Changeset 721 for branches/gui/eml/stage_separators/reboiler.mso

Timestamp:

Feb 25, 2009, 7:51:53 PM (15 years ago)

Author:

gerson bicca

Message:

updates (tank/reboiler/condenser/column)

File:

• branches/gui/eml/stage_separators/reboiler.mso (modified) (3 diffs)

branches/gui/eml/stage_separators/reboiler.mso

@@ -225 +225 @@
 Model reboilerReact
         ATTRIBUTES
-        Pallete         = true;
+        Pallete         = false;
         Icon            = "icon/Reboiler"; 
         Brief           = "Model of a dynamic reboiler with reaction.";
@@ -248 +248 @@
 ";
         
-        PARAMETERS
+PARAMETERS
         outer PP as Plugin(Type="PP");
         outer NComp as Integer;
@@ -257 +257 @@
         Hr as energy_mol;
 
-        VARIABLES
-in      Inlet as stream(Brief="Feed Stream", PosX=0.8127, PosY=0, Symbol="_{in}");
-in      InletL as stream(Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
-out     OutletL as liquid_stream(Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
-out     OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
-        InletQ as power (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");
-
-        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");
-        Vol as volume;
-        startup as Real;
-        rhoV as dens_mass;
-        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"
+        Initial_Level                           as length               (Brief="Initial Level of liquid phase");
+        Initial_Temperature                     as temperature  (Brief="Initial Temperature of Reboiler");
+        Initial_Composition(NComp)      as fraction     (Brief="Initial Liquid Composition");
+        
+VARIABLES
+in      InletL  as stream                       (Brief="Liquid inlet stream", PosX=0, PosY=0.5254, Symbol="_{inL}");
+out     OutletL as liquid_stream        (Brief="Liquid outlet stream", PosX=0.2413, PosY=1, Symbol="_{outL}");
+out     OutletV as vapour_stream        (Brief="Vapour outlet stream", PosX=0.5079, PosY=0, Symbol="_{outV}");
+        InletQ  as power                        (Brief="Heat supplied", PosX=1, PosY=0.6123, Symbol="_{in}");
+
+        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");
+        Vol             as volume;
+        rhoV            as dens_mass;
+        r3                      as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
+        C(NComp)        as conc_mol     (Brief = "Molar concentration", Lower = -1);
+
+INITIAL
+
+        Level                                   = Initial_Level;
+        OutletL.T                               = Initial_Temperature;
+        OutletL.z(1:NComp-1)    = Initial_Composition(1:NComp-1)/sum(Initial_Composition);
+
+EQUATIONS
+"Molar Concentration"
         OutletL.z = vL * C;
         
-        "Reaction"
+"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)= Inlet.F*Inlet.z + InletL.F*InletL.z
-                - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL;
-        
-        "Energy Balance"
-        diff(E) = Inlet.F*Inlet.h + InletL.F*InletL.h
-                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + InletQ + Hr * r3 * vL*ML;
-        
-        "Molar Holdup"
+"Component Molar Balance"
+        diff(M)= InletL.F*InletL.z- OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL;
+        
+"Energy Balance"
+        diff(E) = InletL.F*InletL.h- OutletL.F*OutletL.h - OutletV.F*OutletV.h + InletQ + Hr * r3 * vL*ML;
+        
+"Molar Holdup"
         M = ML*OutletL.z + MV*OutletV.z; 
         
-        "Energy Holdup"
+"Energy Holdup"
         E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
         
-        "Mol fraction normalisation"
+"Mol fraction normalisation"
         sum(OutletL.z)=1.0;
         
-        "Liquid Volume"
+"Liquid Volume"
         vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
-        "Vapour Volume"
+
+"Vapour Volume"
         vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);  
-        "Vapour Density"
+
+"Vapour Density"
         rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z);
         
-        "Level of liquid phase"
+"Level of liquid phase"
         Level = ML*vL/Across;
 
         Vol = ML*vL;
         
-        "Mechanical Equilibrium"
+"Mechanical Equilibrium"
         OutletL.P = OutletV.P;
         
-        "Thermal Equilibrium"
+"Thermal Equilibrium"
         OutletL.T = OutletV.T;  
         
-        "Geometry Constraint"
+"Geometry Constraint"
         V = ML*vL + MV*vV;              
 
-        "Chemical Equilibrium"
+"Chemical Equilibrium"
         PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 
         PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;