Changeset 493 for branches/packed


Ignore:
Timestamp:
Apr 4, 2008, 3:03:40 PM (15 years ago)
Author:
Paula Bettio Staudt
Message:

I am almost there

Location:
branches/packed
Files:
1 added
3 edited

Legend:

Unmodified
Added
Removed

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

    r477 r493  
    169169end
    170170
     171#*-------------------------------------------------------------------
     172* Model of a tray with reaction
     173*------------------------------------------------------------------*#
     174Model trayReact
     175        ATTRIBUTES
     176        Pallete         = false;
     177        Icon            = "icon/Tray";
     178        Brief           = "Model of a tray with reaction.";
     179        Info            =
     180"== Assumptions ==
     181* both phases (liquid and vapour) exists all the time;
     182* thermodymanic equilibrium with Murphree plate efficiency;
     183* no entrainment of liquid or vapour phase;
     184* no weeping;
     185* the dymanics in the downcomer are neglected.
     186       
     187== Specify ==
     188* the Feed stream;
     189* the Liquid inlet stream;
     190* the Vapour inlet stream;
     191* the Vapour outlet flow (OutletV.F);
     192* the reaction related variables.
     193       
     194== Initial ==
     195* the plate temperature (OutletL.T)
     196* the liquid height (Level) OR the liquid flow OutletL.F
     197* (NoComps - 1) OutletL compositions
     198";
     199
     200        PARAMETERS
     201        outer PP as Plugin(Type="PP");
     202        outer NComp as Integer;
     203        V as volume(Brief="Total Volume of the tray");
     204        Q as power (Brief="Rate of heat supply");
     205        Ap as area (Brief="Plate area = Atray - Adowncomer");
     206       
     207        Ah as area (Brief="Total holes area");
     208        lw as length (Brief="Weir length");
     209        g as acceleration (Default=9.81);
     210        hw as length (Brief="Weir height");
     211        beta as fraction (Brief="Aeration fraction");
     212        alfa as fraction (Brief="Dry pressure drop coefficient");
     213
     214        stoic(NComp) as Real(Brief="Stoichiometric matrix");
     215        Hr as energy_mol;
     216        Pstartup as pressure;
     217       
     218        VapourFlow as Switcher(Valid = ["on", "off"], Default = "off");
     219        LiquidFlow as Switcher(Valid = ["on", "off"], Default = "off");
     220       
     221        VARIABLES
     222in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
     223in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
     224in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
     225out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
     226out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
     227
     228        yideal(NComp) as fraction;
     229        Emv as Real (Brief = "Murphree efficiency");
     230
     231        M(NComp) as mol (Brief="Molar Holdup in the tray");
     232        ML as mol (Brief="Molar liquid holdup");
     233        MV as mol (Brief="Molar vapour holdup");
     234        E as energy (Brief="Total Energy Holdup on tray");
     235        vL as volume_mol (Brief="Liquid Molar Volume");
     236        vV as volume_mol (Brief="Vapour Molar volume");
     237        Level as length (Brief="Height of clear liquid on plate");
     238        Vol as volume;
     239       
     240        rhoL as dens_mass;
     241        rhoV as dens_mass;
     242        r3 as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
     243        C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1); #, Unit = "mol/l");
     244       
     245        EQUATIONS
     246        "Molar Concentration"
     247        OutletL.z = vL * C;
     248       
     249        "Reaction"
     250        r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4))*'l/mol/s';
     251       
     252        "Component Molar Balance"
     253        diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
     254                - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL;
     255       
     256        "Energy Balance"
     257        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
     258                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q ) + Hr * r3 * vL*ML;
     259       
     260        "Molar Holdup"
     261        M = ML*OutletL.z + MV*OutletV.z;
     262       
     263        "Energy Holdup"
     264        E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
     265       
     266        "Mol fraction normalisation"
     267        sum(OutletL.z)= 1.0;
     268       
     269        "Liquid Volume"
     270        vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
     271        "Vapour Volume"
     272        vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
     273
     274        "Thermal Equilibrium"
     275        OutletV.T = OutletL.T;
     276       
     277        "Mechanical Equilibrium"
     278        OutletV.P = OutletL.P;
     279       
     280        "Level of clear liquid over the weir"
     281        Level = ML*vL/Ap;
     282
     283        Vol = ML*vL;
     284       
     285        "Liquid Density"
     286        rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
     287        "Vapour Density"
     288        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
     289
     290        switch LiquidFlow
     291                case "on":
     292                "Francis Equation"
     293                OutletL.F*vL = 1.84*'1/s'*lw*((Level-(beta*hw)+1e-6*'m')/(beta))^2;
     294                when Level < (beta * hw) switchto "off";
     295               
     296                case "off":
     297                "Low level"
     298                OutletL.F = 0 * 'mol/h';
     299                when Level > (beta * hw) + 1e-6*'m' switchto "on";
     300        end
     301
     302        switch VapourFlow
     303                case "on":
     304                #InletV.P = OutletV.P + Level*g*rhoL + rhoV*alfa*(InletV.F*vV/Ah)^2;
     305                InletV.F*vV = sqrt((InletV.P - OutletV.P - Level*g*rhoL + 1e-8 * 'atm')/(rhoV*alfa))*Ah;
     306                when InletV.P < OutletV.P + Level*g*rhoL switchto "off";
     307               
     308                case "off":
     309                InletV.F = 0 * 'mol/s';
     310                when InletV.P > OutletV.P + Level*g*rhoL + 3e-2 * 'atm' switchto "on";
     311                #when InletV.P > OutletV.P + Level*beta*g*rhoL + 1e-2 * 'atm' switchto "on";
     312        end
     313
     314        "Chemical Equilibrium"
     315        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
     316                PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, yideal)*yideal;
     317       
     318        OutletV.z = Emv * (yideal - InletV.z) + InletV.z;
     319       
     320        sum(OutletL.z)= sum(OutletV.z);
     321       
     322        "Geometry Constraint"
     323        V = ML* vL + MV*vV;
     324end
     325       
    171326Model packedStage_Navaes as trayBasic
    172327        PARAMETERS
    … …  
    416571end
    417572
    418 #*-------------------------------------------------------------------
    419 * Model of a tray with reaction
    420 *------------------------------------------------------------------*#
    421 Model trayReact
    422         ATTRIBUTES
    423         Pallete         = false;
    424         Icon            = "icon/Tray";
    425         Brief           = "Model of a tray with reaction.";
    426         Info            =
    427 "== Assumptions ==
    428 * both phases (liquid and vapour) exists all the time;
    429 * thermodymanic equilibrium with Murphree plate efficiency;
    430 * no entrainment of liquid or vapour phase;
    431 * no weeping;
    432 * the dymanics in the downcomer are neglected.
    433        
    434 == Specify ==
    435 * the Feed stream;
    436 * the Liquid inlet stream;
    437 * the Vapour inlet stream;
    438 * the Vapour outlet flow (OutletV.F);
    439 * the reaction related variables.
    440        
    441 == Initial ==
    442 * the plate temperature (OutletL.T)
    443 * the liquid height (Level) OR the liquid flow OutletL.F
    444 * (NoComps - 1) OutletL compositions
    445 ";
    446 
     573Model packedStage
    447574        PARAMETERS
    448         outer PP as Plugin(Type="PP");
    449         outer NComp as Integer;
     575outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
     576outer NComp as Integer;
     577        PPwater as Plugin(Brief="Physical Properties",
     578                Type="PP",
     579                Components = [ "water" ],
     580                LiquidModel = "PR",
     581                VapourModel = "PR"
     582        );
     583
    450584        V as volume(Brief="Total Volume of the tray");
    451         Q as power (Brief="Rate of heat supply");
     585        Q as heat_rate (Brief="Rate of heat supply");
    452586        Ap as area (Brief="Plate area = Atray - Adowncomer");
    453        
    454         Ah as area (Brief="Total holes area");
    455         lw as length (Brief="Weir length");
    456         g as acceleration (Default=9.81);
    457         hw as length (Brief="Weir height");
    458         beta as fraction (Brief="Aeration fraction");
    459         alfa as fraction (Brief="Dry pressure drop coefficient");
    460 
    461         stoic(NComp) as Real(Brief="Stoichiometric matrix");
    462         Hr as energy_mol;
    463         Pstartup as pressure;
    464        
    465         VapourFlow as Switcher(Valid = ["on", "off"], Default = "off");
    466         LiquidFlow as Switcher(Valid = ["on", "off"], Default = "off");
    467        
     587
     588        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
     589        g as acceleration;
     590        e as Real (Brief="Void fraction of packing, m^3/m^3");
     591        ds as length (Brief="Column diameter");
     592        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
     593        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
     594        hs as length (Brief="Height of the packing stage");
     595
    468596        VARIABLES
    469597in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
    … …  
    473601out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
    474602
    475         yideal(NComp) as fraction;
    476         Emv as Real (Brief = "Murphree efficiency");
    477 
    478603        M(NComp) as mol (Brief="Molar Holdup in the tray");
    479604        ML as mol (Brief="Molar liquid holdup");
    … …  
    482607        vL as volume_mol (Brief="Liquid Molar Volume");
    483608        vV as volume_mol (Brief="Vapour Molar volume");
    484         Level as length (Brief="Height of clear liquid on plate");
    485         Vol as volume;
    486        
     609       
     610        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
     611        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
    487612        rhoL as dens_mass;
    488613        rhoV as dens_mass;
    489         r3 as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s');
    490         C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1); #, Unit = "mol/l");
    491        
     614       
     615        deltaP as pressure;
     616       
     617        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
     618        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
     619        dp as length (Brief="Particle diameter", Default=1e-3);
     620        invK as Real (Brief="Wall factor");
     621        Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
     622        Al as area;
     623        hl as Real (Brief="Column holdup", Unit='m^3/m^3');
     624        Qsil as Real (Brief="Resistance coefficient on the liquid load", Lower = 0);
     625
     626        SET
     627        Mw = PP.MolecularWeight();
     628
    492629        EQUATIONS
    493         "Molar Concentration"
    494         OutletL.z = vL * C;
    495        
    496         "Reaction"
    497         r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4))*'l/mol/s';
    498        
    499630        "Component Molar Balance"
    500631        diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
    501                 - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL;
    502        
     632                - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
     633
    503634        "Energy Balance"
    504635        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
    505                 - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q ) + Hr * r3 * vL*ML;
     636                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
    506637       
    507638        "Molar Holdup"
    … …  
    518649        "Vapour Volume"
    519650        vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
    520 
     651       
     652        "Chemical Equilibrium"
     653        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
     654                PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
     655       
    521656        "Thermal Equilibrium"
    522657        OutletV.T = OutletL.T;
    523658       
    524659        "Mechanical Equilibrium"
    525         OutletV.P = OutletL.P;
    526        
    527         "Level of clear liquid over the weir"
    528         Level = ML*vL/Ap;
    529 
    530         Vol = ML*vL;
     660        OutletL.P = OutletV.P;
     661       
     662        "Geometry Constraint"
     663        V*e = ML*vL + MV*vV;
    531664       
    532665        "Liquid Density"
    … …  
    534667        "Vapour Density"
    535668        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
    536 
    537         switch LiquidFlow
    538                 case "on":
    539                 "Francis Equation"
    540                 OutletL.F*vL = 1.84*'1/s'*lw*((Level-(beta*hw)+1e-6*'m')/(beta))^2;
    541                 when Level < (beta * hw) switchto "off";
    542                
    543                 case "off":
    544                 "Low level"
    545                 OutletL.F = 0 * 'mol/h';
    546                 when Level > (beta * hw) + 1e-6*'m' switchto "on";
     669        "Liquid viscosity"
     670        miL = PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
     671        "Vapour viscosity"
     672        miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
     673
     674        "Area occupied by the liquid"
     675        Al = ML*vL/hs;
     676
     677        "Volume flow rate of liquid, m^3/m^2/s"
     678        uL * Al = OutletL.F * vL;
     679        "Volume flow rate of vapor, m^3/m^2/s"
     680        uV * (Ap*e - Al) = OutletV.F * vV;
     681       
     682        "Liquid holdup"
     683        hl = ML*vL/V/e;
     684       
     685        "Particle diameter"
     686        dp = 6 * (1-e)/a;
     687       
     688        "Wall Factor"
     689        invK = (1 + (2*dp/(3*ds*(1-e))));
     690       
     691        "Reynolds number of the vapor stream"
     692        Rev*invK = dp*uV*rhoV / (miV*(1-e));
     693       
     694        deltaP = InletV.P - OutletV.P;
     695       
     696        "Pressure drop and Vapor flow"
     697        deltaP/hs  = Qsil*a*uV^2*rhoV*invK / (2*(e-hl)^3);
     698
     699        "Liquid holdup"
     700        hl = (12*miL*a^2*uL/rhoL/g)^1/3;
     701end
     702
     703Model packedStage_old
     704        PARAMETERS
     705outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
     706outer NComp as Integer;
     707        V as volume(Brief="Total Volume of the tray");
     708        Q as heat_rate (Brief="Rate of heat supply");
     709        Ap as area (Brief="Plate area = Atray - Adowncomer");
     710
     711        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
     712        g as acceleration;
     713        e as Real (Brief="Void fraction of packing, m^3/m^3");
     714        ds as length (Brief="Column diameter");
     715        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
     716        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
     717        hs as length (Brief="Height of the packing stage");
     718        Qsio as Real (Brief="Resistance coefficient", Lower = 0);
     719
     720        VARIABLES
     721in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
     722in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
     723in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
     724out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
     725out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
     726
     727        M(NComp) as mol (Brief="Molar Holdup in the tray");
     728        ML as mol (Brief="Molar liquid holdup");
     729        MV as mol (Brief="Molar vapour holdup");
     730        E as energy (Brief="Total Energy Holdup on tray");
     731        vL as volume_mol (Brief="Liquid Molar Volume");
     732        vV as volume_mol (Brief="Vapour Molar volume");
     733       
     734        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
     735        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
     736        rhoL as dens_mass;
     737        rhoV as dens_mass;
     738        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
     739        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
     740        dp as length (Brief="Particle diameter", Default=1e-3);
     741        invK as Real (Brief="Wall factor");
     742        Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
     743#       Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
     744#       Qsil as Real;
     745        Al as area;
     746        hl as Real (Brief="Column holdup", Unit='m^3/m^3');
     747#       hls as Real (Brief="Column holdup at loading point", Unit='m^3/m^3');
     748       
     749        SET
     750        Mw = PP.MolecularWeight();
     751
     752        EQUATIONS
     753        "Component Molar Balance"
     754        diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
     755                - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
     756#       diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
     757#       OutletL.z = OutletV.z;
     758
     759        "Energy Balance"
     760        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
     761                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
     762       
     763        "Molar Holdup"
     764        M = ML*OutletL.z + MV*OutletV.z;
     765       
     766        "Energy Holdup"
     767        E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
     768       
     769        "Mol fraction normalisation"
     770        sum(OutletL.z)= 1.0;
     771        #sum(OutletL.z)=sum(OutletV.z);
     772       
     773        "Liquid Volume"
     774        vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
     775        "Vapour Volume"
     776        vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
     777       
     778        "Chemical Equilibrium"
     779#       OutletV.z = OutletL.z;
     780        PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
     781                PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
     782       
     783        "Thermal Equilibrium"
     784        OutletV.T = OutletL.T;
     785       
     786        "Mechanical Equilibrium"
     787        OutletL.P = OutletV.P;
     788       
     789        "Geometry Constraint"
     790        V*e = ML*vL + MV*vV;
     791       
     792        "Liquid Density"
     793        rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
     794        "Vapour Density"
     795        rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
     796        "Liquid viscosity"
     797        miL = PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
     798        "Vapour viscosity"
     799        miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
     800       
     801        Al = ML*vL/hs;
     802
     803        "Volume flow rate of liquid, m^3/m^2/s"
     804        uL * Al = OutletL.F * vL;
     805        "Volume flow rate of vapor, m^3/m^2/s"
     806        uV * (Ap*e - Al) = OutletV.F * vV;
     807       
     808        "Liquid holdup and Liquid flow"
     809        hl = (12*miL*a^2*uL/rhoL/g)^1/3;
     810       
     811        "Liquid holdup"
     812        hl = ML*vL/V/e;
     813       
     814        "Particle diameter"
     815        dp = 6 * (1-e)/a;
     816       
     817        "Wall Factor"
     818        invK = (1 + (2*dp/(3*ds*(1-e))));
     819       
     820        "Reynolds number of the vapor stream"
     821        Rev*invK = dp*uV*rhoV / (miV*(1-e));
     822
     823#*      if Rev > 1e-4 then
     824                "Resistance Coefficient"       
     825                Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
     826        else
     827                Qsio = 1;
    547828        end
    548 
    549         switch VapourFlow
    550                 case "on":
    551                 #InletV.P = OutletV.P + Level*g*rhoL + rhoV*alfa*(InletV.F*vV/Ah)^2;
    552                 InletV.F*vV = sqrt((InletV.P - OutletV.P - Level*g*rhoL + 1e-8 * 'atm')/(rhoV*alfa))*Ah;
    553                 when InletV.P < OutletV.P + Level*g*rhoL switchto "off";
    554                
    555                 case "off":
    556                 InletV.F = 0 * 'mol/s';
    557                 when InletV.P > OutletV.P + Level*g*rhoL + 3e-2 * 'atm' switchto "on";
    558                 #when InletV.P > OutletV.P + Level*beta*g*rhoL + 1e-2 * 'atm' switchto "on";
     829       
     830#       "Liquid Holdup at loading point"
     831#       hls = (12*a^2*miL*uL/g/rhoL)^0.333;
     832
     833        if e-hl < 1e-4 then
     834                Qsil = 1e-3;
     835        else
     836                Qsil = Qsio * ((e-hl)/e)^1.5 * (hl/hl)^0.3 * exp(13300/'m^1.5'/a^1.5 * sqrt(uL^2*a/g));
    559837        end
    560 
     838*#
     839        "Pressure drop and Vapor flow"
     840        (InletV.P - OutletV.P)/hs  = Qsio*a*uV^2*rhoV*invK / (2*e^3);
     841        #(InletV.P - OutletV.P)/hs  = Qsil*a*uV^2*rhoV*invK / (2*(e-hl)^3);     
     842end
     843
     844# component #1 = nitrogen; #2 = water
     845Model packedStage_AirWater
     846        PARAMETERS
     847outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
     848outer NComp as Integer;
     849        V as volume(Brief="Total Volume of the tray");
     850        Q as heat_rate (Brief="Rate of heat supply");
     851        Ap as area (Brief="Plate area = Atray - Adowncomer");
     852
     853        a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
     854        g as acceleration;
     855        e as Real (Brief="Void fraction of packing, m^3/m^3");
     856        ds as length (Brief="Column diameter");
     857        Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
     858        Ch as Real (Brief="Constant for ah equation"); # Billet and Schultes, 1999.
     859        Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
     860        hs as length (Brief="Height of the packing stage");
     861        #Qsio as Real (Brief="Resistance coefficient", Lower = 0);
     862
     863        VARIABLES
     864in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
     865in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
     866in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
     867out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
     868out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
     869
     870        M(NComp) as mol (Brief="Molar Holdup in the tray");
     871        ML as mol (Brief="Molar liquid holdup");
     872        MV as mol (Brief="Molar vapour holdup");
     873        E as energy (Brief="Total Energy Holdup on tray");
     874        vL as volume_mol (Brief="Liquid Molar Volume");
     875        vV as volume_mol (Brief="Vapour Molar volume");
     876       
     877        miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
     878        miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
     879        rhoL as dens_mass;
     880        rhoV as dens_mass;
     881        uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
     882        uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
     883        dp as length (Brief="Particle diameter", Default=1e-3);
     884        invK as Real (Brief="Wall factor");
     885        Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
     886#       Rel as Real (Brief="Reynolds number of the liquid stream", Lower = 0, Default=100);
     887#       ah as Real (Brief="Hydraulic surface area", Unit='m^2/m^3');
     888        Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
     889#       Qsil as Real;
     890        Al as area;
     891#       hls as Real (Brief="Column holdup at loading point", Unit='m^3/m^3');
     892        hl as Real (Brief="Column holdup", Unit='m^3/m^3');
     893       
     894        SET
     895        Mw = PP.MolecularWeight();
     896
     897        EQUATIONS
     898        "Component Molar Balance"
     899        diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
     900
     901        "Energy Balance"
     902        diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
     903                - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
     904       
     905        "Molar Holdup"
     906        M = ML*OutletL.z + MV*OutletV.z;
     907       
     908        "Energy Holdup"
     909        E = ML*OutletL.h + MV*OutletV.h - OutletV.P*(V*e);
     910       
    561911        "Chemical Equilibrium"
    562         PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
    563                 PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, yideal)*yideal;
    564        
    565         OutletV.z = Emv * (yideal - InletV.z) + InletV.z;
    566        
    567         sum(OutletL.z)= sum(OutletV.z);
     912        OutletV.z = [1 0];
     913        OutletL.z = [0 1];
     914
     915        "Thermal Equilibrium"
     916        OutletV.T = OutletL.T;
     917       
     918        "Mechanical Equilibrium"
     919        OutletL.P = OutletV.P;
    568920       
    569921        "Geometry Constraint"
    570         V = ML* vL + MV*vV;
     922        V*e = ML*vL + MV*vV;
     923       
     924        "Liquid Density"
     925        rhoL = 999 * 'kg/m^3';#PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z); #
     926        "Vapour Density"
     927        rhoV = 1.19 * 'kg/m^3'; #PP.VapourDensity(InletV.T, InletV.P, InletV.z); #
     928        "Liquid viscosity"
     929        miL = 0.001 * 'kg/m/s' ; #PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z); #
     930        "Vapour viscosity"
     931        miV = 1.86e-5 * 'kg/m/s'; #PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
     932        "Liquid Volume"
     933        vL = 18 * 'g/mol' / rhoL; #PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z); #
     934        "Vapour Volume"
     935        vV = 28 * 'g/mol' / rhoV; #PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); #
     936
     937        "Cross section area ocupied by the liquid"
     938        Al = ML*vL/hs;
     939
     940        "Volume flow rate of liquid, m^3/m^2/s"
     941        uL * Al = OutletL.F * vL;
     942
     943        "Volume flow rate of vapor, m^3/m^2/s"
     944        uV * (Ap*e - Al) = OutletV.F * vV;
     945
     946        "Particle diameter"
     947        dp = 6 * (1-e)/a;
     948       
     949        "Wall Factor"
     950        invK = (1 + (2*dp/(3*ds*(1-e))));
     951       
     952        "Reynolds number of the vapor stream"
     953        Rev*invK = dp*uV*rhoV / (miV*(1-e));
     954
     955        "Liquid Holdup"
     956        hl = vL * ML / (V*e);
     957       
     958#       "Liquid Holdup at loading point"
     959#       hls = (12*a^2*miL*uL/g/rhoL)^0.333;
     960       
     961        "Liquid holdup and Liquid flow"
     962        hl = (12*miL*a^2*uL/rhoL/g)^1/3; # * (ah/a)^1;
     963       
     964        if Rev < 1e-4 then
     965                Qsio = 1;
     966        else
     967                "Resistance Coefficient"
     968                Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
     969        end
     970       
     971#*      if e-hl < 1e-4 then
     972                Qsil = 1e-3;
     973        else
     974                Qsil = Qsio * ((e-hl)/e)^1.5 * (hl/hl)^0.3 * exp(13300/'m^1.5'/a^1.5 * sqrt(uL^2*a/g));
     975        end
     976*#
     977        "Pressure drop and Vapor flow"
     978        #(InletV.P - OutletV.P)/hs  = Qsio*a*uV^2*rhoV*invK / (2*e^3);
     979        #(InletV.P - OutletV.P)/hs  = Qsil*a*uV^2*rhoV*invK / (2*(e-hl)^3);
     980        (InletV.P - OutletV.P)/hs  = Qsio*a*uV^2*rhoV*invK / (2*(e-hl)^3);
    571981end
    572982
    … …  
    6561066#       N = 6400 * '1/m^3';
    6571067
    658         OPTIONS
    659         GuessFile = "/home/paula/test.rlt";
    660        
    6611068end
    6621069
    663 Model packedStage
    664         PARAMETERS
    665 outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
    666 outer NComp as Integer;
    667         V as volume(Brief="Total Volume of the tray");
    668         Q as heat_rate (Brief="Rate of heat supply");
    669         Ap as area (Brief="Plate area = Atray - Adowncomer");
    670 
    671         a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
    672         g as acceleration;
    673         e as Real (Brief="Void fraction of packing, m^3/m^3");
    674         ds as length (Brief="Column diameter");
    675         Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
    676         Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
    677         hs as length (Brief="Height of the packing stage");
    678         Qsio as Real (Brief="Resistance coefficient", Lower = 0);
    679 
    680         VARIABLES
    681 in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
    682 in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
    683 in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
    684 out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
    685 out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
    686 
    687         M(NComp) as mol (Brief="Molar Holdup in the tray");
    688         ML as mol (Brief="Molar liquid holdup");
    689         MV as mol (Brief="Molar vapour holdup");
    690         E as energy (Brief="Total Energy Holdup on tray");
    691         vL as volume_mol (Brief="Liquid Molar Volume");
    692         vV as volume_mol (Brief="Vapour Molar volume");
    693        
    694         miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
    695         miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
    696         rhoL as dens_mass;
    697         rhoV as dens_mass;
    698         uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
    699         uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
    700         dp as length (Brief="Particle diameter", Default=1e-3);
    701         invK as Real (Brief="Wall factor");
    702 #       Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
    703 #       Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
    704         Al as area;
    705        
    706         SET
    707         Mw = PP.MolecularWeight();
    708 
    709         EQUATIONS
    710         "Component Molar Balance"
    711         diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
    712                 - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
    713 #       diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
    714 #       OutletL.z = OutletV.z;
    715 
    716         "Energy Balance"
    717         diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
    718                 - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
    719        
    720         "Molar Holdup"
    721         M = ML*OutletL.z + MV*OutletV.z;
    722        
    723         "Energy Holdup"
    724         E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
    725        
    726         "Mol fraction normalisation"
    727         sum(OutletL.z)= 1.0;
    728         sum(OutletL.z)=sum(OutletV.z);
    729        
    730         "Liquid Volume"
    731         vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
    732         "Vapour Volume"
    733         vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
    734        
    735         "Chemical Equilibrium"
    736 #       OutletV.z = OutletL.z;
    737         PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
    738                 PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
    739        
    740         "Thermal Equilibrium"
    741         OutletV.T = OutletL.T;
    742        
    743         "Mechanical Equilibrium"
    744         OutletL.P = OutletV.P;
    745        
    746         "Geometry Constraint"
    747         V*e = ML*vL + MV*vV;
    748        
    749         "Liquid Density"
    750         rhoL = PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
    751         "Vapour Density"
    752         rhoV = PP.VapourDensity(InletV.T, InletV.P, InletV.z);
    753         "Liquid viscosity"
    754         miL = PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
    755         "Vapour viscosity"
    756         miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
    757        
    758         Al = ML*vL/hs;
    759 
    760         "Volume flow rate of liquid, m^3/m^2/s"
    761         uL * Al = OutletL.F * vL;
    762         "Volume flow rate of vapor, m^3/m^2/s"
    763         uV * (Ap*e - Al) = OutletV.F * vV;
    764        
    765         "Liquid holdup and Liquid flow"
    766         vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;
    767        
    768         "Particle diameter"
    769         dp = 6 * (1-e)/a;
    770        
    771         "Wall Factor"
    772         invK = (1 + (2*dp/(3*ds*(1-e))));
    773        
    774 #*      "Reynolds number of the vapor stream"
    775         Rev*invK = dp*uV*rhoV / (miV*(1-e));
    776 
    777         Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
    778         if Rev > 1e-4 then
    779                 "Resistance Coefficient"       
    780                 Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
    781         else
    782                 Qsio = 1;
    783         end
    784 *#
    785         "Pressure drop and Vapor flow"
    786         (InletV.P - OutletV.P)/hs  = Qsio*a*uV^2*rhoV*invK / (2*e^3);
    787 end
    788 
    789 # component #1 = nitrogen; #2 = water
    790 Model packedStage_AirWater
    791         PARAMETERS
    792 outer PP as Plugin(Brief = "External Physical Properties", Type="PP");
    793 outer NComp as Integer;
    794         V as volume(Brief="Total Volume of the tray");
    795         Q as heat_rate (Brief="Rate of heat supply");
    796         Ap as area (Brief="Plate area = Atray - Adowncomer");
    797 
    798         a as Real (Brief="surface area per packing volume", Unit='m^2/m^3');
    799         g as acceleration;
    800         e as Real (Brief="Void fraction of packing, m^3/m^3");
    801         ds as length (Brief="Column diameter");
    802         Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999.
    803         Ch as Real (Brief="Constant for ah equation"); # Billet and Schultes, 1999.
    804         Mw(NComp)       as molweight    (Brief = "Component Mol Weight");
    805         hs as length (Brief="Height of the packing stage");
    806         #Qsio as Real (Brief="Resistance coefficient", Lower = 0);
    807 
    808         VARIABLES
    809 in      Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}");
    810 in      InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}");
    811 in      InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}");
    812 out     OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}");
    813 out     OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}");
    814 
    815         M(NComp) as mol (Brief="Molar Holdup in the tray");
    816         ML as mol (Brief="Molar liquid holdup");
    817         MV as mol (Brief="Molar vapour holdup");
    818         E as energy (Brief="Total Energy Holdup on tray");
    819         vL as volume_mol (Brief="Liquid Molar Volume");
    820         vV as volume_mol (Brief="Vapour Molar volume");
    821        
    822         miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s');
    823         miV as viscosity (Brief="Vapor dynamic viscosity", DisplayUnit='kg/m/s');
    824         rhoL as dens_mass;
    825         rhoV as dens_mass;
    826         uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = -10, Default = 0.007);
    827         uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = -10, Default = 1.14);
    828         dp as length (Brief="Particle diameter", Default=1e-3);
    829         invK as Real (Brief="Wall factor");
    830         Rev as Real (Brief="Reynolds number of the vapor stream", Lower = 0, Default=100);
    831 #       Rel as Real (Brief="Reynolds number of the liquid stream", Lower = -10, Default=100);
    832 #       ah as Real (Brief="Hydraulic surface area", Unit='m^2/m^3');
    833         Qsio as Real (Brief="Resistance coefficient", Lower = 0, Default=100);
    834         Al as area;
    835        
    836         SET
    837         Mw = PP.MolecularWeight();
    838 
    839         EQUATIONS
    840         "Component Molar Balance"
    841 #       diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z
    842 #               - OutletL.F*OutletL.z - OutletV.F*OutletV.z;
    843         diff(sum(M))=Inlet.F + InletL.F + InletV.F - OutletL.F - OutletV.F;
    844 
    845         "Energy Balance"
    846         diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h
    847                 - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q );
    848        
    849         "Molar Holdup"
    850         M = ML*OutletL.z + MV*OutletV.z;
    851        
    852         "Energy Holdup"
    853         E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V;
    854        
    855 #       "Mol fraction normalisation"
    856 #       sum(OutletL.z)= 1.0;
    857 #       sum(OutletL.z)=sum(OutletV.z);
    858        
    859         "Chemical Equilibrium"
    860         OutletV.z = [1 0];
    861         OutletL.z = [0 1];
    862 #       PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z =
    863 #               PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
    864        
    865         "Thermal Equilibrium"
    866         OutletV.T = OutletL.T;
    867        
    868         "Mechanical Equilibrium"
    869         OutletL.P = OutletV.P;
    870        
    871         "Geometry Constraint"
    872         V*e = ML*vL + MV*vV;
    873        
    874         "Liquid Density"
    875         rhoL = 999 * 'kg/m^3';#PP.LiquidDensity(OutletL.T, OutletL.P, OutletL.z);
    876         "Vapour Density"
    877         rhoV = 1.19 * 'kg/m^3'; #PP.VapourDensity(InletV.T, InletV.P, InletV.z);
    878         "Liquid viscosity"
    879         miL = 0.001 * 'kg/m/s' ; #PP.LiquidViscosity(OutletL.T, OutletL.P, OutletL.z);
    880         "Vapour viscosity"
    881         miV = PP.VapourViscosity(InletV.T, InletV.P, InletV.z);
    882         "Liquid Volume"
    883         vL = 18 * 'g/mol' / rhoV; #PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z);
    884         "Vapour Volume"
    885         vV = 28 * 'g/mol' / rhoL; #PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z);
    886 
    887         "Cross section area ocupied by the liquid"
    888         Al = ML*vL/hs;
    889 
    890         "Volume flow rate of liquid, m^3/m^2/s"
    891         uL * Al = OutletL.F * vL;
    892 
    893         "Volume flow rate of vapor, m^3/m^2/s"
    894         uV * (Ap*e - Al) = OutletV.F * vV;
    895 
    896         "Particle diameter"
    897         dp = 6 * (1-e)/a;
    898        
    899         "Wall Factor"
    900         invK = (1 + (2*dp/(3*ds*(1-e))));
    901        
    902         "Reynolds number of the vapor stream"
    903         Rev*invK = dp*uV*rhoV / (miV*(1-e));
    904 #*      "Reynolds number of the liquid stream"
     1070#*
     1071        "Reynolds number of the liquid stream"
    9051072        Rel = uL*rhoL / (a*miL);
    9061073
    … …  
    9151082                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; #
    9161083        end
     1084       
     1085
    9171086*#     
    918 #       if ah equal 0 then
    919 #               uL = 0 * 'm/s';
    920 #       else
    921                 "Liquid holdup and Liquid flow"
    922                 vL * ML = V * (12*miL*a^2*uL/rhoL/g)^1/3; # * (ah/a)^1;
    923 #       end
    924        
    925         "Resistance Coefficient"       
    926         Qsio = Cpo * (64/Rev + 1.8/Rev^0.08);
    927 
    928         "Pressure drop and Vapor flow"
    929         (InletV.P - OutletV.P)/hs  = 3*Qsio*a*uV^2*rhoV*invK / (2*e^3);
    930 end

  • branches/packed/sample/stage_separators/sample_column.mso

    r477 r493  
    554554        reb.T = 325 * 'K';
    555555        reb.z = [0.16, 0.542, 0.013, 0.008, 0.277];
    556        
     556
     557        sec.stage.Qsil = 0.1;
     558        #sec.stage(1).OutletV.F = 150 * 'kmol/h';
     559        sec.stage.deltaP = 0.0001 * 'atm';
     560
    557561        SET
    558562        sec.H = 4 * 'm';
    … …  
    564568        sec.stage.e = 0.951;
    565569        sec.stage.a = 112.6 * 'm^2/m^3';
    566         sec.stage.Qsio = 0.8;
    567570
    568571        INITIAL

  • branches/packed/sample/stage_separators/sample_tray.mso

    r477 r493  
    369369        inV.z = [0.0584, 0.9416];#[0.5, 0.5];#
    370370       
    371         t1.OutletV.P = 145 * 'kPa';
     371        #t1.OutletV.P = 145 * 'kPa';
     372        t1.OutletV.F = 190 * 'kmol/h';
     373        t1.Qsil = 10;
    372374       
    373375        SET
    … …  
    381383        t1.a = 112.6 * 'm^2/m^3';
    382384        t1.hs = 0.4 * 'm';
    383         t1.Qsio = 1;
    384385       
    385386        INITIAL
    … …  
    410411
    411412        VARIABLES
    412         deltaP as Real (Unit='inH2O/m*mm/in');
     413        deltaP as Real (Unit='atm/m'); #(Unit='inH2O/m*mm/in');
    413414        phiL as Real;
    414415       
    … …  
    444445        inV.z = [0.265, 0.233, 0.150, 0.014, 0.338];
    445446       
    446         #t1.OutletV.P = 2.305 * 'atm';
    447         #t1.OutletV.F = 165 * 'kmol/h';
     447        #t1.deltaP = 0.01 * 'atm';
     448        t1.OutletV.F = 165 * 'kmol/h';
     449        t1.Qsil = 10;
    448450       
    449451        SET
    … …  
    462464        t1.hs = 1 * 'ft';
    463465        t1.ds = 2.26 * 'ft';
    464         t1.Qsio = 100;
    465466
    466467        INITIAL
    … …  
    472473        DAESolver(File="sundials");
    473474        #InitialFile = "/home/paula/tray_Test_2.rlt";
    474         TimeStep = 0.01;
    475         TimeEnd = 10;
     475        TimeStep = 10;
     476        TimeEnd = 100;
    476477end
    477478
    … …  
    491492        VARIABLES
    492493        deltaP as Real (Unit='inH2O/m*mm/in');
    493         phiL as Real;
    494494       
    495495        DEVICES
    … …  
    506506        EQUATIONS
    507507        deltaP = (t1.InletV.P - t1.OutletV.P)/t1.hs;
    508         phiL = t1.vL * t1.ML/t1.V;
    509508
    510509        SPECIFY
    511510        feed.Outlet.F = 0 * 'kmol/h';
    512         feed.Outlet.T = 300 * 'K';
     511        feed.Outlet.T = 293 * 'K';
    513512        feed.Outlet.P = 1 * 'atm';
    514513        feed.Outlet.z = [0 1];
    515514
    516         inL.F = 71.21 * 'kmol/h';       
     515        inL.F = 100 * 'kmol/h'; #71.21 * 'kmol/h';     
    517516        inL.P = 1 * 'atm';
    518517        inL.T = 293 * 'K';
    … …  
    520519
    521520        inV.F = 175.3 * 'kmol/h';
    522         inV.P = 1.06 * 'atm';
     521        inV.P = 1.1 * 'atm';
    523522        inV.T = 295 * 'K';
    524523        inV.z = [1 0];
    525524       
    526         t1.OutletV.P = 1.05 * 'atm';
     525        t1.OutletV.P = 1.08 * 'atm';
    527526       
    528527        SET
    … …  
    540539
    541540        INITIAL
    542         t1.OutletL.T = 294 *'K';
    543         t1.ML = 0.0002 * 'kmol';
    544         t1.OutletL.z(1) = 0.01;
     541        t1.OutletL.T = 293 *'K';
     542        t1.ML = 0.002 * 'kmol';
    545543       
    546544        OPTIONS
Note: See TracChangeset for help on using the changeset viewer.