Changeset 454 for branches


Ignore:
Timestamp:
Feb 8, 2008, 6:20:12 PM (15 years ago)
Author:
Paula Bettio Staudt
Message:

A new shot. Model with Billet and Schultes correlations

Location:
branches/packed
Files:
2 edited

Legend:

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Added
Removed
  • branches/packed/eml/stage_separators/tray.mso

    r453 r454  
    169169end
    170170
    171 Model packedStageOld as trayBasic
     171Model packedStage_Navaes as trayBasic
    172172        PARAMETERS
    173173        PPwater as Plugin(Brief="Physical Properties",
     
    277277end
    278278
    279 Model packedStage as trayBasic
     279Model packedStage_Billet as trayBasic
    280280        PARAMETERS
    281281        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
     
    329329        uV * Across = OutletV.F * vV;
    330330       
    331 #       "Coefficient of Resistance"
    332 #       ksi * C^2 * (uL/uV * sqrt(rhoV/rhoL) * (niL/niV)^5.8)^3 = g/1*'s^2/m';
     331        "Coefficient of Resistance"
     332        ksi * C^2 * (uL/uV * sqrt(rhoV/rhoL) * (niL/niV)^2)^0.5 = g/1*'s^2/m';
    333333        #ksil = Cp * (exp(uL*rhoL/a/niL/200)*(hL/hLs)^0.3) * (64/Rev+(1.8/Rev)) *
    334334        ksil = Cp * (exp(uL*rhoL/a/niL/200)*(hL/hLs)^0.3) * (64/Rev+(1.8/Rev)) *
    335                                         ((e-hL)/e);
     335                                        ((e-hL)/e)^1.5;
    336336       
    337337#       "Liquid holdup and Liquid flow"
     
    345345
    346346        "Theoretical Liquid Holdup"
    347         #hLs = (12*a^2*niL*uL/g/rhoL)^0.333;
    348         hLs = (12*a^2*niL*uL/g/rhoL);
     347        hLs = (12*a^2*niL*uL/g/rhoL)^0.333;
     348        #hLs = (12*a^2*niL*uL/g/rhoL);
     349end
     350
     351Model packedStage_BilletSchultes as trayBasic
     352        PARAMETERS
     353        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
     354        g as acceleration;
     355        e as Real (Brief="Void fraction of packing, m^3/m^3");
     356        ds as length (Brief="Column diameter");
     357        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
     358        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
     359
     360        VARIABLES
     361        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
     362        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
     363        rhoL as dens_mass;
     364        rhoV as dens_mass;
     365        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Default = 0.007);
     366        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Default = 1.14);
     367        hs as length (Brief="Height of the packing stage");
     368        dp as length (Brief="Particle diameter");
     369        K as Real (Brief="Wall factor");
     370        Rev as Real (Brief="Reynolds number of the vapor stream");
     371        Qsio as Real (Brief="Resistance coefficient");
     372       
     373        SET
     374        Mw = PP.MolecularWeight();
     375       
     376        EQUATIONS
     377        "Liquid Density"
     378        rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
     379        "Vapour Density"
     380        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
     381        "Liquid viscosity"
     382        miL = PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
     383        "Vapour viscosity"
     384        miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
     385
     386        "Volume flow rate of liquid, m^3/m^2/s"
     387        uL * Ap = OutletL.F * vL;
     388        "Volume flow rate of vapor, m^3/m^2/s"
     389        uV * Ap = OutletV.F * vV;
     390       
     391#       "Liquid holdup and Liquid flow"
     392#       vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;
     393       
     394        "Particle diameter"
     395        dp = 6 * ((1-e)/a);
     396       
     397        "Wall Factor"
     398        1 = K * 1+(2*dp/(3*ds*(1-e)));
     399       
     400        "Reynolds number of the vapor stream"
     401        Rev = K*dp*uV*rhoV / (miV*(1-e));
     402       
     403        #"Resistance Coefficient"
     404        #Qsio = Cpo * (64/Rev) + 1.8/Rev^0.08);
     405        #Qsio = Cpo * (64/Rev);# + 1.8/Rev^0.08);
     406
     407        "Pressure drop and Vapor flow"
     408        (InletV.P - OutletV.P)/hs = Qsio*a*uV^2*rhoV / (2*e^2*K);
    349409end
    350410
  • branches/packed/sample/stage_separators/sample_tray.mso

    r453 r454  
    113113       
    114114        DEVICES
    115         t1 as packedStage;
     115        t1 as packedStage_Billet;
    116116        feed as source;
    117117        inL as liquid_stream;
     
    145145        t1.hs = 0.4 * 'm';#0.075 * 'm';
    146146        t1.OutletV.F = 147.1 * 'kmol/h';
    147         t1.OutletL.F = 229.5 * 'kmol/h';
    148         t1.ksi = 0.805;
     147#       t1.OutletL.F = 229.5 * 'kmol/h';
     148        #t1.ksi = 0.805;
    149149       
    150150        SET
     
    162162        INITIAL
    163163        t1.OutletL.T = 350 *'K';
    164         t1.ML = 0.2 * 'mol';
    165         t1.OutletL.z(1) = 0.1;
     164        t1.ML = 0.5 * 'mol';
     165        t1.OutletL.z(1) = 0.2;
     166       
     167        OPTIONS
     168        #InitialFile = "/home/paula/tray_Test.rlt";
     169        #InitialFile = "/home/paula/packedStage_Test.rlt";
     170        TimeStep = 2;   
     171        TimeEnd = 50;
     172end
     173
     174FlowSheet packedStage_BilletSchultes_Test
     175        PARAMETERS
     176        PP      as Plugin(Brief="Physical Properties",
     177                Type="PP",
     178                Components = [ "n-pentane", "benzene"],
     179                LiquidModel = "PR",
     180                VapourModel = "PR"
     181        );
     182        NComp   as Integer;
     183
     184        SET
     185        NComp = PP.NumberOfComponents;
     186
     187        VARIABLES
     188        deltaP as Real (Unit='atm/m');
     189       
     190        DEVICES
     191        t1 as packedStage_BilletSchultes;
     192        feed as source;
     193        inL as liquid_stream;
     194        inV as vapour_stream;
     195       
     196        CONNECTIONS
     197        feed.Outlet to t1.Inlet;
     198        inL to t1.InletL;
     199        inV to t1.InletV;
     200
     201        EQUATIONS
     202        deltaP = (t1.InletV.P - t1.OutletV.P)/t1.hs;
     203
     204        SPECIFY
     205        feed.Outlet.F = 113.4 * 'kmol/h';
     206        feed.Outlet.T = 291 * 'K';
     207        feed.Outlet.P = 1.66 * 'atm';
     208        feed.Outlet.z = [0.5, 0.5];
     209
     210        inL.F = 61.99 * 'kmol/h';       
     211        inL.P = 1.63 * 'atm';
     212        inL.T = 310 * 'K';
     213        inL.z = [0.1641, 0.8359];
     214
     215        inV.F = 201.25 * 'kmol/h';
     216        inV.P = 1.48 * 'atm';
     217        inV.T = 321 * 'K';
     218        inV.z = [0.0584, 0.9416];
     219
     220        t1.Emv = 1;
     221        t1.hs = 0.4 * 'm';#0.075 * 'm';
     222#       t1.OutletV.F = 147.1 * 'kmol/h';
     223        t1.OutletL.F = 229.5 * 'kmol/h';
     224        t1.Qsio = 0.8;
     225       
     226        SET
     227        #Metal Pall Ring - nominal packing size 50 mm - Billet and Schultes, 1999.
     228        t1.Q = 0 * 'kW';
     229        t1.Ap = 0.8 * 'm^2';
     230        t1.V = 0.8 * 'm^2' * 0.4 * 'm';
     231        t1.ds = 1.009 * 'm';
     232        t1.Cpo = 0.763;
     233        t1.e = 0.951;
     234        t1.a = 112.6 * 'm^2/m^3';
     235
     236        INITIAL
     237        t1.OutletL.T = 350 *'K';
     238        t1.ML = 0.5 * 'mol';
     239        t1.OutletL.z(1) = 0.2;
    166240       
    167241        OPTIONS
    168242        #InitialFile = "/home/paula/tray_Test.rlt";
    169243        InitialFile = "/home/paula/packedStage_Test.rlt";
    170         #DAESolver(File="dassl");
    171244        TimeStep = 2;   
    172245        TimeEnd = 50;
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