Changeset 700 for branches/gui/eml


Ignore:
Timestamp:
Dec 12, 2008, 5:17:09 PM (14 years ago)
Author:
gerson bicca
Message:

improved model DistillationReac? (BRANCH)

Location:
branches/gui/eml/stage_separators
Files:
4 edited

Legend:

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

    r699 r700  
    13871387        WeirHeight                              as length               (Brief="Weir height");
    13881388
     1389        stoic(NComp)    as Real(Brief="Stoichiometric matrix");
     1390        Hr                                              as energy_mol;
     1391        Pstartup                                as pressure;
     1392       
     1393        TopTemperature                  as temperature;
     1394        TbottomTemperature      as temperature;
     1395        LevelFraction                                   as fraction     (Brief = "Level Fraction");
     1396
     1397        TopComposition(NComp)                           as fraction     (Brief = "Component Molar Fraction at Top");
     1398        BottomComposition(NComp)                as fraction     (Brief = "Component Molar Fraction at Bottom");
     1399       
    13891400SET
    13901401
     
    14061417        VapourDrawOffFlow  as flow_mol          (Brief = "Stream Molar Flow Rate");
    14071418        LiquidDrawOffFlow   as flow_mol                         (Brief = "Stream Molar Flow Rate");
    1408        
     1419        MurphreeEff                     as Real         (Brief = "Murphree efficiency");
     1420
    14091421        out     VapourDrawOff   as vapour_stream                (Brief="Vapour Outlet in the section", PosX=1, PosY=0.50,Protected = true);
    14101422        out     LiquidDrawOff           as liquid_stream                        (Brief="Liquid Outlet in the section", PosX=1, PosY=0.61,Protected = true);
     
    14621474for i in [1:NumberOfTrays] do
    14631475
     1476"Murphree Efficiency"
     1477        TRAYS(i).OutletV.z =  MurphreeEff * (TRAYS(i).yideal - TRAYS(i).InletV.z) + TRAYS(i).InletV.z;
     1478       
    14641479"Energy Holdup"
    14651480        TRAYS(i).E = TRAYS(i).ML*TRAYS(i).OutletL.h + TRAYS(i).MV*TRAYS(i).OutletV.h - TRAYS(i).OutletL.P*V;
    14661481
     1482"Component Molar Balance"
     1483        diff(TRAYS(i).M)=TRAYS(i).Inlet.F*TRAYS(i).Inlet.z + TRAYS(i).InletL.F*TRAYS(i).InletL.z + TRAYS(i).InletV.F*TRAYS(i).InletV.z- TRAYS(i).OutletL.F*TRAYS(i).OutletL.z - TRAYS(i).OutletV.F*TRAYS(i).OutletV.z-
     1484        TRAYS(i).LiquidSideStream.F*TRAYS(i).LiquidSideStream.z-TRAYS(i).VapourSideStream.F*TRAYS(i).VapourSideStream.z + stoic*TRAYS(i).r3*TRAYS(i).ML*TRAYS(i).vL;
     1485       
    14671486"Energy Balance"
    14681487        diff(TRAYS(i).E) = ( TRAYS(i).Inlet.F*TRAYS(i).Inlet.h + TRAYS(i).InletL.F*TRAYS(i).InletL.h + TRAYS(i).InletV.F*TRAYS(i).InletV.h- TRAYS(i).OutletL.F*TRAYS(i).OutletL.h - TRAYS(i).OutletV.F*TRAYS(i).OutletV.h
    1469         -TRAYS(i).VapourSideStream.F*TRAYS(i).VapourSideStream.h - TRAYS(i).LiquidSideStream.F*TRAYS(i).LiquidSideStream.h + Q ) + TRAYS(i).Hr * TRAYS(i).r3 *TRAYS(i). vL*TRAYS(i).ML;
     1488        -TRAYS(i).VapourSideStream.F*TRAYS(i).VapourSideStream.h - TRAYS(i).LiquidSideStream.F*TRAYS(i).LiquidSideStream.h + Q ) + Hr * TRAYS(i).r3 *TRAYS(i). vL*TRAYS(i).ML;
    14701489
    14711490"Level of clear liquid over the weir"
     
    15691588        VapourDrawOffFlow = VapourDrawOff.F;
    15701589        LiquidDrawOffFlow = LiquidDrawOff.F;
     1590
     1591INITIAL
     1592
     1593for i in 1:NumberOfTrays do
     1594       
     1595"The initial temperature of the TRAYS"
     1596        TRAYS(i).OutletL.T = TopTemperature+(TbottomTemperature-TopTemperature)*((i-1)/(NumberOfTrays-1));
     1597
     1598"The initial Level of the TRAYS"
     1599        TRAYS(i).Level = LevelFraction*hw;
     1600
     1601end
     1602
     1603for i in 1:NComp-1 do
     1604       
     1605for j in 1:NumberOfTrays do
     1606
     1607"The initial composition of the TRAYS"
     1608        TRAYS(j).OutletL.z(i) = TopComposition(i) +(BottomComposition(i)-TopComposition(i) )*((j-1)/(NumberOfTrays-1));
     1609
     1610end
     1611
     1612end
    15711613
    15721614end
  • branches/gui/eml/stage_separators/icon/DistillationReac.svg

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  • branches/gui/eml/stage_separators/tray.mso

    r698 r700  
    192192        outer NComp     as Integer;
    193193       
    194         stoic(NComp)    as Real(Brief="Stoichiometric matrix");
    195         Hr                                              as energy_mol;
    196         Pstartup                                as pressure;
    197        
    198194VARIABLES
    199195
     
    209205
    210206        yideal(NComp)   as fraction;
    211         Emv                                     as Real (Brief = "Murphree efficiency");
    212207
    213208        M(NComp)                as mol                          (Brief="Molar Holdup in the tray");
     
    233228        r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4))*'l/mol/s';
    234229       
    235 "Component Molar Balance"
    236         diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z- OutletL.F*OutletL.z - OutletV.F*OutletV.z-
    237         LiquidSideStream.F*LiquidSideStream.z-VapourSideStream.F*VapourSideStream.z + stoic*r3*ML*vL;
    238 
    239230"Molar Holdup"
    240231        M = ML*OutletL.z + MV*OutletV.z;
     
    283274"Chemical Equilibrium"
    284275        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =       PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, yideal)*yideal;
    285 
    286         OutletV.z = Emv * (yideal - InletV.z) + InletV.z;
    287276
    288277        sum(OutletL.z)= sum(OutletV.z);
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