	337	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - ttop.Outlet.P)/"Pa"))/2 *
[6]	338	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	339	ttop.Outlet.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	340
[6]	341	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	342	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	343	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	344	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	345	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	346	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	347	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	348
	349	CONNECTIONS
	350	#vapor
[6]	351	reb.OutletV to trays(bot).InletV;
	352	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	353	trays(top).OutletV to cond.InletV;
[1]	354
	355	#liquid
[6]	356	cond.OutletL to ttop.Inlet;
	357	ttop.Outlet to sptop.Inlet;
	358	sptop.Outlet2 to pump1.Inlet;
	359	pump1.Outlet to trays(top).InletL;
	360	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	361	trays(bot).OutletL to reb.InletL;
[1]	362	end
	363
	364
	365	#*----------------------------------------------------------------------
	366	* Model of a rectifier containing:
	367	* - NTrays like tray;
	368	* - dymamic condenser without subcooling;
	369	* - a splitter which separate reflux and distillate;
	370	* - a pump in reflux stream;
	371	---------------------------------------------------------------------#
	372	Model Rectifier
	373	PARAMETERS
	374	ext PP as CalcObject;
	375	ext NComp as Integer;
	376	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	377	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	378	top as Integer(Brief="Number of top tray");
	379	bot as Integer(Brief="Number of bottom tray");
	380
	381	SET
	382	top = (NTrays-1)*(1-topdown)/2+1;
	383	bot = NTrays/top;
[1]	384
	385	VARIABLES
	386	trays(NTrays) as tray;
	387	cond as condenser;
[6]	388	sptop as splitter;
[1]	389	pump1 as pump;
	390
	391	EQUATIONS
	392	"Pressure Drop through the tray"
[37]	393	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - cond.OutletL.P)/"Pa"))/2 *
[6]	394	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	395	cond.OutletL.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	396
[6]	397	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	398	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	399	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	400	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	401	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	402	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	403	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	404
	405	CONNECTIONS
	406	#vapor
[6]	407	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	408	trays(top).OutletV to cond.InletV;
	409
[1]	410	#liquid
[6]	411	cond.OutletL to sptop.Inlet;
	412	sptop.Outlet2 to pump1.Inlet;
	413	pump1.Outlet to trays(top).InletL;
	414	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	415	end
	416
	417
	418	#* -------------------------------------------------------------------
	419	* Rectifier Column with:
	420	*
	421	* - NTrays like tray;
	422	* - a steady state condenser with subcooling;
	423	* - a vessel drum (layed cilinder);
	424	* - a splitter which separate reflux and distillate;
	425	* - a pump in reflux stream.
	426	*
	427	* ------------------------------------------------------------------*#
	428	Model Rectifier_subcooling
	429	PARAMETERS
	430	ext PP as CalcObject;
	431	ext NComp as Integer;
	432	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	433	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	434	top as Integer(Brief="Number of top tray");
	435	bot as Integer(Brief="Number of bottom tray");
	436
	437	SET
	438	top = (NTrays-1)*(1-topdown)/2+1;
	439	bot = NTrays/top;
[1]	440
	441	VARIABLES
	442	trays(NTrays) as tray;
	443	cond as condenserSteady;
	444	ttop as tank_cylindrical;
	445	sptop as splitter;
	446	pump1 as pump;
	447
	448	EQUATIONS
	449	"Pressure Drop through the tray"
[37]	450	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - ttop.Outlet.P)/"Pa"))/2 *
[6]	451	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	452	ttop.Outlet.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	453
[6]	454	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	455	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	456	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	457	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	458	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	459	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	460	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	461
	462	CONNECTIONS
	463	#vapor
[6]	464	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	465	trays(top).OutletV to cond.InletV;
[1]	466
	467	#liquid
[6]	468	cond.OutletL to ttop.Inlet;
	469	ttop.Outlet to sptop.Inlet;
	470	sptop.Outlet2 to pump1.Inlet;
	471	pump1.Outlet to trays(top).InletL;
	472	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	473	end
	474
	475
	476	#*----------------------------------------------------------------------
	477	* Model of a Refluxed Stripping column containing:
	478	* - NTrays like tray;
	479	* - dymamic condenser without subcooling;
	480	* - a splitter which separate reflux and distillate;
	481	* - a pump in reflux stream;
	482	---------------------------------------------------------------------#
	483	Model Refluxed_Stripping
	484	PARAMETERS
	485	ext PP as CalcObject;
	486	ext NComp as Integer;
	487	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	488	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	489	top as Integer(Brief="Number of top tray");
	490	bot as Integer(Brief="Number of bottom tray");
	491
	492	SET
	493	top = (NTrays-1)*(1-topdown)/2+1;
	494	bot = NTrays/top;
[1]	495
	496	VARIABLES
	497	trays(NTrays) as tray;
	498	cond as condenser;
[6]	499	sptop as splitter;
[1]	500	pump1 as pump;
	501
	502	EQUATIONS
	503	"Pressure Drop through the tray"
[37]	504	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - cond.OutletL.P)/"Pa"))/2 *
[6]	505	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	506	cond.OutletL.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	507
[6]	508	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	509	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	510	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	511	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	512	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	513	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	514	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	515
	516	CONNECTIONS
	517	#vapor
[6]	518	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	519	trays(top).OutletV to cond.InletV;
	520
[1]	521	#liquid
[6]	522	cond.OutletL to sptop.Inlet;
	523	sptop.Outlet2 to pump1.Inlet;
	524	pump1.Outlet to trays(top).InletL;
	525	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	526	end
	527
	528
	529	#* -------------------------------------------------------------------
	530	* Refluxed Stripping Column with:
	531	*
	532	* - NTrays like tray;
	533	* - a steady state condenser (with subcooling);
	534	* - a vessel drum (layed cilinder);
	535	* - a splitter which separate reflux and distillate;
	536	* - a pump in reflux stream.
	537	*
	538	* ------------------------------------------------------------------*#
	539	Model Refluxed_Stripping_subcooling
	540	PARAMETERS
	541	ext PP as CalcObject;
	542	ext NComp as Integer;
	543	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	544	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	545	top as Integer(Brief="Number of top tray");
	546	bot as Integer(Brief="Number of bottom tray");
	547
	548	SET
	549	top = (NTrays-1)*(1-topdown)/2+1;
	550	bot = NTrays/top;
[1]	551
	552	VARIABLES
	553	trays(NTrays) as tray;
	554	cond as condenserSteady;
	555	ttop as tank_cylindrical;
	556	sptop as splitter;
	557	pump1 as pump;
	558
	559	EQUATIONS
	560	"Pressure Drop through the tray"
[37]	561	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - ttop.Outlet.P)/"Pa"))/2 *
[6]	562	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	563	ttop.Outlet.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	564
[6]	565	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	566	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	567	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	568	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	569	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	570	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	571	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	572
	573	CONNECTIONS
	574	#vapor
[6]	575	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	576	trays(top).OutletV to cond.InletV;
[1]	577
	578	#liquid
[6]	579	cond.OutletL to ttop.Inlet;
	580	ttop.Outlet to sptop.Inlet;
	581	sptop.Outlet2 to pump1.Inlet;
	582	pump1.Outlet to trays(top).InletL;
	583	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	584	end
	585
	586
	587	#*----------------------------------------------------------------------
	588	* Model of a Refluxed Absorption column containing:
	589	* - NTrays like tray;
	590	* - dymamic condenser without subcooling;
	591	* - a splitter which separate reflux and distillate;
	592	* - a pump in reflux stream;
	593	---------------------------------------------------------------------#
	594	Model Refluxed_Absorption
	595	PARAMETERS
	596	ext PP as CalcObject;
	597	ext NComp as Integer;
	598	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	599	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	600	top as Integer(Brief="Number of top tray");
	601	bot as Integer(Brief="Number of bottom tray");
	602
	603	SET
	604	top = (NTrays-1)*(1-topdown)/2+1;
	605	bot = NTrays/top;
[1]	606
	607	VARIABLES
	608	trays(NTrays) as tray;
	609	cond as condenser;
[6]	610	sptop as splitter;
[1]	611	pump1 as pump;
	612
	613	EQUATIONS
	614	"Pressure Drop through the tray"
[37]	615	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - cond.OutletL.P)/"Pa"))/2 *
[6]	616	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	617	cond.OutletL.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	618
[6]	619	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	620	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	621	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	622	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	623	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	624	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	625	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	626
	627	CONNECTIONS
	628	#vapor
[6]	629	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	630	trays(top).OutletV to cond.InletV;
	631
[1]	632	#liquid
[6]	633	cond.OutletL to cond.InletV;
	634	cond.OutletL to sptop.Inlet;
	635	sptop.Outlet2 to pump1.Inlet;
	636	pump1.Outlet to trays(top).InletL;
	637	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	638	end
	639
	640
	641	#* -------------------------------------------------------------------
	642	* Refluxed Absorption Column with:
	643	*
	644	* - NTrays like tray;
	645	* - a steady state condenser (with subcooling);
	646	* - a vessel drum (layed cilinder);
	647	* - a splitter which separate reflux and distillate;
	648	* - a pump in reflux stream.
	649	*
	650	* ------------------------------------------------------------------*#
	651	Model Refluxed_Absorption_subcooling
	652	PARAMETERS
	653	ext PP as CalcObject;
	654	ext NComp as Integer;
	655	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	656	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	657	top as Integer(Brief="Number of top tray");
	658	bot as Integer(Brief="Number of bottom tray");
	659
	660	SET
	661	top = (NTrays-1)*(1-topdown)/2+1;
	662	bot = NTrays/top;
[1]	663
	664	VARIABLES
	665	trays(NTrays) as tray;
	666	cond as condenserSteady;
	667	ttop as tank_cylindrical;
	668	sptop as splitter;
	669	pump1 as pump;
	670
	671	EQUATIONS
	672	"Pressure Drop through the tray"
[37]	673	trays(top).OutletV.F = (1 + tanh(1 * (trays(top).OutletV.P - ttop.Outlet.P)/"Pa"))/2 *
[6]	674	trays(top).Ah/trays(top).vV * sqrt(2*(trays(top).OutletV.P -
	675	ttop.Outlet.P + 1e-8 * "atm") / (trays(top).alfa*trays(top).rhoV));
[1]	676
[6]	677	trays([top+topdown:topdown:bot]).OutletV.F = (1 + tanh(1 *
	678	(trays([top+topdown:topdown:bot]).OutletV.P -
[37]	679	trays([top+topdown:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	680	trays([top+topdown:topdown:bot]).Ah/trays([top+topdown:topdown:bot]).vV *
	681	sqrt(2*(trays([top+topdown:topdown:bot]).OutletV.P -
	682	trays([top+topdown:topdown:bot]).InletL.P + 1e-8 * "atm") /
	683	(trays([top+topdown:topdown:bot]).alfa*trays([top+topdown:topdown:bot]).rhoV));
[1]	684
	685	CONNECTIONS
	686	#vapor
[6]	687	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
	688	trays(top).OutletV to cond.InletV;
[1]	689
	690	#liquid
[6]	691	cond.OutletL to ttop.Inlet;
	692	ttop.Outlet to sptop.Inlet;
	693	sptop.Outlet2 to pump1.Inlet;
	694	pump1.Outlet to trays(top).InletL;
	695	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
[1]	696	end
	697
	698
	699	#* -------------------------------------------------------------------
	700	* Reboiled Stripping Column model with:
	701	*
	702	* - NTrays like tray;
	703	* - a kettle reboiler;
	704	*
	705	* ------------------------------------------------------------------*#
	706	Model Reboiled_Stripping_kettle
	707	PARAMETERS
	708	ext PP as CalcObject;
	709	ext NComp as Integer;
	710	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	711	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	712	top as Integer(Brief="Number of top tray");
	713	bot as Integer(Brief="Number of bottom tray");
	714
	715	SET
	716	top = (NTrays-1)*(1-topdown)/2+1;
	717	bot = NTrays/top;
[1]	718
	719	VARIABLES
	720	trays(NTrays) as tray;
	721	reb as reboiler;
	722
	723	EQUATIONS
	724	if (reb.OutletV.P > reb.InletL.P) then
	725	"Pressure Drop through the tray"
[6]	726	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
	727	/ (trays(bot).beta*reb.rhoV) );
[1]	728	else
	729	"Prato selado"
	730	reb.OutletV.F = 0.0 * "mol/s";
	731	end
	732
	733	"Pressure Drop through the tray"
[6]	734	trays([top:topdown:bot]).OutletV.F = (1 + tanh(1 *
	735	(trays([top:topdown:bot]).OutletV.P -
[37]	736	trays([top:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	737	trays([top:topdown:bot]).Ah/trays([top:topdown:bot]).vV *
	738	sqrt(2*(trays([top:topdown:bot]).OutletV.P -
	739	trays([top:topdown:bot]).InletL.P + 1e-8 * "atm") /
	740	(trays([top:topdown:bot]).alfa*trays([top:topdown:bot]).rhoV));
[1]	741
	742	CONNECTIONS
	743	#vapor
[6]	744	reb.OutletV to trays(bot).InletV;
	745	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
[1]	746
	747	#liquid
[6]	748	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	749	trays(bot).OutletL to reb.InletL;
[1]	750	end
	751
	752
	753	#* -------------------------------------------------------------------
	754	* Reboiled Stripping Column model with:
	755	*
	756	* - NTrays like tray;
	757	* - a vessel in the bottom of column;
	758	* - a splitter which separate the bottom product and the stream to reboiler;
	759	* - steady state reboiler (thermosyphon);
	760	*
	761	* ------------------------------------------------------------------*#
	762	Model Reboiled_Stripping_thermosyphon
	763	PARAMETERS
	764	ext PP as CalcObject;
	765	ext NComp as Integer;
	766	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	767	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	768	top as Integer(Brief="Number of top tray");
	769	bot as Integer(Brief="Number of bottom tray");
	770
	771	SET
	772	top = (NTrays-1)*(1-topdown)/2+1;
	773	bot = NTrays/top;
[1]	774
	775	VARIABLES
	776	trays(NTrays) as tray;
	777	reb as reboilerSteady;
	778	spbottom as splitter;
	779	tbottom as tank;
	780
	781	EQUATIONS
	782	if (reb.OutletV.P > reb.InletL.P) then
	783	"Pressure Drop through the tray"
[6]	784	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
[99]	785	/ (trays(bot).alfa*reb.rhoV) );
[1]	786	else
	787	"Prato selado"
	788	reb.OutletV.F = 0.0 * "mol/s";
	789	end
	790
	791	"Pressure Drop through the tray"
[6]	792	trays([top:topdown:bot]).OutletV.F = (1 + tanh(1 *
	793	(trays([top:topdown:bot]).OutletV.P -
[37]	794	trays([top:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	795	trays([top:topdown:bot]).Ah/trays([top:topdown:bot]).vV *
	796	sqrt(2*(trays([top:topdown:bot]).OutletV.P -
	797	trays([top:topdown:bot]).InletL.P + 1e-8 * "atm") /
	798	(trays([top:topdown:bot]).alfa*trays([top:topdown:bot]).rhoV));
[1]	799
	800	CONNECTIONS
	801	#vapor
[6]	802	reb.OutletV to trays(bot).InletV;
	803	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
[1]	804
	805	#liquid
[6]	806	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	807	trays(bot).OutletL to tbottom.Inlet;
[1]	808	tbottom.Outlet to spbottom.Inlet;
	809	spbottom.Outlet2 to reb.InletL;
	810	end
	811
	812
	813	#* -------------------------------------------------------------------
	814	* Reboiled Absorption Column model with:
	815	*
	816	* - NTrays like tray;
	817	* - a kettle reboiler;
	818	*
	819	* ------------------------------------------------------------------*#
	820	Model Reboiled_Absorption_kettle
	821	PARAMETERS
	822	ext PP as CalcObject;
	823	ext NComp as Integer;
	824	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	825	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	826	top as Integer(Brief="Number of top tray");
	827	bot as Integer(Brief="Number of bottom tray");
	828
	829	SET
	830	top = (NTrays-1)*(1-topdown)/2+1;
	831	bot = NTrays/top;
[1]	832
	833	VARIABLES
	834	trays(NTrays) as tray;
	835	reb as reboiler;
	836
	837	EQUATIONS
	838	if (reb.OutletV.P > reb.InletL.P) then
	839	"Pressure Drop through the tray"
[6]	840	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
[37]	841	/ (trays(bot).beta*reb.rhoV) );
[1]	842	else
	843	"Prato selado"
	844	reb.OutletV.F = 0.0 * "mol/s";
	845	end
	846
	847	"Pressure Drop through the tray"
[6]	848	trays([top:topdown:bot]).OutletV.F = (1 + tanh(1 *
	849	(trays([top:topdown:bot]).OutletV.P -
[37]	850	trays([top:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	851	trays([top:topdown:bot]).Ah/trays([top:topdown:bot]).vV *
	852	sqrt(2*(trays([top:topdown:bot]).OutletV.P -
	853	trays([top:topdown:bot]).InletL.P + 1e-8 * "atm") /
	854	(trays([top:topdown:bot]).alfa*trays([top:topdown:bot]).rhoV));
[1]	855
	856	CONNECTIONS
	857	#vapor
[6]	858	reb.OutletV to trays(bot).InletV;
	859	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
[1]	860
	861	#liquid
[6]	862	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	863	trays(bot).OutletL to reb.InletL;
[1]	864	end
	865
	866
	867	#* -------------------------------------------------------------------
	868	* Reboiled Absorption Column model with:
	869	*
	870	* - NTrays like tray;
	871	* - a vessel in the bottom of column;
	872	* - a splitter which separate the bottom product and the stream to reboiler;
	873	* - steady state reboiler (thermosyphon);
	874	*
	875	* ------------------------------------------------------------------*#
	876	Model Reboiled_Absorption_thermosyphon
	877	PARAMETERS
	878	ext PP as CalcObject;
	879	ext NComp as Integer;
	880	NTrays as Integer(Brief="Number of trays", Default=2);
[6]	881	topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
	882	top as Integer(Brief="Number of top tray");
	883	bot as Integer(Brief="Number of bottom tray");
	884
	885	SET
	886	top = (NTrays-1)*(1-topdown)/2+1;
	887	bot = NTrays/top;
[1]	888
	889	VARIABLES
	890	trays(NTrays) as tray;
	891	reb as reboilerSteady;
	892	spbottom as splitter;
	893	tbottom as tank;
	894
	895	EQUATIONS
	896	if (reb.OutletV.P > reb.InletL.P) then
	897	"Pressure Drop through the tray"
[6]	898	reb.OutletV.F = trays(bot).Ah/reb.vV * sqrt((reb.OutletV.P - trays(bot).OutletL.P)
[99]	899	/ (trays(bot).alfa*reb.rhoV) );
[1]	900	else
	901	"Prato selado"
	902	reb.OutletV.F = 0.0 * "mol/s";
	903	end
	904
	905	"Pressure Drop through the tray"
[6]	906	trays([top:topdown:bot]).OutletV.F = (1 + tanh(1 *
	907	(trays([top:topdown:bot]).OutletV.P -
[37]	908	trays([top:topdown:bot]).InletL.P)/"Pa"))/2 *
[6]	909	trays([top:topdown:bot]).Ah/trays([top:topdown:bot]).vV *
	910	sqrt(2*(trays([top:topdown:bot]).OutletV.P -
	911	trays([top:topdown:bot]).InletL.P + 1e-8 * "atm") /
	912	(trays([top:topdown:bot]).alfa*trays([top:topdown:bot]).rhoV));
[1]	913
	914	CONNECTIONS
	915	#vapor
[6]	916	reb.OutletV to trays(bot).InletV;
	917	trays([top+topdown:topdown:bot]).OutletV to trays([top:topdown:bot-topdown]).InletV;
[1]	918
	919	#liquid
[6]	920	trays([top:topdown:bot-topdown]).OutletL to trays([top+topdown:topdown:bot]).InletL;
	921	trays(bot).OutletL to tbottom.Inlet;
[1]	922	tbottom.Outlet to spbottom.Inlet;
	923	spbottom.Outlet2 to reb.InletL;
	924	end
[38]	925
[72]	926	#* -------------------------------------------------------------------
	927	* Reactive Distillation Column
	928	*
	929	* ------------------------------------------------------------------*#
[38]	930	Model ReactiveDistillation
	931	PARAMETERS
	932	ext PP as CalcObject;
	933	ext NComp as Integer;
	934	NTrays as Integer(Brief="Number of trays", Default=2);
	935
	936	VARIABLES
	937	trays(NTrays) as trayReact;
	938	cond as condenserReact;
	939	reb as reboilerReact;
	940	sp as splitter;
	941	p as pump;
	942
	943	EQUATIONS
	944	if ( reb.OutletV.P > 1 * "atm" ) then
	945	"Pressure Drop through the tray"
	946	reb.OutletV.F = trays(1).Ah/reb.vV * sqrt((reb.OutletV.P - 1"atm") / (0.15reb.rhoV) );
	947	else
	948	"Prato selado"
	949	reb.OutletV.F = 0.0 * "mol/s";
	950	end
	951
	952	CONNECTIONS
	953	#vapor
	954	reb.OutletV to trays([NTrays]).InletV;
	955	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	956	trays(1).OutletV to cond.InletV;
	957
	958	#liquid
	959	cond.OutletL to sp.Inlet;
	960	sp.Outlet2 to p.Inlet;
	961	p.Outlet to trays(1).InletL;
	962	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	963	trays(NTrays).OutletL to reb.InletL;
	964	end

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