Ignore:
Timestamp:
Oct 23, 2006, 5:26:39 PM (16 years ago)
Author:
Paula Bettio Staudt
Message:

Included reactive distillation column

File:
1 edited

Legend:

Unmodified
Added
Removed
  • mso/eml/stage_separators/tray.mso

    r37 r38  
    142142end
    143143
     144#*-------------------------------------------------------------------
     145* Model of a tray with reaction
     146*-------------------------------------------------------------------*#
     147Model trayReact
     148
     149        PARAMETERS
     150ext PP as CalcObject;
     151ext NComp as Integer;
     152        V as volume(Brief="Total Volume of the tray");
     153        Q as power (Brief="Rate of heat supply");
     154        Ap as area (Brief="Plate area = Atray - Adowncomer");
     155       
     156        Ah as area (Brief="Total holes area");
     157        lw as length (Brief="Weir length");
     158        g as acceleration (Default=9.81);
     159        hw as length (Brief="Weir height");
     160        beta as fraction (Brief="Aeration fraction");
     161        alfa as fraction (Brief="Dry pressure drop coefficient");
     162
     163        stoic(NComp) as Real(Brief="Stoichiometric matrix");
     164        Hr as energy_mol;
     165        Pstartup as pressure;
     166       
     167        VARIABLES
     168in      Inlet as stream;
     169in      InletL as stream;
     170in      InletV as stream;
     171out     OutletL as stream_therm;
     172out     OutletV as stream_therm;
     173
     174        yideal(NComp) as fraction;
     175        Emv as Real (Brief = "Murphree efficiency");
     176
     177        M(NComp) as mol (Brief="Molar Holdup in the tray");
     178        ML as mol (Brief="Molar liquid holdup");
     179        MV as mol (Brief="Molar vapour holdup");
     180        E as energy (Brief="Total Energy Holdup on tray");
     181        vL as volume_mol (Brief="Liquid Molar Volume");
     182        vV as volume_mol (Brief="Vapour Molar volume");
     183        Level as length (Brief="Height of clear liquid on plate");
     184        Vol as volume;
     185       
     186        rhoL as dens_mass;
     187        rhoV as dens_mass;
     188        r as reaction_mol (Brief = "Reaction rate", Unit = "mol/l/s");
     189        C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1); #, Unit = "mol/l");
     190       
     191        EQUATIONS
     192        "Molar Concentration"
     193        OutletL.z = vL * C;
     194       
     195        "Component Molar Balance"
     196        diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
     197                - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r*ML*vL;
     198       
     199        "Energy Balance"
     200        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
     201                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q ) + Hr * r * vL*ML;
     202       
     203        "Molar Holdup"
     204        M = ML*OutletL.z + MV*OutletV.z;
     205       
     206        "Energy Holdup"
     207        E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
     208       
     209        "Mol fraction normalisation"
     210        sum(OutletL.z)= 1.0;
     211       
     212        "Liquid Volume"
     213        vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
     214        "Vapour Volume"
     215        vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
     216
     217        "Thermal Equilibrium"
     218        OutletV.T = OutletL.T;
     219       
     220        "Mechanical Equilibrium"
     221        OutletV.P = OutletL.P;
     222       
     223        "vaporization fraction "
     224        OutletV.v = 1.0;
     225        OutletL.v = 0.0;
     226       
     227        "Level of clear liquid over the weir"
     228        Level = ML*vL/Ap;
     229
     230        Vol = ML*vL;
     231       
     232        "Liquid Density"
     233        rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
     234        "Vapour Density"
     235        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
     236
     237        if (Level > (beta * hw)) then
     238                "Francis Equation"
     239                OutletL.F = (1.84*"m^0.5/s"*lw*((Level-(beta*hw))/(beta))^1.5/vL);
     240        else
     241                "Low level"
     242                OutletL.F = 0 * "mol/h";
     243        end
     244
     245               
     246        "Pressure Drop through the tray"
     247        OutletV.F = (1 + tanh(1 * (OutletV.P - Pstartup)/"Pa"))/2 *
     248                Ah/vV * sqrt(2*(OutletV.P - InletL.P + 1e-8 * "atm") / (alfa*rhoV) );
     249       
     250
     251        "Chemical Equilibrium"
     252        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
     253                PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*yideal;
     254       
     255        OutletV.z = Emv * (yideal - InletV.z) + InletV.z;
     256       
     257        sum(OutletL.z)= sum(OutletV.z);
     258       
     259        "Geometry Constraint"
     260        V = ML* vL + MV*vV;
     261end
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