trunk/models/column.a4l

REQUIRE "flash.a4l";
(* => flash.a4l, stream_holdup.a4l, thermodynamics.a4l, components.a4l,
 *    phases.a4l, atoms.a4l, measures.a4l, system.a4l, basemodel.a4l *)
PROVIDE "column.a4l";

(*
 *  column.a4l
 *  by Ben Allan, Art Westerberg, and Jennifer Perry
 *  Part of the ASCEND Library
 *  $Date: 1998/06/17 18:50:36 $
 *  $Revision: 1.5 $
 *  $Author: mthomas $
 *  $Source: /afs/cs.cmu.edu/project/ascend/Repository/models/column.a4l,v $
 *
 *  This file is part of the ASCEND Modeling Library.
 *  It defines basic tray-by-tray steady-state distillation models.
 *
 *  Copyright (C) 1997,1998 Carnegie Mellon University
 *
 *  The ASCEND Modeling Library is free software; you can redistribute
 *  it and/or modify it under the terms of the GNU General Public
 *  License as published by the Free Software Foundation; either
 *  version 2 of the License, or (at your option) any later version.
 *
 *  The ASCEND Modeling Library is distributed in hope that it
 *  will be useful, but WITHOUT ANY WARRANTY; without even the implied
 *  warranty of MERCHANTABILITY or FITNESS FOR A PARTICULAR PURPOSE.
 *  See the GNU General Public License for more details.
 *
 *  You should have received a copy of the GNU General Public License
 *  along with the program; if not, write to the Free Software
 *  Foundation, Inc., 675 Mass Ave, Cambridge, MA 02139 USA.  Check
 *  the file named COPYING.
 *)

MODEL colmodel() REFINES cmumodel();
	boundwidth IS_A bound_width;
END colmodel;

MODEL tray_stack(
	n_trays WILL_BE integer_constant;
	vapout WILL_BE stream;
	liqin WILL_BE stream;
	vapin WILL_BE stream;
	liqout WILL_BE stream;
	reduce WILL_BE fraction;
	equilibrated WILL_BE boolean;
) WHERE (
	n_trays > 1;
	vapout, liqin, vapin, liqout WILL_NOT_BE_THE_SAME;
	vapout.cd, vapin.cd, liqout.cd, liqin.cd WILL_BE_THE_SAME;
	vapout.pd, vapin.pd WILL_BE_THE_SAME;
	liqout.pd, liqin.pd WILL_BE_THE_SAME;
	liqout.pd.phase_indicator == 'L';
	vapin.pd.phase_indicator == 'V';
	liqin.pd.phase_indicator == 'L';
	vapout.pd.phase_indicator == 'V';
) REFINES colmodel();

NOTES 'ascii-picture'
SELF {
vapout ^ |
       | v liqin
      +---+
      |_1_|
      |___| n_trays (at least 2)
      |___|
      |_n_|
 vapin ^ |
       | v liqout
}
'usage'
equilibrated {
When TRUE, enforces equilbrium between phases on all the trays.
When FALSE, uses constant alpha between phases on all the trays.
}
reduce {
Homotopy parameter used by reduce_Q to move fixed errors in the
energy balances (Qin per tray) toward 0.
}
'contra-indications' SELF {
For a n==1 tray stack, use a "tray" MODEL from the flash library.
}
END NOTES;

	cd ALIASES liqout.cd;
	pdL ALIASES liqout.pd;
	pdV ALIASES vapout.pd;
	vap_option ALIASES pdV.vapor_option;
	liq_option ALIASES pdL.liquid1_option;
	pdVL IS_A phases_data('VL', vap_option, liq_option, 'none');

	(*
	 * The ALIASES/IS_A break if the liqout,vapout are on the same tray.
	 *)

	Tray_set IS_A set OF integer_constant;
	Tray_set :== [1..n_trays];

	components ALIASES cd.components;
	phases ALIASES pdVL.phases;

	(* there are alternative ways of building repeated structures.
	 * This is the first one I came up with. It may not be the best.
	 * BAA.
	 *)

	(* build the internal phase mixing rules, and interior stream
	 * states, and interior streams.
	 *)
	internal_liquid_mixture[1..n_trays-1]
		IS_A select_mixture_type(cd, liq_option);
	FOR k IN [1..n_trays-1] CREATE
		internal_liquid_phase[k]['liquid1'] ALIASES
			internal_liquid_mixture[k].phase;
	END FOR;
	FOR k IN [1..n_trays-1] CREATE
		internal_liquid_state[k] IS_A
		thermodynamics(cd, pdL, internal_liquid_phase[k], equilibrated);
	END FOR;
	FOR k IN [1..n_trays-1] CREATE
		internal_liquid_stream[k] IS_A
		detailed_stream(internal_liquid_state[k]);
	END FOR;
	internal_vapor_mixture[2..n_trays]
		IS_A select_mixture_type(cd, vap_option);
	FOR k IN [2..n_trays] CREATE
		internal_vapor_phase[k]['vapor'] ALIASES
			internal_vapor_mixture[k].phase;
	END FOR;
	FOR k IN [2..n_trays] CREATE
		internal_vapor_state[k] IS_A
		thermodynamics(cd, pdV, internal_vapor_phase[k], equilibrated);
	END FOR;
	FOR k IN [2..n_trays] CREATE
		internal_vapor_stream[k] IS_A
		detailed_stream(internal_vapor_state[k]);
	END FOR;

	(* build tray VLE objects *)

	(* assemble into intermediate, easily accessed arrays *)
	tray_liquid_mixture[tlTrays] ALIASES
		(internal_liquid_mixture[1..n_trays-1].phase,
		liqout.smt['liquid1'].phase)
		WHERE tlTrays IS_A set OF integer_constant
		WITH_VALUE (1..n_trays);
	tray_vapor_mixture[tvTrays] ALIASES
		(vapout.smt['vapor'].phase,
		internal_vapor_mixture[2..n_trays].phase)
		WHERE tvTrays IS_A set OF integer_constant
		WITH_VALUE (1..n_trays);
	(* assemble into little pairs for building VLE states *)
	FOR k IN [Tray_set] CREATE
		trayVL[k][VLphases[k]] ALIASES
		(tray_vapor_mixture[k],tray_liquid_mixture[k])
		WHERE VLphases[k] IS_A set OF symbol_constant
		WITH_VALUE ('vapor','liquid1');
	END FOR;
	(* compile vle of each tray *)
	FOR k IN [1..n_trays] CREATE
		tray_state[k] IS_A
			thermodynamics(cd, pdVL, trayVL[k], equilibrated);
	END FOR;
	(* setup
	 * tray_liqin[1..n_trays+1], tray_vapin[0..n_trays],
	 * input streams.
	 *)
	tray_vapin[tV] ALIASES (vapout.Details,
		internal_vapor_stream[2..n_trays], vapin.Details)
		WHERE tV IS_A set OF integer_constant
		WITH_VALUE (0..n_trays);

	tray_liqin[tL] ALIASES (liqin.Details,
		internal_liquid_stream[1..n_trays-1], liqout.Details)
		WHERE tL IS_A set OF integer_constant
		WITH_VALUE (1..n_trays+1);

	Qin[Tray_set] IS_A energy_rate;

	FOR k IN Tray_set CREATE
		Stack[k] IS_A detailed_tray(
			Qin[k],
			equilibrated,
			tray_liqin[k],
			tray_vapin[k],
			tray_liqin[k+1],
			tray_vapin[k-1],
			tray_state[k]
		);
	END FOR;

	FOR k IN Tray_set CREATE
		P[k] ALIASES tray_state[k].P;
		T[k] ALIASES tray_state[k].T;
	END FOR;

METHODS

METHOD default_all;
	RUN liqin.default_all;
	RUN liqout.default_all;
	RUN vapin.default_all;
	RUN vapout.default_all;
	RUN default_self;
END default_all;

METHOD default_self;
	Qin[Tray_set] := 0{watt};
	boundwidth := 100;
	RUN pdVL.default_self;
	RUN internal_liquid_mixture[1..n_trays-1].default_self;
	RUN internal_vapor_mixture[2..n_trays].default_self;
	RUN internal_liquid_state[1..n_trays-1].default_self;
	RUN internal_vapor_state[2..n_trays].default_self;
	RUN internal_liquid_stream[1..n_trays-1].default_self;
	RUN internal_vapor_stream[2..n_trays].default_self;
	RUN tray_state[Tray_set].default_self;
	Stack[Tray_set].flowscale := 10{mole/second};
	Stack[Tray_set].H_flowscale := 1000{J/second};
END default_self;

METHOD check_all;
	RUN liqin.check_all;
	RUN liqout.check_all;
	RUN vapin.check_all;
	RUN vapout.check_all;
	RUN check_self;
END check_all;

METHOD check_self;
	RUN pdVL.check_self;
	RUN internal_liquid_mixture[1..n_trays-1].check_self;
	RUN internal_vapor_mixture[2..n_trays].check_self;
	RUN internal_liquid_state[1..n_trays-1].check_self;
	RUN internal_vapor_state[2..n_trays].check_self;
	RUN internal_liquid_stream[1..n_trays-1].check_self;
	RUN internal_vapor_stream[2..n_trays].check_self;
	RUN tray_state[Tray_set].check_self;
END check_self;

METHOD scale_all;
	RUN liqin.scale_all;
	RUN liqout.scale_all;
	RUN vapin.scale_all;
	RUN vapout.scale_all;
	RUN scale_self;
END scale_all;

METHOD scale_self;
	(* fortunately no local equations to scale *)
	RUN pdVL.scale_self;
	RUN internal_liquid_mixture[1..n_trays-1].scale_self;
	RUN internal_vapor_mixture[2..n_trays].scale_self;
	RUN internal_liquid_state[1..n_trays-1].scale_self;
	RUN internal_vapor_state[2..n_trays].scale_self;
	RUN internal_liquid_stream[1..n_trays-1].scale_self;
	RUN internal_vapor_stream[2..n_trays].scale_self;
	RUN tray_state[Tray_set].scale_self;
END scale_self;

METHOD bound_all;
	RUN liqin.bound_all;
	RUN liqout.bound_all;
	RUN vapin.bound_all;
	RUN vapout.bound_all;
	RUN bound_self;
END bound_all;

METHOD bound_self;
	(* fortunately no local variables to scale *)
	RUN pdVL.bound_self;

	internal_liquid_mixture[1..n_trays-1].boundwidth := boundwidth;
	internal_vapor_mixture[2..n_trays].boundwidth := boundwidth;
	internal_liquid_state[1..n_trays-1].boundwidth := boundwidth;
	internal_vapor_state[2..n_trays].boundwidth := boundwidth;
	internal_liquid_stream[1..n_trays-1].boundwidth := boundwidth;
	internal_vapor_stream[2..n_trays].boundwidth := boundwidth;
	tray_state[Tray_set].boundwidth := boundwidth;

	RUN internal_liquid_mixture[1..n_trays-1].bound_self;
	RUN internal_vapor_mixture[2..n_trays].bound_self;
	RUN internal_liquid_state[1..n_trays-1].bound_self;
	RUN internal_vapor_state[2..n_trays].bound_self;
	RUN internal_liquid_stream[1..n_trays-1].bound_self;
	RUN internal_vapor_stream[2..n_trays].bound_self;
	RUN tray_state[Tray_set].bound_self;

END bound_self;

METHOD specify;
	RUN seqmod;
	RUN liqin.specify;
	RUN vapin.specify;
END specify;

METHOD seqmod;
	RUN Stack[Tray_set].seqmod;
END seqmod;

METHOD scale;
	RUN Stack[Tray_set].scale;
END scale;

METHOD reset_to_mass_balance;
	equilibrated := FALSE;
	RUN reset;
END reset_to_mass_balance;

METHOD reset_to_full_thermo;
	equilibrated := TRUE;
	RUN reset;
END reset_to_full_thermo;

METHOD reset_to_adiabatic;
	RUN reset_to_full_thermo;
	Stack[Tray_set].cmo_ratio.fixed := FALSE;
	Stack[Tray_set].Qin.fixed := TRUE;
	Stack[Tray_set].Qin := 0{W};
END reset_to_adiabatic;

METHOD reduce_Q;
	FOR j IN [Tray_set] DO
		Stack[j].Qin := reduce * Stack[j].Qin;
	END FOR;
END reduce_Q;

END tray_stack;

MODEL test_tray_stack() REFINES testcmumodel();
	n_trays_below	IS_A integer_constant;
	n_trays_below :== 2;
	equilibrated	IS_A start_false;
	reduce		IS_A fraction;

NOTES
'usage' equilibrated {
This variable and feed.equilibrated may or may not be the same.
Do not assume they are when writing methods.
}
reduce {
This is a fraction from 0 to 1. The method reduce_Q uses it
to move the Qin on each stack and feed tray toward 0.
Essentially this is a physical homotopy parameter.
}
END NOTES;


	cd IS_A components_data(['n_pentane','n_hexane','n_heptane'],
				 'n_heptane');
	pdV IS_A phases_data('V', 'Pitzer_vapor_mixture', 'none', 'none');
	pdL IS_A phases_data('L', 'none', 'UNIFAC_liquid_mixture', 'none');

	Vapout		IS_A stream(cd, pdV, equilibrated);
	Liqin		IS_A stream(cd, pdL, equilibrated);
	Vapin		IS_A stream(cd, pdV, equilibrated);
	Liqout		IS_A stream(cd, pdL, equilibrated);

	Section IS_A tray_stack(
		n_trays_below,
		Vapout,
		Liqin,
		Vapin,
		Liqout,
		reduce,
		equilibrated
	);

METHODS

METHOD default_all;
	RUN default_self;
END default_all;
METHOD default_self;
	equilibrated := FALSE;
	RUN Section.default_self;
END default_self;

METHOD check_all;
	RUN check_self;
END check_all;

METHOD check_self;
	RUN Section.check_all;
END check_self;

METHOD bound_all;
	RUN bound_self;
END bound_all;

METHOD bound_self;
	RUN Section.bound_self;
END bound_self;

METHOD scale_all;
	RUN scale_self;
END scale_all;

METHOD scale_self;
	RUN Section.scale_self;
END scale_self;

METHOD specify;
	RUN Section.specify;
END specify;

METHOD reset_to_adiabatic;
	RUN Section.reset_to_adiabatic;
END reset_to_adiabatic;
END test_tray_stack;


MODEL simple_column(
	pdVL		WILL_BE phases_data;
	distillate	WILL_BE stream;
	n_trays_above	WILL_BE integer_constant;
	feed 		WILL_BE stream;
	n_trays_below	WILL_BE integer_constant;
	bottoms		WILL_BE stream;
	equilibrated	WILL_BE boolean;
	reduce		WILL_BE fraction;
) WHERE (
	n_trays_above > 1;
	n_trays_below > 1;
	distillate, bottoms, feed WILL_NOT_BE_THE_SAME;
	feed.cd, distillate.cd, bottoms.cd WILL_BE_THE_SAME;
	pdVL.phase_indicator == 'VL';
	distillate.pd, bottoms.pd WILL_BE_THE_SAME;
	distillate.pd.phase_indicator == 'L';
	pdVL.liquid1_option == distillate.pd.liquid1_option;
	feed.pd.phase_indicator IN ['V','L','VL'] == TRUE;
) REFINES colmodel();

NOTES
'ascii-picture' SELF {
	         ___   total condenser
	        /   \________> distillate liquid
	        |___|
(condenser_vapin)^ |
	         | |
	         | v(rectifier_liqin)
	        +---+
	        |___|
	        |___| n_trays_above (at least 2)
	        |___|
	        |___|
(rectifier_vapin)^ |
	         | |
	         | v(feed_tray_liqin)
	        +---+
 V/L feed ----->|   |
	        +___+
(feed_tray_vapin)^ |
	         | |
	         | v(stripper_liqin)
	        +---+
	        |___|
	        |___| n_trays_below (at least 2)
	        |___|
	        |___|
 (stripper_vapin)^ |
	         | |
	         | v(reboiler_liqin)
	         ___
	        |   |________> bottoms liquid
	        \___/ non-adiabatic flash
}
'usage' equilibrated {
This variable and feed.equilibrated may or may not be the same.
Do not assume they are when writing methods.
}
reduce {
This is a fraction from 0 to 1. The method reduce_Q uses it
to move the Qin on each stack and feed tray toward 0.
Essentially this is a physical homotopy parameter.
}
'changing' SELF {
This MODEL is very large, therefore it is very carefully
structured following the ascii-picture.
It should be relatively easy to modify this MODEL
just by carefully following the patterns we use. The pattern is
that all streams are given names corresponding to their input
roles.

You can build arbitrarily complicated columns with bypasses,
recycles, intercoolers, etc just by copying this MODEL
and rerouting section or tray connections after adding or
removing sections, exchangers, and so forth.
}
END NOTES;

(*
 * The creation steps:
 *	alias the options from the feed stream. (done above).
 *	inter-section streams (single phase)
 *	column sections
 * At the end of the steps, everything has been wired up
 * simply by passing common parts to both places they belong.
 * For clarity, no arrays are used.
 *
 * If you are nuts enough to reimplement this MODEL using
 * arrays, have a look at tray_stack for techniques to avoid
 * sending the compiler to hell.
 *
 * The thermodynamic options of the given pdVL
 * column without using ARE_ALIKE or ARE_THE_SAME.
 *)

	pdL ALIASES bottoms.pd;
	pdV IS_A phases_data('V', pdVL.vapor_option, 'none', 'none');
	cd ALIASES feed.cd;
	components ALIASES feed.components;

	(* inter-section streams *)
	condenser_vapin "vapor rising to condenser",
	rectifier_vapin "vapor rising from feed tray",
	feed_tray_vapin "vapor rising from stripper",
	stripper_vapin "vapor rising from reboiler"
		IS_A stream(cd, pdV, equilibrated);

	rectifier_liqin "reflux condensate",
	feed_tray_liqin "liquid falling from rectifier",
	stripper_liqin "liquid falling from feed tray",
	reboiler_liqin "liquid falling to reboiler"
		IS_A stream(cd, pdL, equilibrated);

	(* typical heat duties *)
	Qin_condenser "condenser duty",
	Qin_feed "feed heater duty",
	Qin_reboiler "reboiler duty" IS_A energy_rate;

	(* column sections *)
	condenser IS_A total_condenser(
		Qin_condenser,
		condenser_vapin,
		rectifier_liqin,
		distillate
	);
	rectifying_section "the trays above the feed" IS_A tray_stack(
		n_trays_above,
		condenser_vapin,
		rectifier_liqin,
		rectifier_vapin,
		feed_tray_liqin,
		reduce,
		equilibrated
	);
	feed_tray IS_A feed_tray(
		Qin_feed,
		equilibrated,
		feed,
		feed_tray_liqin,
		feed_tray_vapin,
		stripper_liqin,
		rectifier_vapin
	);
	stripping_section "the trays below the feed" IS_A tray_stack(
		n_trays_below,
		feed_tray_vapin,
		stripper_liqin,
		stripper_vapin,
		reboiler_liqin,
		reduce,
		equilibrated
	);
	reboiler IS_A simple_reboiler(
		Qin_reboiler,
		equilibrated,
		reboiler_liqin,
		stripper_vapin,
		bottoms
	);

	(* this array has the common type flash_base,
	 * so it is mainly useful for methods.
	 *)
	Tray[zTr] ALIASES (
		condenser,
		rectifying_section.Stack[1..n_trays_above],
		feed_tray,
		stripping_section.Stack[1..n_trays_below],
		reboiler)
	WHERE zTr IS_A set OF integer_constant
	WITH_VALUE (0..N_trays);

	(* useful things to know from an END user perspective *)
	N_trays IS_A integer_constant;
	N_trays :== n_trays_above + 1 + n_trays_below + 1;
	VLE_set IS_A set OF integer_constant;
	VLE_set :== [1 .. N_trays];
	Feed_loc IS_A integer_constant;
	Feed_loc :== n_trays_above +1;

	(* why is this here? total reflux? *)
	omb_slack[components]	IS_A molar_rate;
	FOR i IN components CREATE
	overall_mass_balance[i]:
		feed.f[i] = (distillate.f[i] + bottoms.f[i] + omb_slack[i]);
	END FOR;

METHODS

METHOD default_self;
	omb_slack[components] := 0 {mol/s};
	omb_slack[components].lower_bound := -1000{mole/s};
	RUN condenser.default_self;
	RUN rectifying_section.default_self;
	RUN feed_tray.default_self;
	RUN stripping_section.default_self;
	RUN reboiler.default_self;
END default_self;

METHOD default_all;
	RUN pdVL.default_all;
	RUN distillate.default_all;
	RUN feed.default_all;
	RUN bottoms.default_all;
	RUN default_self;
END default_all;

METHOD check_all;
	RUN check_self;
	RUN pdVL.check_all;
	RUN distillate.check_all;
	RUN feed.check_all;
	RUN bottoms.check_all;
END check_all;

METHOD check_self;
	FOR i IN components DO
		IF ( omb_slack[i]/feed.flow.nominal > 1.0e-4 ) THEN
			STOP {Column violates over-all species balance};
		END IF;
	END FOR;
	RUN pdV.check_self;
	RUN condenser_vapin.check_self;
	RUN rectifier_vapin.check_self;
	RUN feed_tray_vapin.check_self;
	RUN stripper_vapin.check_self;
	RUN rectifier_liqin.check_self;
	RUN feed_tray_liqin.check_self;
	RUN stripper_liqin.check_self;
	RUN reboiler_liqin.check_self;
	RUN condenser.check_self;
	RUN rectifying_section.check_self;
	RUN feed_tray.check_self;
	RUN stripping_section.check_self;
	RUN reboiler.check_self;
END check_self;

METHOD scale_all;
	RUN pdVL.scale_all;
	RUN distillate.scale_all;
	RUN feed.scale_all;
	RUN bottoms.scale_all;
	RUN scale_self;
END scale_all;

METHOD scale_self;
	RUN pdV.scale_self;
	RUN condenser_vapin.scale_self;
	RUN rectifier_vapin.scale_self;
	RUN feed_tray_vapin.scale_self;
	RUN stripper_vapin.scale_self;
	RUN rectifier_liqin.scale_self;
	RUN feed_tray_liqin.scale_self;
	RUN stripper_liqin.scale_self;
	RUN reboiler_liqin.scale_self;
	RUN condenser.scale_self;
	RUN rectifying_section.scale_self;
	RUN feed_tray.scale_self;
	RUN stripping_section.scale_self;
	RUN reboiler.scale_self;
END scale_self;

METHOD bound_all;
	RUN pdVL.bound_all;
	RUN distillate.bound_all;
	RUN feed.bound_all;
	RUN bottoms.bound_all;
	RUN bound_self;
END bound_all;

METHOD bound_self;
	RUN pdV.bound_self;
	RUN condenser_vapin.bound_self;
	RUN rectifier_vapin.bound_self;
	RUN feed_tray_vapin.bound_self;
	RUN stripper_vapin.bound_self;
	RUN rectifier_liqin.bound_self;
	RUN feed_tray_liqin.bound_self;
	RUN stripper_liqin.bound_self;
	RUN reboiler_liqin.bound_self;
	RUN condenser.bound_self;
	RUN rectifying_section.bound_self;
	RUN feed_tray.bound_self;
	RUN stripping_section.bound_self;
	RUN reboiler.bound_self;
END bound_self;

METHOD seqmod;
	RUN condenser.seqmod;
	RUN rectifying_section.seqmod;
	RUN feed_tray.seqmod;
	RUN stripping_section.seqmod;
	RUN reboiler.seqmod;
END seqmod;

METHOD specify;
	RUN seqmod;
	RUN feed.specify;
        IF (feed.equilibrated AND (feed.pd.phase_indicator == 'VL')) THEN
		feed.Details.state.phase[feed.pd.reference_phase].T.fixed := FALSE;
		feed.Details.state.phase_fraction[feed.pd.other_phases].fixed := TRUE;
        END IF;
END specify;

METHOD reset_to_mass_balance;
	equilibrated := FALSE;
	feed.state.equilibrated := FALSE;
	RUN reset;
END reset_to_mass_balance;

METHOD reset_to_full_thermo;
	equilibrated := TRUE;
	feed.state.equilibrated := TRUE;
	RUN reset;
END reset_to_full_thermo;

METHOD reset_to_adiabatic;
	RUN reset_to_full_thermo;
	(* condenser, reboiler Qin left free *)
	rectifying_section.Stack[1..n_trays_above].cmo_ratio.fixed := FALSE;
	stripping_section.Stack[1..n_trays_below].cmo_ratio.fixed := FALSE;
	Tray[1..N_trays-1].Qin.fixed := TRUE;
	Tray[1..N_trays-1].Qin := 0{W};
	feed_tray.q.fixed := FALSE;
END reset_to_adiabatic;

METHOD propagate_feed_values;
	(* propagate feed tray flows and relative volatilities,
	 * after solving the feed tray.
	 *)
	FOR i IN components DO
		(* use feed alpha everywhere *)
		Tray[VLE_set].alpha[i] := feed_tray.alpha[i];
		(* copy feed flow rates to all internal streams *)
		(* This copying should factor in the RR and BR *)
		Tray[0..N_trays-1].liqout.f[i] := feed.f[i];
		Tray[1..N_trays].vapout.f[i] := feed.f[i];
	END FOR;
END propagate_feed_values;

END simple_column;

MODEL simple_column_profiles(
	sc WILL_BE simple_column;
) REFINES colmodel();

	traynum[sc.VLE_set] IS_A integer_constant;
	FOR i IN sc.VLE_set CREATE
		traynum[i] :== i;
	END FOR;

	cmo_ratio[zc] ALIASES (
		sc.rectifying_section.Stack[1..sc.n_trays_above].cmo_ratio,
		sc.stripping_section.Stack[1..sc.n_trays_below].cmo_ratio)
	WHERE zc IS_A set OF integer_constant
	WITH_VALUE (	1 .. sc.n_trays_above,
			sc.Feed_loc+1 .. sc.Feed_loc+sc.n_trays_below);

	P[zP] ALIASES (
		sc.rectifying_section.P[1..sc.n_trays_above],
		sc.feed_tray.P,
		sc.stripping_section.P[1..sc.n_trays_below],
		sc.reboiler.P)
	WHERE zP IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	T[zT] ALIASES (
		sc.rectifying_section.T[1..sc.n_trays_above],
		sc.feed_tray.T,
		sc.stripping_section.T[1..sc.n_trays_below],
		sc.reboiler.T)
	WHERE zT IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	(* next one is simple because flash_base defines Qin *)
	Qin[zQ] ALIASES (sc.Tray[0..sc.N_trays].Qin)
	WHERE zQ IS_A set OF integer_constant WITH_VALUE (0..sc.N_trays);

	Lin[zL] ALIASES (
		sc.rectifying_section.tray_liqin[1..sc.n_trays_above].flow,
		sc.feed_tray.liqin.flow,
		sc.stripping_section.tray_liqin[1..sc.n_trays_below].flow,
		sc.reboiler.liqin.flow)
	WHERE zL IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	Vin[zV] ALIASES (
		sc.rectifying_section.tray_vapin[0..sc.n_trays_above].flow,
		sc.feed_tray.vapin.flow,
		sc.stripping_section.tray_vapin[1..sc.n_trays_below].flow)
	WHERE zV IS_A set OF integer_constant WITH_VALUE (0..sc.N_trays-1);

	FOR i IN sc.components CREATE

	x[i][zx[i]] ALIASES (
		sc.rectifying_section.Stack[1..sc.n_trays_above].x[i],
		sc.feed_tray.x[i],
		sc.stripping_section.Stack[1..sc.n_trays_below].x[i],
		sc.reboiler.x[i])
	WHERE zx[i] IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	y[i][zy[i]] ALIASES (
		sc.rectifying_section.Stack[1..sc.n_trays_above].y[i],
		sc.feed_tray.y[i],
		sc.stripping_section.Stack[1..sc.n_trays_below].y[i],
		sc.reboiler.y[i])
	WHERE zy[i] IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	kvalues_when_full_thermo[i][zk[i]] ALIASES (
		sc.rectifying_section.Stack[1..sc.n_trays_above].alpha[i],
		sc.feed_tray.alpha[i],
		sc.stripping_section.Stack[1..sc.n_trays_below].alpha[i],
		sc.reboiler.alpha[i])
	WHERE zk[i] IS_A set OF integer_constant WITH_VALUE (sc.VLE_set);

	END FOR (* components *);

METHODS
(* This MODEL defines no new equations, variables, or submodels *)
(* so we put in a bunch of harmless methods so the system defined
 * ones get replaced.
 *)
METHOD check_self;
END check_self;
METHOD check_all;
END check_all;
METHOD default_self;
END default_self;
METHOD default_all;
END default_all;
METHOD scale_self;
END scale_self;
METHOD scale_all;
END scale_all;
METHOD bound_self;
END bound_self;
METHOD bound_all;
END bound_all;
METHOD specify;
END specify;

END simple_column_profiles;


MODEL test_simple_column() REFINES testcmumodel();

	cd IS_A components_data(
		['n_pentane','n_hexane','n_heptane'], 'n_heptane'
	);
	pdVL IS_A phases_data('VL','Pitzer_vapor_mixture',
				'UNIFAC_liquid_mixture','none');
	pdV IS_A phases_data('V','Pitzer_vapor_mixture','none','none');
	pdL IS_A phases_data('L','none','UNIFAC_liquid_mixture','none');


	Feed_equil, Equilibrated IS_A start_false;
	Feed		IS_A stream(cd, pdVL, Feed_equil);
	Distillate	IS_A stream(cd, pdL, Equilibrated);
	Bottoms		IS_A stream(cd, pdL, Equilibrated);

	n_trays_above, n_trays_below IS_A integer_constant;
	n_trays_above :== 6;
	n_trays_below :== 5;
	reduce IS_A fraction;
	Column IS_A simple_column(
		pdVL,
		Distillate,
		n_trays_above,
		Feed,
		n_trays_below,
		Bottoms,
		Equilibrated,
		reduce
	);

	Profile IS_A simple_column_profiles(Column);
	boundwidth IS_A bound_width;

METHODS

METHOD default_self;
	boundwidth := 100;
	RUN Feed.default_self;
	RUN Distillate.default_self;
	RUN Bottoms.default_self;
	RUN Column.default_self;
	RUN Profile.default_self;
END default_self;

METHOD check_self;
	RUN Feed.check_self;
	RUN Distillate.check_self;
	RUN Bottoms.check_self;
	RUN Column.check_self;
	RUN Profile.check_self;
END check_self;

METHOD scale_self;
	RUN Feed.scale_self;
	RUN Distillate.scale_self;
	RUN Bottoms.scale_self;
	RUN Column.scale_self;
	RUN Profile.scale_self;
END scale_self;

METHOD bound_self;
	Column.boundwidth := boundwidth;
	Profile.boundwidth := boundwidth;
	Feed.boundwidth := boundwidth;
	Distillate.boundwidth := boundwidth;
	Bottoms.boundwidth := boundwidth;
	RUN Feed.bound_self;
	RUN Distillate.bound_self;
	RUN Bottoms.bound_self;
	RUN Column.bound_self;
	RUN Profile.bound_self;
END bound_self;

METHOD bound_all;
	RUN bound_self;
END bound_all;

METHOD scale_all;
	RUN scale_self;
END scale_all;

METHOD check_all;
	RUN check_self;
END check_all;

METHOD default_all;
	RUN default_self;
END default_all;

METHOD values;
	Column.feed_tray.alpha['n_pentane'] := 3;
	Column.feed_tray.alpha['n_hexane'] := 2;
	Column.feed_tray.alpha['n_heptane'] := 1;
	Column.condenser.reflux_ratio := 1.3;
	Feed.T := 298 {K};
	Feed.P := 1{atm};
	Feed.f['n_pentane'] := 3{mole/s};
	Feed.f['n_hexane'] := 3{mole/s};
	Feed.f['n_heptane'] := 3{mole/s};
	(* here we should SOLVE the feed tray *)
	RUN Column.propagate_feed_values;
END values;

END test_simple_column;

MODEL demo_column(
	components IS_A set OF symbol_constant;
	reference IS_A symbol_constant;
	n_trays IS_A integer_constant;
	feed_location IS_A integer_constant;
) WHERE (
	reference IN components == TRUE;
	n_trays > 5;
	feed_location > 2;
	feed_location < n_trays - 2;
) REFINES colmodel();

	cd	IS_A components_data(components,reference);
	pdVL IS_A phases_data('VL','Pitzer_vapor_mixture',
				'UNIFAC_liquid_mixture','none');
	pdV IS_A phases_data('V','Pitzer_vapor_mixture','none','none');
	pdL IS_A phases_data('L','none','UNIFAC_liquid_mixture','none');

	Equilibrated IS_A start_false;
	Feed		IS_A stream(cd, pdVL, Equilibrated);
	Distillate	IS_A stream(cd, pdL, Equilibrated);
	Bottoms		IS_A stream(cd, pdL, Equilibrated);

	n_trays_above, n_trays_below IS_A integer_constant;
	n_trays_above :== feed_location - 1;
	n_trays_below :== n_trays - feed_location - 1;
	reduce IS_A fraction;
	Column IS_A simple_column(
		pdVL,
		Distillate,
		n_trays_above,
		Feed,
		n_trays_below,
		Bottoms,
		Equilibrated,
		reduce
	);

	(* component names in order of boiling point. useful for methods. *)
	z_boiling_comp[1..CARD[components]] IS_A symbol;
	z_bc IS_A symbol;
	z_bi IS_A integer;

METHODS

METHOD default_self;
	boundwidth := 100;
	RUN Feed.default_self;
	RUN Distillate.default_self;
	RUN Bottoms.default_self;
	RUN Column.default_self;
END default_self;

METHOD check_self;
	RUN Feed.check_self;
	RUN Distillate.check_self;
	RUN Bottoms.check_self;
	RUN Column.check_self;
END check_self;

METHOD scale_self;
	RUN Feed.scale_self;
	RUN Distillate.scale_self;
	RUN Bottoms.scale_self;
	RUN Column.scale_self;
END scale_self;

METHOD bound_self;
	Column.boundwidth := boundwidth;
	Feed.boundwidth := boundwidth;
	Distillate.boundwidth := boundwidth;
	Bottoms.boundwidth := boundwidth;
	RUN Feed.bound_self;
	RUN Distillate.bound_self;
	RUN Bottoms.bound_self;
	RUN Column.bound_self;
END bound_self;

METHOD bound_all;
	RUN bound_self;
END bound_all;

METHOD scale_all;
	RUN scale_self;
END scale_all;

METHOD check_all;
	RUN check_self;
END check_all;

METHOD default_all;
	RUN default_self;
END default_all;

METHOD values;
	(* The demo user may very well want to rewrite this method
	 * for their particular mixture.
	 *)
	z_bi := 1;
	(* order the components arbitrarily in a list *)
	FOR i IN components DO
		z_boiling_comp[z_bi] := i;
		z_bi := z_bi + 1;
	END FOR;
	(* use a bubble point sort, pun intended, to order the components. *)
	FOR i IN [1..CARD[components]-1] DO
		FOR j IN [i+1 .. CARD[components]] DO
			IF cd.data[z_boiling_comp[i]].Tb >
				cd.data[z_boiling_comp[j]].Tb THEN
				z_bc := z_boiling_comp[j];
				z_boiling_comp[j] := z_boiling_comp[i];
				z_boiling_comp[i] := z_bc;
			END IF;
		END FOR;
	END FOR;
	z_bi := 1;
	(* assign close alpha's *)
	FOR i IN [1.. CARD[components]] DO
		Column.feed_tray.alpha[z_boiling_comp[i]] :=
			1+ 1.0*(CARD[components]-i+1); (* 1.0 here --> 0.2 *)
		IF (Feed.pd.phase_indicator == 'VL') THEN
			Feed.state.phase['vapor'].alpha[z_boiling_comp[i]] :=
				Column.feed_tray.alpha[z_boiling_comp[i]];
		END IF;
	END FOR;
	Column.condenser.reflux_ratio := 1.3;
	Feed.T := 298 {K};
	Feed.P := 1{atm};
	Feed.f[components] := 3{mole/s};
	RUN Column.propagate_feed_values;
END values;

END demo_column;


MODEL test_demo_column() REFINES testcmumodel();

METHODS
METHOD check_self;
	RUN demo.check_self;
END check_self;
METHOD check_all;
	RUN demo.check_all;
END check_all;
METHOD default_self;
	RUN demo.default_self;
END default_self;
METHOD default_all;
	RUN demo.scale_all;
END default_all;
METHOD scale_self;
	RUN demo.scale_self;
END scale_self;
METHOD scale_all;
	RUN demo.scale_all;
END scale_all;
METHOD bound_self;
	RUN demo.bound_self;
END bound_self;
METHOD bound_all;
	RUN demo.bound_all;
END bound_all;

METHOD specify;
	RUN demo.specify;
END specify;

METHOD values;
	RUN demo.values;
END values;

METHOD reset_to_mass_balance;
	RUN demo.Column.reset_to_mass_balance;
END reset_to_mass_balance;

METHOD reset_to_full_thermo;
	RUN demo.Column.reset_to_full_thermo;
END reset_to_full_thermo;

METHOD reset_to_adiabatic;
	RUN demo.Column.reset_to_adiabatic;
END reset_to_adiabatic;

END test_demo_column;

MODEL mw_demo_column() REFINES test_demo_column();
	demo IS_A demo_column(['methanol','water'],'water',13,7);
METHODS
END mw_demo_column;

MODEL abc_demo_column() REFINES test_demo_column();
	demo IS_A
	demo_column(['benzene','chloroform','acetone'],'benzene',13,7);
METHODS
END abc_demo_column;

MODEL c567_demo_column() REFINES test_demo_column();
	demo IS_A
	demo_column(['n_pentane','n_hexane','n_heptane'],'n_heptane',13,7);
METHODS
END c567_demo_column;