Changeset 455 for branches/packed


Ignore:
Timestamp:
Feb 12, 2008, 4:55:35 PM (15 years ago)
Author:
Paula Bettio Staudt
Message:

More flowsheet tests

Location:
branches/packed
Files:
1 added
4 edited

Legend:

Unmodified
Added
Removed
  • branches/packed/eml/stage_separators/column.mso

    r453 r455  
    12641264
    12651265Model Section_Column_Packed
    1266         ATTRIBUTES
    1267         Pallete         = true;
    1268         Icon            = "icon/SectionColumn";
    1269         Brief           = "Model of a column section.";
    1270         Info            =
    1271 "== Model of a column section containing ==
    1272 * NTrays trays.
    1273        
    1274 == Specify ==
    1275 * the feed stream of each tray (Inlet);
    1276 * the Murphree eficiency for each tray Emv;
    1277 * the InletL stream of the top tray;
    1278 * the InletV stream of the bottom tray.
    1279        
    1280 == Initial Conditions ==
    1281 * the trays temperature (OutletL.T);
    1282 * the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
    1283 * (NoComps - 1) OutletL (OR OutletV) compositions for each tray.
    1284 ";
    1285        
    1286         PARAMETERS
    1287         outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
    1288         outer NComp as Integer;
    1289         NTrays as Integer(Brief="Number of trays", Default=2);
     1266       
     1267        PARAMETERS
     1268        outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
     1269        outer NComp as Integer;
     1270        NStages as Integer(Brief="Number of trays", Default=2);
    12901271        topdown as Integer(Brief="Trays counting (1=top-down, -1=bottom-up)", Default=1);
    12911272        top as Integer(Brief="Number of top tray");
     
    12931274        H as length (Brief="Height of packing");
    12941275
    1295         SET
    1296         top = (NTrays-1)*(1-topdown)/2+1;
    1297         bot = NTrays/top;
    1298        
    1299         VARIABLES
    1300         stage(NTrays) as packedStage;
    1301        
    1302         EQUATIONS
    1303         stage.hs = H/NTrays;
    1304 
     1276        VARIABLES
     1277        stage(NStages) as packedStage_BilletSchultes;
     1278       
     1279        SET
     1280        top = (NStages-1)*(1-topdown)/2+1;
     1281        bot = NStages/top;
     1282        stage.hs = H/NStages;   
     1283        stage.V = stage.hs * stage.Ap;
     1284       
    13051285        CONNECTIONS
    13061286        stage([top+topdown:topdown:bot]).OutletV to stage([top:topdown:bot-topdown]).InletV;
     
    13161296        top as Integer(Brief="Number of top tray");
    13171297        bot as Integer(Brief="Number of bottom tray");
    1318        
    1319         SET
    1320         top = (NStages-1)*(1-topdown)/2+1;
    1321         bot = NStages/top;
    1322        
    1323         VARIABLES
    1324         stage(NStages) as packedStage;
     1298        H as length (Brief="Height of packing");
     1299        K as Real (Brief="Reboiler flow constant", Unit='mol*s^0.5/kg^0.5/m');
     1300       
     1301        VARIABLES
     1302        stage(NStages) as packedStage_BilletSchultes;
    13251303        cond as condenser;
    13261304        reb as reboiler;
    13271305        sptop as splitter;
    13281306        pump1 as pump;
     1307       
     1308        SET
     1309        top = (NStages-1)*(1-topdown)/2+1;
     1310        bot = NStages/top;
     1311        stage.hs = H/NStages;   
     1312        stage.V = stage.hs * stage.Ap;
    13291313       
    13301314        CONNECTIONS
     
    13401324        stage([top:topdown:bot-topdown]).OutletL to stage([top+topdown:topdown:bot]).InletL;
    13411325        stage(bot).OutletL to reb.InletL;
    1342        
    1343         EQUATIONS
    1344         reb.OutletV.F = stage(bot).OutletV.F;
    1345 end
     1326end
  • branches/packed/eml/stage_separators/tray.mso

    r454 r455  
    357357        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
    358358        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
    359 
     359        hs as length (Brief="Height of the packing stage");
     360       
    360361        VARIABLES
    361362        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
     
    365366        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Default = 0.007);
    366367        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");
    368368        dp as length (Brief="Particle diameter");
    369369        K as Real (Brief="Wall factor");
     
    389389        uV * Ap = OutletV.F * vV;
    390390       
    391 #       "Liquid holdup and Liquid flow"
    392 #       vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;
     391        "Liquid holdup and Liquid flow"
     392        vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;
    393393       
    394394        "Particle diameter"
     
    396396       
    397397        "Wall Factor"
    398         1 = K * 1+(2*dp/(3*ds*(1-e)));
     398        1 = K * (1 + (2*dp/(3*ds*(1-e))));
    399399       
    400400        "Reynolds number of the vapor stream"
     
    402402       
    403403        #"Resistance Coefficient"
    404         #Qsio = Cpo * (64/Rev) + 1.8/Rev^0.08);
     404        #Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
    405405        #Qsio = Cpo * (64/Rev);# + 1.8/Rev^0.08);
    406406
    407407        "Pressure drop and Vapor flow"
    408         (InletV.P - OutletV.P)/hs = Qsio*a*uV^2*rhoV / (2*e^2*K);
     408        (InletV.P - OutletV.P)/hs * 'm'/'Pa' = Qsio*a*uV^2*rhoV / (2*e^3*K) * 's^2'*'m^2'/'kg';
     409       
     410        "Efficiency"
     411        Emv = 1;
    409412end
    410413
  • branches/packed/sample/stage_separators/sample_column.mso

    r453 r455  
    508508        PP      as Plugin(Brief="Physical Properties",
    509509                Type="PP",
    510                 Components = [ "isobutane", "benzene"],
     510                Components = [ "isobutene", "n-pentane", "propylene", "benzene", "isobutane"],
    511511                LiquidModel = "PR",
    512512                VapourModel = "PR"
     
    525525       
    526526        CONNECTIONS
    527         feed.Outlet to sec.stage(15).Inlet;
    528        
    529         zero to sec.stage([1:14]).Inlet;
    530         zero to sec.stage([16:24]).Inlet;
    531        
    532         reb to sec.stage(24).InletV;
     527        feed.Outlet to sec.stage(10).Inlet;
     528       
     529        zero to sec.stage(1:9).Inlet;
     530        zero to sec.stage([11:sec.NStages]).Inlet;
     531       
     532        reb to sec.stage(sec.NStages).InletV;
    533533        cond to sec.stage(1).InletL;
     534
     535        VARIABLES
     536        deltaP_TOP as Real (Unit='atm/m');
     537        deltaP_BOT       as Real (Unit='atm/m');
     538       
     539        EQUATIONS
     540        deltaP_TOP = (sec.stage(1).InletV.P - sec.stage(1).OutletV.P)/sec.stage(1).hs;
     541        deltaP_BOT = (sec.stage(sec.NStages).InletV.P - sec.stage(sec.NStages).OutletV.P)/sec.stage(sec.NStages).hs;
    534542       
    535543        SPECIFY
     
    537545        feed.Outlet.T = 291 * 'K';
    538546        feed.Outlet.P = 168.3 * 'kPa';
    539         feed.Outlet.z = [0.5, 0.5];
     547        feed.Outlet.z = 1/NComp;
    540548
    541549        zero.F = 0 * 'kmol/h';
    542550        zero.T = 300 * 'K';
    543551        zero.P = 1 * 'atm';
    544         zero.z = [0.5, 0.5];
     552        zero.z = 1/NComp;
    545553        zero.v = 0;
    546554        zero.h = 0 * 'J/mol';
    547555       
    548         cond.F = 68 * 'kmol/h';
    549         cond.P = 150 * 'kPa';
    550         cond.T = 281.75 * 'K';
    551         cond.z = [0.6664, 0.3336];
    552 
    553         reb.F = 153 * 'kmol/h';
    554         reb.P = 185 * 'kPa';
    555         reb.T = 328.12 * 'K';
    556         reb.z = [0.001848, 0.9982];
    557        
    558         sec.stage.Emv = 1;
    559 #       sec.stage(1).OutletV.F = 150 * 'kmol/h';
    560 
    561         SET
    562         sec.NTrays = 24;
    563        
    564 #       sec.stage.PressureDropModel = "Leva";
    565 #       sec.stage.PackingType = "random";
    566 
    567         sec.stage.V = 4 * 'ft^3';
     556        cond.F = 85 * 'kmol/h';
     557        cond.P = 2.2 * 'atm';
     558        cond.T = 273 * 'K';
     559        cond.z = [0.26682, 0.19950, 0.26682, 0.000051, 0.26680];
     560
     561        reb.F = 143.4 * 'kmol/h';
     562        reb.P = 5 * 'atm';
     563        reb.T = 361 * 'K';
     564        reb.z = [0.0001611, 0.51834, 0.00000076, 0.48115, 0.00035];
     565       
     566        #sec.stage.Qsio = 1;
     567       
     568        SET
     569        sec.H = 4 * 'm';
     570        sec.NStages = 16;
    568571        sec.stage.Q = 0 * 'kW';
    569         sec.stage.Ap = 3.94 * 'ft^2';
     572        sec.stage.Ap = 1.5 * 'm^2';
     573        sec.stage.ds = 1.009 * 'm';
     574        sec.stage.Cpo = 0.763;
     575        sec.stage.e = 0.951;
     576        sec.stage.a = 112.6 * 'm^2/m^3';
    570577
    571578        INITIAL
    572         sec.stage.OutletL.T = [290:(330-290)/(sec.NTrays-1):330] *'K';
    573         sec.stage.Level = 0.5 * 'ft';
    574         sec.stage.OutletL.z(1) = 0.5;
     579        sec.stage.OutletL.T = [273:(360-273)/(sec.NStages-1):360] *'K';
     580        sec.stage.ML = 0.5 * 'kmol';
     581        sec.stage.OutletL.z([1:4]) = 1/NComp;
    575582       
    576583        OPTIONS
    577         InitialFile = "/home/paula/SectionColumn_Test_with8tray.rlt";
    578         TimeStep = 1;
    579         TimeEnd = 100;
    580         #GuessFile="SectionColumn_Test_with8tray.rlt";
    581         #Dynamic = false;
     584        DAESolver(File="dassl");
     585        TimeStep = 0.01;
     586        TimeEnd = 1;
    582587end
    583588
    584 FlowSheet Packed_kettle_cond_Test
     589FlowSheet Packed_kettle_cond_Test_1
    585590        PARAMETERS
    586591        PP      as Plugin(Brief="Physical Properties",
     
    630635        Qc.OutletQ.Q = -700 * 'cal/min';
    631636        col.pump1.dP = 0.1 * 'atm';
    632         col.stage.Emv = 1;
    633         col.stage.hs = 100 * 'mm';
    634        
    635         SET
    636         col.NStages = 10;
     637        col.stage.Qsio = 0.05;
     638       
     639        EQUATIONS
     640        col.reb.OutletV.F = col.K * sqrt(Qr.OutletQ.Q);
     641       
     642        SET
     643        col.NStages = 5;
    637644        col.cond.V = 1 * 'l';
    638645        col.cond.Across = 100 * 'cm^2';
     646        col.K = 0.2 * 'mol*min^0.5/kg^0.5/m';
    639647        col.reb.V = 2 * 'l';
    640648        col.reb.Across = 200 * 'cm^2';
    641         col.stage.V = 576.4 * 'cm^3';
    642649        col.stage.Q = 0 * 'kW';
    643650        col.stage.Ap = 56.74 * 'cm^2';
    644651        col.stage.ds = 85 * 'mm';
    645         col.stage.d = 20 * 'mm';
    646         col.stage.C = 2.18;
    647         col.stage.Cp = 1.329;
    648652        col.stage.e = 0.662;
    649653        col.stage.a = 185.4 * 'm^2/m^3';
    650 
     654        col.H = 1 * 'm';
     655        col.stage.Cpo = 0.763;
     656       
    651657        INITIAL
    652658        # condenser
    653659        col.cond.OutletL.T = (63.5+273.15) *'K';
    654660        col.cond.Level = 2 * 'cm';
    655         col.cond.OutletL.z(1) = 0.16;
     661        col.cond.OutletL.z(1) = 0.8; #0.16;
    656662
    657663        # reboiler
     
    662668        # column stages
    663669        col.stage.OutletL.T = [(63.5+273.15):((82+273.15)-(63.5+273.15))/(col.NStages-1):(82+273.15)] * 'K';
    664         col.stage.Level = 1 * 'cm';
    665         col.stage.OutletL.z(1) = 0.16;
     670        col.stage.Level = 2 * 'cm';
     671        #col.stage.ML = 0.2 * 'mol';
     672        col.stage.OutletL.z(1) = 0.5; #0.16;
    666673
    667674        OPTIONS
    668675        TimeStep = 0.1;
    669676        TimeEnd = 50;
    670         #GuessFile = "/home/paula/SectionColumn_Test_with8tray.rlt";
    671         #GuessFile="Distillation_kettle_cond_Test.rlt";
    672         #Dynamic = false;       
    673677end
  • branches/packed/sample/stage_separators/sample_tray.mso

    r454 r455  
    218218        inV.z = [0.0584, 0.9416];
    219219
    220         t1.Emv = 1;
    221220        t1.hs = 0.4 * 'm';#0.075 * 'm';
    222221#       t1.OutletV.F = 147.1 * 'kmol/h';
    223         t1.OutletL.F = 229.5 * 'kmol/h';
    224         t1.Qsio = 0.8;
     222#       t1.OutletL.F = 229.5 * 'kmol/h';
     223#       t1.Qsio = 2.2;
    225224       
    226225        SET
     
    235234
    236235        INITIAL
    237         t1.OutletL.T = 350 *'K';
     236        t1.OutletL.T = 310 *'K';
    238237        t1.ML = 0.5 * 'mol';
    239         t1.OutletL.z(1) = 0.2;
     238        t1.OutletL.z(1) = 0.05;
    240239       
    241240        OPTIONS
    242         #InitialFile = "/home/paula/tray_Test.rlt";
    243         InitialFile = "/home/paula/packedStage_Test.rlt";
     241        InitialFile = "packedStage_BilletSchultes_Test.rlt";
    244242        TimeStep = 2;   
    245243        TimeEnd = 50;
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