#*-------------------------------------------------------------------
* EMSO Model Library (EML) Copyright (C) 2004 - 2007 ALSOC.
*
* This LIBRARY is free software; you can distribute it and/or modify
* it under the therms of the ALSOC FREE LICENSE as available at
* http://www.enq.ufrgs.br/alsoc.
*
* EMSO Copyright (C) 2004 - 2007 ALSOC, original code
* from http://www.rps.eng.br Copyright (C) 2002-2004.
* All rights reserved.
*
* EMSO is distributed under the therms of the ALSOC LICENSE as
* available at http://www.enq.ufrgs.br/alsoc.
*
*----------------------------------------------------------------------
* Author: Paula B. Staudt
* $Id: reboiler.mso 353 2007-08-30 16:12:27Z arge $
*--------------------------------------------------------------------*#

using "streams";

Model reboiler
	ATTRIBUTES
	Pallete 	= true;
	Icon 		= "icon/Reboiler"; 
	Brief 		= "Model of a dynamic reboiler - kettle.";
	Info 		=
"== Assumptions ==

* perfect mixing of both phases;
* thermodynamics equilibrium;
* no liquid entrainment in the vapour stream.
	
== Specify ==

* the inlet stream;
* the liquid inlet stream;
* the outlet flows: OutletV.F and OutletL.F;
* the heat supply.
	
== Initial Conditions ==

* the reboiler temperature (OutletL.T);
* the reboiler liquid level (Level);
* (NoComps - 1) OutletL (OR OutletV) compositions.
";	
	
	PARAMETERS
	outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
	outer NComp as Integer;
	Across as area (Brief="Cross Section Area of reboiler");
	V as volume (Brief="Total volume of reboiler");

	VARIABLES
in	Inlet as stream(Brief="Feed Stream", PosX=0.8127, PosY=0, Symbol="_{in}");
in	InletL as stream(Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
out	OutletL as liquid_stream(Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
out	OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
in	InletQ as energy_stream (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");

	M(NComp) as mol (Brief="Molar Holdup in the tray");
	ML as mol (Brief="Molar liquid holdup");
	MV as mol (Brief="Molar vapour holdup");
	E as energy (Brief="Total Energy Holdup on tray");
	vL as volume_mol (Brief="Liquid Molar Volume");
	vV as volume_mol (Brief="Vapour Molar volume");
	Level as length (Brief="Level of liquid phase");
	rhoV as dens_mass (Brief="Vapour Density");

	EQUATIONS
	"Component Molar Balance"
	diff(M)= Inlet.F*Inlet.z + InletL.F*InletL.z
		- OutletL.F*OutletL.z - OutletV.F*OutletV.z;
	
	"Energy Balance"
	diff(E) = Inlet.F*Inlet.h + InletL.F*InletL.h
		- OutletL.F*OutletL.h - OutletV.F*OutletV.h + InletQ.Q;
	
	"Molar Holdup"
	M = ML*OutletL.z + MV*OutletV.z; 
	
	"Energy Holdup"
	E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
	
	"Mol fraction normalisation"
	sum(OutletL.z)=1.0;
	sum(OutletL.z)=sum(OutletV.z);

	"Vapour Density"
	rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z);

	"Liquid Volume"
	vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
	
	"Vapour Volume"
	vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
	
	"Chemical Equilibrium"
	PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 
		PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;

	"Mechanical Equilibrium"
	OutletL.P = OutletV.P;
	
	"Thermal Equilibrium"
	OutletL.T = OutletV.T;
	
	"Geometry Constraint"
	V = ML*vL + MV*vV;
	
	"Level of liquid phase"
	Level = ML*vL/Across;
end

#*----------------------------------------------------------------------
* Model of a  Steady State reboiler with no thermodynamics equilibrium
*---------------------------------------------------------------------*# 
Model reboilerSteady
	ATTRIBUTES
	Pallete 	= true;
	Icon 		= "icon/ReboilerSteady"; 
	Brief 		= "Model of a  Steady State reboiler with no thermodynamics equilibrium - thermosyphon.";
	Info 		=
"== Assumptions ==
* perfect mixing of both phases;
* no thermodynamics equilibrium;
* no liquid entrainment in the vapour stream.
	
== Specify ==
* the InletL stream;
* the heat supply OR the outlet temperature (OutletV.T);
";	

	PARAMETERS
	outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
	outer NComp as Integer;
	DP as press_delta (Brief="Pressure Drop in the reboiler");

	VARIABLES
in	InletL as stream(Brief="Liquid inlet stream", PosX=0.3345, PosY=1, Symbol="_{inL}");
out	OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.3369, PosY=0, Symbol="_{outV}");
in	InletQ as energy_stream (Brief="Heat supplied", PosX=1, PosY=0.6111, Symbol="_{in}");
	vV as volume_mol (Brief="Vapour Molar volume");
	rhoV as dens_mass (Brief="Vapour Density");

	EQUATIONS
	"Molar Balance"
	InletL.F = OutletV.F;
	InletL.z = OutletV.z;
	
	"Vapour Volume"
	vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
	
	"Vapour Density"
	rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z);

	"Energy Balance"
	InletL.F*InletL.h + InletQ.Q = OutletV.F*OutletV.h;
	
	"Pressure"
	DP = InletL.P - OutletV.P;
end

#*----------------------------------------------------------------------
* Model of a  Steady State reboiler with fake calculation of 
* vaporisation fraction and output temperature, but with a real
* calculation of the output stream enthalpy
*---------------------------------------------------------------------*# 
Model reboilerSteady_fakeH
	ATTRIBUTES
	Pallete 	= true;
	Icon 		= "icon/ReboilerSteady"; 
	Brief 		= "Model of a  Steady State reboiler with fake calculation of outlet conditions.";
	Info 		=
"Model of a  Steady State reboiler with fake calculation of 
vaporisation fraction and output temperature, but with a real 
calculation of the output stream enthalpy.
";
	
	PARAMETERS
	outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
	outer NComp as Integer;
	DP as press_delta (Brief="Pressure Drop in the reboiler");
	k as Real (Brief = "Flow Constant", Unit='mol/J');
	
	VARIABLES
in	InletL as stream(Brief="Liquid inlet stream", PosX=0.3345, PosY=1, Symbol="_{inL}");
out	OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.3369, PosY=0, Symbol="_{outV}");
in	InletQ as energy_stream (Brief="Heat supplied", PosX=1, PosY=0.6111, Symbol="_{in}");

	EQUATIONS
	"Molar Balance"
	InletL.F = OutletV.F;
	InletL.z = OutletV.z;
	
	"Energy Balance"
	InletL.F*InletL.h + InletQ.Q = OutletV.F*OutletV.h;
	
	"Pressure"
	DP = InletL.P - OutletV.P;

	"Fake Vapourisation Fraction"
	OutletV.v = 1.0;
	
	"Fake output temperature"
	OutletV.T = 300*'K';
	
	"Pressure Drop through the reboiler"
	OutletV.F = k*InletQ.Q;
end

#*-------------------------------------------------------------------
* Model of a dynamic reboiler with reaction
*-------------------------------------------------------------------*#
Model reboilerReact
	ATTRIBUTES
	Pallete 	= true;
	Icon 		= "icon/Reboiler"; 
	Brief 		= "Model of a dynamic reboiler with reaction.";
	Info 		=
"== Assumptions ==
* perfect mixing of both phases;
* thermodynamics equilibrium;
* no liquid entrainment in the vapour stream;
* the reaction takes place only in the liquid phase.
	
== Specify ==
* the kinetics variables;
* the inlet stream;
* the liquid inlet stream;
* the outlet flows: OutletV.F and OutletL.F;
* the heat supply.

== Initial Conditions ==
* the reboiler temperature (OutletL.T);
* the reboiler liquid level (Level);
* (NoComps - 1) OutletL (OR OutletV) compositions.
";
	
	PARAMETERS
	outer PP as Plugin(Type="PP");
	outer NComp as Integer;
	Across as area (Brief="Cross Section Area of reboiler");
	V as volume (Brief="Total volume of reboiler");

	stoic(NComp) as Real(Brief="Stoichiometric matrix");
	Hr as energy_mol;
	Pstartup as pressure;

	VARIABLES
in	Inlet as stream(Brief="Feed Stream", PosX=0.8127, PosY=0, Symbol="_{in}");
in	InletL as stream(Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
out	OutletL as liquid_stream(Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
out	OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
in	InletQ as energy_stream (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");

	M(NComp) as mol (Brief="Molar Holdup in the tray");
	ML as mol (Brief="Molar liquid holdup");
	MV as mol (Brief="Molar vapour holdup");
	E as energy (Brief="Total Energy Holdup on tray");
	vL as volume_mol (Brief="Liquid Molar Volume");
	vV as volume_mol (Brief="Vapour Molar volume");
	Level as length (Brief="Level of liquid phase");
	Vol as volume;
	startup as Real;
	rhoV as dens_mass;
	r3 as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
	C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1);

	EQUATIONS
	"Molar Concentration"
	OutletL.z = vL * C;
	
	"Reaction"
	r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4)) * 'l/mol/s';

	"Component Molar Balance"
	diff(M)= Inlet.F*Inlet.z + InletL.F*InletL.z
		- OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL;
	
	"Energy Balance"
	diff(E) = Inlet.F*Inlet.h + InletL.F*InletL.h
		- OutletL.F*OutletL.h - OutletV.F*OutletV.h + InletQ.Q + Hr * r3 * vL*ML;
	
	"Molar Holdup"
	M = ML*OutletL.z + MV*OutletV.z; 
	
	"Energy Holdup"
	E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
	
	"Mol fraction normalisation"
	sum(OutletL.z)=1.0;
	
	"Liquid Volume"
	vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
	"Vapour Volume"
	vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);	
	"Vapour Density"
	rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z);
	
	"Level of liquid phase"
	Level = ML*vL/Across;

	Vol = ML*vL;
	
	"Mechanical Equilibrium"
	OutletL.P = OutletV.P;
	
	"Thermal Equilibrium"
	OutletL.T = OutletV.T;	
	
	"Geometry Constraint"
	V = ML*vL + MV*vV;		

	"Chemical Equilibrium"
	PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 
	PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;

	sum(OutletL.z)=sum(OutletV.z);
	
end