Changeset 477 for branches/packed/eml/stage_separators/tray.mso
 Timestamp:
 Mar 7, 2008, 3:46:44 PM (15 years ago)
 File:

 1 edited
Legend:
 Unmodified
 Added
 Removed

branches/packed/eml/stage_separators/tray.mso
r470 r477 365 365 rhoL as dens_mass; 366 366 rhoV as dens_mass; 367 uL as Real (Brief="volume flow rate of liquid, m^3/m^2/s", Default = 0.007);368 uV as Real (Brief="volume flow rate of vapor, m^3/m^2/s", Default = 1.14);367 uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Lower = 0, Default = 0.007); 368 uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Lower = 0, Default = 1.14); 369 369 dp as length (Brief="Particle diameter", Default=1e3); 370 370 invK as Real (Brief="Wall factor"); … … 661 661 end 662 662 663 663 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=1e3); 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 * (1e)/a; 770 771 "Wall Factor" 772 invK = (1 + (2*dp/(3*ds*(1e)))); 773 774 #* "Reynolds number of the vapor stream" 775 Rev*invK = dp*uV*rhoV / (miV*(1e)); 776 777 Qsio = Cpo * (64/Rev + 1.8/Rev^0.08); 778 if Rev > 1e4 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=1e3); 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 * (1e)/a; 898 899 "Wall Factor" 900 invK = (1 + (2*dp/(3*ds*(1e)))); 901 902 "Reynolds number of the vapor stream" 903 Rev*invK = dp*uV*rhoV / (miV*(1e)); 904 #* "Reynolds number of the liquid stream" 905 Rel = uL*rhoL / (a*miL); 906 907 if Rel < 5 then 908 if Rel < 1e4 then 909 ah = 0 * '1/m'; 910 else 911 "Hydraulic surface area" 912 ah = a * Ch * Rel^0.15 * (uL^2*a/g)^0.1; #(Rel^2*a^3*miL^2/rhoL^2/g)^0.1; # 913 end 914 else 915 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; # 916 end 917 *# 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
Note: See TracChangeset
for help on using the changeset viewer.