Changeset 477

Timestamp:

Mar 7, 2008, 3:46:44 PM (15 years ago)

Author:

Paula Bettio Staudt

Message:

Some modifications

Location:

branches/packed

Files:

• eml/stage_separators/column.mso (modified) (1 diff)
• eml/stage_separators/tray.mso (modified) (2 diffs)
• sample/stage_separators/sample_column.mso (modified) (5 diffs)
• sample/stage_separators/sample_tray.mso (modified) (1 diff)

branches/packed/eml/stage_separators/column.mso

@@ -1275 +1275 @@
 
         VARIABLES
-        stage(NStages) as packedStage_BilletSchultes;
+        stage(NStages) as packedStage;#_BilletSchultes;
         
         SET

branches/packed/eml/stage_separators/tray.mso

@@ -365 +365 @@
         rhoL as dens_mass;
         rhoV as dens_mass;
-        uL as Real (Brief="volume flow rate of liquid, m^3/m^2/s", Default = 0.007);
-        uV as Real (Brief="volume flow rate of vapor, m^3/m^2/s", Default = 1.14);
+        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = 0, Default = 0.007);
+        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = 0, Default = 1.14);
         dp as length (Brief="Particle diameter", Default=1e-3);
         invK as Real (Brief="Wall factor");
@@ -661 +661 @@
 end
 
-
+Model packedStage
+        PARAMETERS
+outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
+outer NComp as Integer;
+        V as volume(Brief="Total Volume of the tray");
+        Q as heat_rate (Brief="Rate of heat supply"); 
+        Ap as area (Brief="Plate area = Atray - Adowncomer");
+
+        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
+        g as acceleration;
+        e as Real (Brief="Void fraction of packing, m^3/m^3");
+        ds as length (Brief="Column diameter");
+        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
+        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
+        hs as length (Brief="Height of the packing stage");
+        Qsio as Real (Brief="Resistance coefficient", Lower = 0);
+
+        VARIABLES
+in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
+in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
+in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
+out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
+out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
+
+        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");
+        
+        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
+        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
+        rhoL as dens_mass;
+        rhoV as dens_mass;
+        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
+        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
+        dp as length (Brief="Particle diameter", Default=1e-3);
+        invK as Real (Brief="Wall factor");
+#       Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
+#       Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
+        Al as area;
+        
+        SET
+        Mw = PP.MolecularWeight();
+
+        EQUATIONS
+        "Component Molar Balance"
+        diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
+                - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
+#       diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
+#       OutletL.z = OutletV.z;
+
+        "Energy Balance"
+        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
+                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
+        
+        "Molar Holdup"
+        M = ML*OutletL.z + MV*OutletV.z;
+        
+        "Energy Holdup"
+        E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
+        
+        "Mol fraction normalisation"
+        sum(OutletL.z)= 1.0;
+        sum(OutletL.z)=sum(OutletV.z);
+        
+        "Liquid Volume"
+        vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour Volume"
+        vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
+        
+        "Chemical Equilibrium"
+#       OutletV.z = OutletL.z;
+        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 
+                PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
+        
+        "Thermal Equilibrium"
+        OutletV.T = OutletL.T;
+        
+        "Mechanical Equilibrium"
+        OutletL.P = OutletV.P;
+        
+        "Geometry Constraint"
+        V*e = ML*vL + MV*vV;
+        
+        "Liquid Density"
+        rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour Density"
+        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
+        "Liquid viscosity"
+        miL = PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour viscosity"
+        miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
+        
+        Al = ML*vL/hs;
+
+        "Volume flow rate of liquid, m^3/m^2/s"
+        uL * Al = OutletL.F * vL;
+        "Volume flow rate of vapor, m^3/m^2/s"
+        uV * (Ap*e - Al) = OutletV.F * vV;
+        
+        "Liquid holdup and Liquid flow"
+        vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;
+        
+        "Particle diameter"
+        dp = 6 * (1-e)/a;
+        
+        "Wall Factor"
+        invK = (1 + (2*dp/(3*ds*(1-e))));
+        
+#*      "Reynolds number of the vapor stream"
+        Rev*invK = dp*uV*rhoV / (miV*(1-e));
+
+        Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
+        if Rev > 1e-4 then
+                "Resistance Coefficient"        
+                Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
+        else
+                Qsio = 1;
+        end
+*#
+        "Pressure drop and Vapor flow"
+        (InletV.P - OutletV.P)/hs  = Qsio*a*uV^2*rhoV*invK / (2*e^3);
+end
+
+# component #1 = nitrogen; #2 = water
+Model packedStage_AirWater
+        PARAMETERS
+outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
+outer NComp as Integer;
+        V as volume(Brief="Total Volume of the tray");
+        Q as heat_rate (Brief="Rate of heat supply"); 
+        Ap as area (Brief="Plate area = Atray - Adowncomer");
+
+        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
+        g as acceleration;
+        e as Real (Brief="Void fraction of packing, m^3/m^3");
+        ds as length (Brief="Column diameter");
+        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
+        Ch as Real (Brief="Constant for ah equation"); # Billet and Schultes, 1999.
+        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
+        hs as length (Brief="Height of the packing stage");
+        #Qsio as Real (Brief="Resistance coefficient", Lower = 0);
+
+        VARIABLES
+in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
+in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
+in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
+out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
+out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
+
+        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");
+        
+        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
+        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
+        rhoL as dens_mass;
+        rhoV as dens_mass;
+        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
+        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
+        dp as length (Brief="Particle diameter", Default=1e-3);
+        invK as Real (Brief="Wall factor");
+        Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
+#       Rel as Real (Brief="Reynolds number of the liquid stream", Lower = -10, Default=100);
+#       ah as Real (Brief="Hydraulic surface area", Unit='m^2/m^3');
+        Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
+        Al as area;
+        
+        SET
+        Mw = PP.MolecularWeight();
+
+        EQUATIONS
+        "Component Molar Balance"
+#       diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
+#               - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
+        diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
+
+        "Energy Balance"
+        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
+                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
+        
+        "Molar Holdup"
+        M = ML*OutletL.z + MV*OutletV.z;
+        
+        "Energy Holdup"
+        E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
+        
+#       "Mol fraction normalisation"
+#       sum(OutletL.z)= 1.0;
+#       sum(OutletL.z)=sum(OutletV.z);
+        
+        "Chemical Equilibrium"
+        OutletV.z = [1 0];
+        OutletL.z = [0 1];
+#       PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 
+#               PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
+        
+        "Thermal Equilibrium"
+        OutletV.T = OutletL.T;
+        
+        "Mechanical Equilibrium"
+        OutletL.P = OutletV.P;
+        
+        "Geometry Constraint"
+        V*e = ML*vL + MV*vV;
+        
+        "Liquid Density"
+        rhoL = 999 * 'kg/m^3';#PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour Density"
+        rhoV = 1.19 * 'kg/m^3'; #PP.VapourDensity(InletV.T, InletV.P, InletV.z);
+        "Liquid viscosity"
+        miL = 0.001 * 'kg/m/s' ; #PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour viscosity"
+        miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
+        "Liquid Volume"
+        vL = 18 * 'g/mol' / rhoV; #PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
+        "Vapour Volume"
+        vV = 28 * 'g/mol' / rhoL; #PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
+
+        "Cross section area ocupied by the liquid"
+        Al = ML*vL/hs;
+
+        "Volume flow rate of liquid, m^3/m^2/s"
+        uL * Al = OutletL.F * vL;
+
+        "Volume flow rate of vapor, m^3/m^2/s"
+        uV * (Ap*e - Al) = OutletV.F * vV;
+
+        "Particle diameter"
+        dp = 6 * (1-e)/a;
+        
+        "Wall Factor"
+        invK = (1 + (2*dp/(3*ds*(1-e))));
+        
+        "Reynolds number of the vapor stream"
+        Rev*invK = dp*uV*rhoV / (miV*(1-e));
+#*      "Reynolds number of the liquid stream"
+        Rel = uL*rhoL / (a*miL);
+
+        if Rel < 5 then
+                if Rel < 1e-4 then
+                        ah = 0 * '1/m';
+                else
+                        "Hydraulic surface area"
+                        ah = a * Ch * Rel^0.15 * (uL^2*a/g)^0.1; #(Rel^2*a^3*miL^2/rhoL^2/g)^0.1; #
+                end
+        else
+                ah = a * Ch * 0.85 * Rel^0.25 * (uL^2*a/g)^0.1; #(Rel^2*a^3*miL^2/rhoL^2/g)^0.1; #
+        end
+*#      
+#       if ah equal 0 then
+#               uL = 0 * 'm/s';
+#       else
+                "Liquid holdup and Liquid flow"
+                vL * ML = V * (12*miL*a^2*uL/rhoL/g)^1/3; # * (ah/a)^1;
+#       end
+        
+        "Resistance Coefficient"        
+        Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
+
+        "Pressure drop and Vapor flow"
+        (InletV.P - OutletV.P)/hs  = 3*Qsio*a*uV^2*rhoV*invK / (2*e^3);
+end

branches/packed/sample/stage_separators/sample_column.mso

@@ -556 +556 @@
         
         SET
-        sec.H = 16 * 'm';
+        sec.H = 4 * 'm';
         sec.NStages = 8;
         sec.stage.Q = 0 * 'kW';
@@ -564 +564 @@
         sec.stage.e = 0.951;
         sec.stage.a = 112.6 * 'm^2/m^3';
-        sec.stage.Qsio = 1;
+        sec.stage.Qsio = 0.8;
 
         INITIAL
         sec.stage.OutletL.T =[283:(325-283)/(sec.NStages-1):325] *'K';
-        sec.stage.ML = 0.3 * 'kmol';
+        sec.stage.ML = 0.1 * 'kmol';
         sec.stage.OutletL.z([1:4]) = [0.2, 0.2, 0.2, 0.2];
 
@@ -574 +574 @@
         #InitialFile = "/home/paula/SectionColumn_Test_with8tray.rlt";
         DAESolver(File="dassl");
+        NLASolver(File="nlasolver");
         TimeStep = 1;
         TimeEnd = 10;
@@ -665 +666 @@
 
         # column stages
-        col.stage.OutletL.T = [(63.5+273.15):((82+273.15)-(63.5+273.15))/(col.NStages-1):(82+273.15)] * 'K';
+        col.stage.OutletL.T = [(62.5+273.15):((83+273.15)-(62.5+273.15))/(col.NStages-1):(83+273.15)] * 'K';
         #col.stage.Level = 2 * 'cm';
         col.stage.ML = 0.2 * 'mol';
@@ -671 +672 @@
 
         OPTIONS
+        DAESolver(File="dassl");
         TimeStep = 0.1;
         TimeEnd = 50;

branches/packed/sample/stage_separators/sample_tray.mso

@@ -321 +321 @@
         TimeEnd = 60;
 end
+
+#to compare with tray_Test_1
+FlowSheet packedStage_Test_1
+        PARAMETERS
+        PP      as Plugin(Brief="Physical Properties",
+                Type="PP",
+                Components = [ "n-pentane", "benzene"],
+                LiquidModel = "PR",
+                VapourModel = "PR"
+        );
+        NComp   as Integer;
+
+        SET
+        NComp = PP.NumberOfComponents;
+        
+        VARIABLES
+        deltaP as Real (Unit='atm/m');
+        
+        DEVICES
+        t1 as packedStage;
+        feed as source;
+        inL as liquid_stream;
+        inV as vapour_stream;
+        
+        CONNECTIONS
+        feed.Outlet to t1.Inlet;
+        inL to t1.InletL;
+        inV to t1.InletV;
+
+        EQUATIONS
+        deltaP = (t1.InletV.P - t1.OutletV.P)/t1.hs;
+        
+        SPECIFY
+        feed.Outlet.F = 113.4 * 'kmol/h';
+        feed.Outlet.T = 291 * 'K';
+        feed.Outlet.P = 1.66 * 'atm';
+        feed.Outlet.z = [0.5, 0.5];
+        
+        inL.P = 165 * 'kPa';
+        inL.T = 315 * 'K'; #310 * 'K';
+        inL.F = 61.99 * 'kmol/h';
+        inL.z = [0.1641, 0.8359];#[0.5, 0.5];#
+
+        inV.F = 201.25 * 'kmol/h';
+        inV.P = 150 * 'kPa';
+        inV.T = 315 * 'K'; #321 * 'K';
+        inV.z = [0.0584, 0.9416];#[0.5, 0.5];#
+        
+        t1.OutletV.P = 145 * 'kPa';
+        
+        SET
+        #Metal Pall Ring - nominal packing size 50 mm - Billet and Schultes, 1999.
+        t1.Q = 0 * 'kW';
+        t1.Ap = 0.8 * 'm^2';
+        t1.V = 0.8 * 'm^2' * 0.4 * 'm';
+        t1.ds = 1.009 * 'm';
+        t1.Cpo = 0.763;
+        t1.e = 0.951;
+        t1.a = 112.6 * 'm^2/m^3';
+        t1.hs = 0.4 * 'm';
+        t1.Qsio = 1;
+        
+        INITIAL
+        t1.OutletL.T = 315 *'K';
+        t1.ML = 0.25 * 'kmol';
+        t1.OutletL.z(1) = 0.1641;
+        
+        OPTIONS
+        DAESolver(File="sundials");
+        TimeStep = 0.001;
+        TimeEnd = 0.1;
+end
+
+#to compare with tray_Test_2
+FlowSheet packedStage_Test_2
+        PARAMETERS
+        PP      as Plugin(Brief="Physical Properties",
+                Type="PP",
+                Components = [ "isobutane", "n-pentane", "propylene",
+                "benzene", "isobutene" ],
+                LiquidModel = "PR",
+                VapourModel = "PR"
+        );
+        NComp   as Integer;
+
+        SET
+        NComp = PP.NumberOfComponents;
+
+        VARIABLES
+        deltaP as Real (Unit='inH2O/m*mm/in');
+        phiL as Real;
+        
+        DEVICES
+        t1 as packedStage;
+        feed as source;
+        inL as liquid_stream;
+        inV as vapour_stream;
+        
+        CONNECTIONS
+        feed.Outlet to t1.Inlet;
+        inL to t1.InletL;
+        inV to t1.InletV;
+
+        EQUATIONS
+        deltaP = (t1.InletV.P - t1.OutletV.P)/t1.hs;
+        phiL = t1.vL * t1.ML/t1.V;
+
+        SPECIFY
+        feed.Outlet.F = 0 * 'kmol/h';
+        feed.Outlet.T = 300 * 'K';
+        feed.Outlet.P = 1.66 * 'atm';
+        feed.Outlet.z = [0.226, 0.425, 0.035, 0.025, 0.289];
+
+        inL.F = 71.21 * 'kmol/h';       
+        inL.P = 2.22 * 'atm';
+        inL.T = 297.6 * 'K';
+        inL.z = [0.226, 0.425, 0.035, 0.025, 0.289];
+
+        inV.F = 175.3 * 'kmol/h';
+        inV.P = 2.3062 * 'atm';
+        inV.T = 308.3 * 'K';
+        inV.z = [0.265, 0.233, 0.150, 0.014, 0.338];
+        
+        #t1.OutletV.P = 2.305 * 'atm';
+        #t1.OutletV.F = 165 * 'kmol/h';
+        
+        SET
+        #Metal Pall Ring - nominal packing size 50 mm - Billet and Schultes, 1999.
+        t1.Q = 0 * 'kW';
+        #t1.Ap = 0.8 * 'm^2';
+        #t1.V = 0.8 * 'm^2' * 0.4 * 'm';
+#       t1.ds = 1.009 * 'm';
+        t1.Cpo = 0.763;
+        t1.e = 0.951;
+        t1.a = 112.6 * 'm^2/m^3';
+#       t1.hs = 0.4 * 'm';
+
+        t1.V = 4 * 'ft^2' * 1 * 'ft';
+        t1.Ap = 4 * 'ft^2';
+        t1.hs = 1 * 'ft';
+        t1.ds = 2.26 * 'ft';
+        t1.Qsio = 100;
+
+        INITIAL
+        t1.OutletL.T = 290 *'K';
+        t1.ML = 0.02 * 'kmol';
+        t1.OutletL.z([1:4]) = [0.226, 0.425, 0.035, 0.025]; #[0.022, 0.0425, 0.0035, 0.95];
+        
+        OPTIONS
+        DAESolver(File="sundials");
+        #InitialFile = "/home/paula/tray_Test_2.rlt";
+        TimeStep = 0.01;
+        TimeEnd = 10;
+end
+
+FlowSheet packedStageAirWater_Test
+        PARAMETERS
+        PP      as Plugin(Brief="Physical Properties",
+                Type="PP",
+                Components = [ "nitrogen", "water"],
+                LiquidModel = "IdealLiquid",
+                VapourModel = "Ideal"
+        );
+        NComp   as Integer;
+
+        SET
+        NComp = PP.NumberOfComponents;
+
+        VARIABLES
+        deltaP as Real (Unit='inH2O/m*mm/in');
+        phiL as Real;
+        
+        DEVICES
+        t1 as packedStage_AirWater;
+        feed as source;
+        inL as liquid_stream;
+        inV as vapour_stream;
+        
+        CONNECTIONS
+        feed.Outlet to t1.Inlet;
+        inL to t1.InletL;
+        inV to t1.InletV;
+
+        EQUATIONS
+        deltaP = (t1.InletV.P - t1.OutletV.P)/t1.hs;
+        phiL = t1.vL * t1.ML/t1.V;
+
+        SPECIFY
+        feed.Outlet.F = 0 * 'kmol/h';
+        feed.Outlet.T = 300 * 'K';
+        feed.Outlet.P = 1 * 'atm';
+        feed.Outlet.z = [0 1];
+
+        inL.F = 71.21 * 'kmol/h';       
+        inL.P = 1 * 'atm';
+        inL.T = 293 * 'K';
+        inL.z = [0 1];
+
+        inV.F = 175.3 * 'kmol/h';
+        inV.P = 1.06 * 'atm';
+        inV.T = 295 * 'K';
+        inV.z = [1 0];
+        
+        t1.OutletV.P = 1.05 * 'atm';
+        
+        SET
+        #Metal Bialecki Ring - nominal packing size 25 mm - Billet and Schultes, 1999.
+        t1.Cpo = 0.891;
+        t1.Ch = 0.692;
+        t1.e = 0.956;
+        t1.a = 210 * 'm^2/m^3';
+
+        t1.Q = 0 * 'kW';
+        t1.V = 0.018 * 'm^2' * 1.4 * 'm';
+        t1.Ap = 0.018 * 'm^2';
+        t1.hs = 1.4 * 'm';
+        t1.ds = 0.15 * 'm';
+
+        INITIAL
+        t1.OutletL.T = 294 *'K';
+        t1.ML = 0.0002 * 'kmol';
+        t1.OutletL.z(1) = 0.01;
+        
+        OPTIONS
+        #InitialFile = "/home/paula/packedStageAirWater_Test.rlt";
+        DAESolver(File="dassl");
+        TimeStep = 10;
+        TimeEnd = 100;
+end