source: trunk/eml/stage_separators/reboiler.mso @ 680

#*-------------------------------------------------------------------
* 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