source: trunk/eml/stage_separators/condenser.mso @ 301

#*-------------------------------------------------------------------
* 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: condenser.mso 300 2007-07-04 22:55:05Z arge $
*--------------------------------------------------------------------*#

using "streams";

Model condenser
        ATTRIBUTES
        Pallete         = true;
        Icon            = "icon/Condenser"; 
        Brief           = "Model of a dynamic condenser.";
        Info            =
        "Assumptions:
         * perfect mixing of both phases;
         * thermodynamics equilibrium.
        
        Specify: 
         * the inlet stream;
         * the outlet flows: OutletV.F and OutletL.F;
         * the heat supply.
        
        Initial Conditions:
         * the condenser temperature (OutletL.T);
         * the condenser liquid level (Level);
         * (NoComps - 1) OutletL (OR OutletV) compositions.
        ";      
        
        PARAMETERS
        outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
        outer NComp as Integer;
        V as volume (Brief="Condenser total volume");
        Across as area (Brief="Cross Section Area of reboiler");

        VARIABLES
in      InletV as stream(Brief="Vapour inlet stream");
out     OutletL as liquid_stream(Brief="Liquid outlet stream");
out     OutletV as vapour_stream(Brief="Vapour outlet stream");
in      Q as heat_rate (Brief="Heat supplied");

        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");

        EQUATIONS
        "Component Molar Balance"
        diff(M) = InletV.F*InletV.z - OutletL.F*OutletL.z
                                - OutletV.F*OutletV.z;

        "Energy Balance"
        diff(E) = InletV.F*InletV.h - OutletL.F*OutletL.h
                                - OutletV.F*OutletV.h + Q;

        "Molar Holdup"
        M = ML*OutletL.z + MV*OutletV.z; 
        
        "Energy Holdup"
        E = ML*OutletL.h + MV*OutletV.h - OutletV.P*V;
        
        "Mol fraction normalisation"
        sum(OutletL.z)=1.0;
        sum(OutletL.z)=sum(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;

        "Thermal Equilibrium"
        OutletL.T = OutletV.T;

        "Mechanical Equilibrium"
        OutletV.P = OutletL.P;

        "Geometry Constraint"
        V = ML*vL + MV*vV;

        "Level of liquid phase"
        Level = ML*vL/Across;
end


#*----------------------------------------------------------------------
* Model of a  Steady State condenser with no thermodynamics equilibrium
*---------------------------------------------------------------------*# 
Model condenserSteady
        ATTRIBUTES
        Pallete         = true;
        Icon            = "icon/CondenserSteady"; 
        Brief           = "Model of a  Steady State condenser with no thermodynamics equilibrium.";
        Info            =
        "Assumptions:
         * perfect mixing of both phases;
         * no thermodynamics equilibrium.
        
        Specify: 
         * the inlet stream;
         * the pressure drop in the condenser;
         * the heat supply.
        ";
        
        PARAMETERS
        outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
        outer NComp as Integer;

        VARIABLES
in      InletV as stream(Brief="Vapour inlet stream");
out     OutletL as liquid_stream(Brief="Liquid outlet stream");
in      Q as heat_rate (Brief="Heat supplied");
        DP as press_delta (Brief="Pressure Drop in the condenser");

        EQUATIONS
        "Molar Balance"
        InletV.F = OutletL.F;
        InletV.z = OutletL.z;
                
        "Energy Balance"
        InletV.F*InletV.h = OutletL.F*OutletL.h + Q;
        
        "Pressure"
        DP = InletV.P - OutletL.P;
end

#*-------------------------------------------------------------------
* Condenser with reaction in liquid phase
*--------------------------------------------------------------------*#
Model condenserReact
        ATTRIBUTES
        Pallete         = true;
        Icon            = "icon/Condenser"; 
        Brief           = "Model of a Condenser with reaction in liquid phase.";
        Info            =
        "Assumptions:
         * perfect mixing of both phases;
         * thermodynamics equilibrium;
         * the reaction only takes place in liquid phase.
        
        Specify:
         * the reaction related variables;
         * the inlet stream;
         * the outlet flows: OutletV.F and OutletL.F;
         * the heat supply.
        
        Initial Conditions:
         * the condenser temperature (OutletL.T);
         * the condenser liquid level (Level);
         * (NoComps - 1) OutletL (OR OutletV) compositions.
        ";
        
        PARAMETERS
        outer PP as Plugin(Type="PP");
        outer NComp as Integer;
        V as volume (Brief="Condenser total volume");
        Across as area (Brief="Cross Section Area of reboiler");

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

        VARIABLES
in      InletV as stream(Brief="Vapour inlet stream");
out     OutletL as liquid_stream(Brief="Liquid outlet stream");
out     OutletV as vapour_stream(Brief="Vapour outlet stream");

        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");
        Q as heat_rate (Brief="Heat supplied");
        Vol as volume;
        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) = InletV.F*InletV.z - OutletL.F*OutletL.z
                                - OutletV.F*OutletV.z + stoic*r3*ML*vL;

        "Energy Balance"
        diff(E) = InletV.F*InletV.h - OutletL.F*OutletL.h
                                - OutletV.F*OutletV.h + Q + Hr * r3 * ML*vL;

        "Molar Holdup"
        M = ML*OutletL.z + MV*OutletV.z; 
        
        "Energy Holdup"
        E = ML*OutletL.h + MV*OutletV.h - OutletV.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);

        "Thermal Equilibrium"
        OutletL.T = OutletV.T;

        "Mechanical Equilibrium"
        OutletV.P = OutletL.P;

        "Geometry Constraint"
        V = ML*vL + MV*vV;

        Vol = ML*vL;
        
        "Level of liquid phase"
        Level = ML*vL/Across;
        
        "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