Ignore:
Timestamp:
Feb 8, 2007, 4:37:44 PM (16 years ago)
Author:
gerson bicca
Message:

testing new formulations for heat exchanger models

File:
1 edited

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  • branches/newlanguage/eml/heat_exchangers/HeatExchangerDetailed.mso

    r135 r160  
    340340        Outlet.Cold.z=Inlet.Cold.z;
    341341       
    342 "No Phase Change In Cold Stream"
    343         Inlet.Cold.v=Outlet.Cold.v;
    344 
    345 "No Phase Change In Hot Stream"
    346         Inlet.Hot.v=Outlet.Hot.v;
    347        
    348342end
    349343
    350 Model Heatex_Detailed          as HeatExchangerDetailed_Basic
     344Model Heatex_Detailed                           as HeatExchangerDetailed_Basic
    351345
    352346ATTRIBUTES
     
    358352PARAMETERS
    359353
    360 outer PP                as Plugin                (Brief="External Physical Properties");
    361                 side        as Integer           (Brief="Fluid Alocation Flag",Lower=0,Upper=1);
    362                 Pi                      as constant     (Brief="Pi Number",Default=3.14159265);
     354outer PP                as Plugin               (Brief="External Physical Properties");
     355        HotSide                 as Switcher     (Brief="Hot Side in the Exchanger",Valid=["shell","tubes"],Default="shell");
     356        Pi                              as constant    (Brief="Pi Number",Default=3.14159265);
     357       
     358        FlowRegime                      as Switcher     (Brief="Tube Side Flow Regime ",Valid=["laminar","transition","turbulent"],Default="laminar");
     359        LaminarCorrelation      as Switcher     (Brief="Heat Transfer Correlation in Laminar Flow",Valid=["Hausen","Schlunder"],Default="Hausen");
     360        TransitionCorrelation as Switcher       (Brief="Heat Transfer Correlation in Transition Flow",Valid=["Gnielinski","ESDU"],Default="Gnielinski");
     361        TurbulentCorrelation  as Switcher       (Brief="Heat Transfer Correlation in Turbulent Flow",Valid=["Petukhov","SiederTate"],Default="Petukhov");
     362
    363363#+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    364364#                               Shell Geometrical Parameters                                           
     
    428428        HE.Lcd                                  = Lcd;
    429429        HE.Ltd                                  = Ltd;
    430         side                                            = HE.FluidAlocation();
    431430       
    432431#"Tube Side Inlet Nozzle Area"
     
    457456EQUATIONS
    458457
    459 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    460 #                               Heat Transfer Correction Factors                                       
    461 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    462458"Ji Factor"
    463459        Shell.HeatTransfer.Ji = HE.JiFactor(Shell.HeatTransfer.Re);
     
    478474        Shell.HeatTransfer.Jtotal =     Shell.HeatTransfer.Jc*Shell.HeatTransfer.Jl*Shell.HeatTransfer.Jb*Shell.HeatTransfer.Jr*Shell.HeatTransfer.Js;
    479475
    480 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    481 #                               Pressure Drop and Velocities                                   
    482 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    483 
    484 if side equal 1
    485        
    486         then
     476#Cheking Flow Regime
     477switch FlowRegime
     478       
     479        case "laminar":
     480       
     481"Not Necessary in Laminar Correlation - Use any one equation that you want"
     482        Tubes.HeatTransfer.fi   = 16/Tubes.HeatTransfer.Re;
     483       
     484switch LaminarCorrelation
     485       
     486        case "Hausen":
     487
     488"Nusselt Number in Laminar Flow - Hausen Equation"
     489        Tubes.HeatTransfer.Nu = 3.665 + ((0.19*((Ditube/Ltube)*Tubes.HeatTransfer.Re*Tubes.HeatTransfer.PR)^0.8)/(1+0.117*((Ditube/Ltube)*Tubes.HeatTransfer.Re*Tubes.HeatTransfer.PR)^0.467));
     490       
     491        case "Schlunder":
     492       
     493"Nusselt Number in Laminar Flow - Schlunder Equation"
     494        Tubes.HeatTransfer.Nu = (49.027896+4.173281*Tubes.HeatTransfer.Re*Tubes.HeatTransfer.PR*(Ditube/Ltube))^(1/3);
     495
     496end
     497       
     498        when Tubes.HeatTransfer.Re > 2300 switchto "transition";
     499       
     500        case "transition":
     501       
     502"Friction Factor for use in Gnielinski Equation"
     503        Tubes.HeatTransfer.fi   = 1/(0.79*ln(Tubes.HeatTransfer.Re)-1.64)^2;
     504       
     505switch TransitionCorrelation
     506       
     507        case "Gnielinski":
     508       
     509"Nusselt Number in Transition Flow - Gnielinski Equation"
     510        Tubes.HeatTransfer.Nu*(1+(12.7*sqrt(0.125*Tubes.HeatTransfer.fi)*((Tubes.HeatTransfer.PR)^(2/3) -1))) = 0.125*Tubes.HeatTransfer.fi*(Tubes.HeatTransfer.Re-1000)*Tubes.HeatTransfer.PR;
     511
     512        case "ESDU":
     513       
     514"Nusselt Number in Transition Flow - ESDU Equation"
     515        Tubes.HeatTransfer.Nu =1;#to be implemented
     516       
     517end
     518
     519        when Tubes.HeatTransfer.Re < 2300 switchto "laminar";
     520        when Tubes.HeatTransfer.Re > 10000 switchto "turbulent";
     521
     522        case "turbulent":
     523
     524"Friction Factor in Petukhov Equation"
     525        Tubes.HeatTransfer.fi   = 1/(1.82*log(Tubes.HeatTransfer.Re)-1.64)^2;
     526
     527switch TurbulentCorrelation
     528       
     529        case "Petukhov":
     530       
     531"Nusselt Number in Turbulent Flow - Petukhov Equation"
     532        Tubes.HeatTransfer.Nu*(1.07+(12.7*sqrt(0.125*Tubes.HeatTransfer.fi)*((Tubes.HeatTransfer.PR)^(2/3) -1))) = 0.125*Tubes.HeatTransfer.fi*Tubes.HeatTransfer.Re*Tubes.HeatTransfer.PR;
     533       
     534        case "SiederTate":
     535
     536"Nusselt Number in Transition Flow - Sieder Tate Equation"
     537        Tubes.HeatTransfer.Nu = 0.027*(Tubes.HeatTransfer.PR)^(1/3)*(Tubes.HeatTransfer.Re)^(4/5);
     538
     539end
     540       
     541        when Tubes.HeatTransfer.Re < 10000 switchto "transition";
     542       
     543end
     544
     545switch HotSide
     546       
     547        case "shell":
     548       
     549"Shell Side Phi correction"
     550        Shell.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Hot.Average.Mu,Properties.Hot.Wall.Mu);
     551       
     552"Tube Side Phi correction"
     553        Tubes.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Cold.Average.Mu,Properties.Cold.Wall.Mu);
     554       
     555"Shell Side inlet Nozzle rho-V^2"
     556        Shell.PressureDrop.RVsquare_in = Properties.Hot.Inlet.rho*(Shell.PressureDrop.Vnozzle_in)^2;
     557
     558"Shell Side Outlet Nozzle rho-V^2"
     559        Shell.PressureDrop.RVsquare_out = Properties.Hot.Outlet.rho*(Shell.PressureDrop.Vnozzle_out)^2;
    487560       
    488561"Tube Side Pressure Drop"
     
    519592        Outlet.Cold.P  = Inlet.Cold.P - Tubes.PressureDrop.Pdtotal;
    520593
    521 
    522         else
     594"Hot Wall Temperature"
     595        Properties.Hot.Wall.Twall       = (Properties.Hot.Average.T+Properties.Cold.Average.T)/2;
     596
     597"ColdWall Temperature"
     598        Properties.Cold.Wall.Twall  = (Properties.Hot.Average.T+Properties.Cold.Average.T)/2;
     599
     600"Tube Side Velocity"
     601        Tubes.HeatTransfer.Vtube        = Properties.Cold.Inlet.Fw*Tpass/((Pi*Ditube*Ditube/4)*Properties.Cold.Average.rho*Ntt);
     602
     603"Tube Side Reynolds Number"
     604        Tubes.HeatTransfer.Re           = (Properties.Cold.Average.rho*Tubes.HeatTransfer.Vtube*Ditube)/Properties.Cold.Average.Mu;
     605       
     606"Tube Side Prandtl Number"
     607        Tubes.HeatTransfer.PR           = ((Properties.Cold.Average.Cp/Properties.Cold.Average.Mw)*Properties.Cold.Average.Mu)/Properties.Cold.Average.K;
     608
     609"Tube Side Prandtl Number at Wall Temperature"
     610        Tubes.HeatTransfer.PRw          = ((Properties.Cold.Wall.Cp/Properties.Cold.Average.Mw)*Properties.Cold.Wall.Mu)/Properties.Cold.Wall.K;
     611
     612"Tube Side Film Coefficient"
     613        Tubes.HeatTransfer.htube= (Tubes.HeatTransfer.Nu*Properties.Cold.Average.K/Ditube)*Tubes.HeatTransfer.Phi;
     614
     615"Shell Side Prandtl Number"
     616        Shell.HeatTransfer.PR           = ((Properties.Hot.Average.Cp/Properties.Hot.Average.Mw)*Properties.Hot.Average.Mu)/Properties.Hot.Average.K;
     617
     618"Shell Side Prandtl Number at Wall Temperature"
     619        Shell.HeatTransfer.PRw          = ((Properties.Hot.Wall.Cp/Properties.Hot.Average.Mw)*Properties.Hot.Wall.Mu)/Properties.Hot.Wall.K;
     620
     621
     622        case "tubes":
     623       
     624"Shell Side Phi correction"
     625        Shell.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Cold.Average.Mu,Properties.Cold.Wall.Mu);
     626       
     627"Tube Side Phi correction"
     628        Tubes.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Hot.Average.Mu,Properties.Hot.Wall.Mu);
     629       
     630"Shell Side inlet Nozzle rho-V^2"
     631        Shell.PressureDrop.RVsquare_in = Properties.Cold.Inlet.rho*(Shell.PressureDrop.Vnozzle_in)^2;
     632
     633"Shell Side Outlet Nozzle rho-V^2"
     634        Shell.PressureDrop.RVsquare_out = Properties.Cold.Outlet.rho*(Shell.PressureDrop.Vnozzle_out)^2;
    523635
    524636"Tube Side Pressure Drop"
     
    555667        Outlet.Cold.P  = Inlet.Cold.P - Shell.PressureDrop.Pdtotal;
    556668
    557 end
    558 
    559 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    560 #                               Nozzles rho-V^2                                                                 
    561 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    562 
    563 if side equal 1
    564        
    565         then
    566 
    567 "Shell Side inlet Nozzle rho-V^2"
    568         Shell.PressureDrop.RVsquare_in = Properties.Hot.Inlet.rho*(Shell.PressureDrop.Vnozzle_in)^2;
    569 
    570 "Shell Side Outlet Nozzle rho-V^2"
    571         Shell.PressureDrop.RVsquare_out = Properties.Hot.Outlet.rho*(Shell.PressureDrop.Vnozzle_out)^2;
    572        
    573         else
    574        
    575 "Shell Side inlet Nozzle rho-V^2"
    576         Shell.PressureDrop.RVsquare_in = Properties.Cold.Inlet.rho*(Shell.PressureDrop.Vnozzle_in)^2;
    577 
    578 "Shell Side Outlet Nozzle rho-V^2"
    579         Shell.PressureDrop.RVsquare_out = Properties.Cold.Outlet.rho*(Shell.PressureDrop.Vnozzle_out)^2;
    580 
    581 end
    582 
    583 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    584 #                               Phi correction                                                                 
    585 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    586 
    587 if side equal 1
    588        
    589         then
    590 
    591 "Shell Side Phi correction"
    592         Shell.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Hot.Average.Mu,Properties.Hot.Wall.Mu);
    593        
    594 "Tube Side Phi correction"
    595         Tubes.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Cold.Average.Mu,Properties.Cold.Wall.Mu);
    596        
    597         else
    598        
    599 "Shell Side Phi correction"
    600         Shell.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Cold.Average.Mu,Properties.Cold.Wall.Mu);
    601        
    602 "Tube Side Phi correction"
    603         Tubes.HeatTransfer.Phi  = HE.PhiCorrection(Properties.Hot.Average.Mu,Properties.Hot.Wall.Mu);
    604 
    605 end
    606 
    607 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#                                                                                                                                   #
    608 #                               Heat Transfer                                                                           
    609 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    610 
    611 if side equal 1
    612        
    613         then
    614        
    615 "Hot Wall Temperature"
    616         Properties.Hot.Wall.Twall       = (Properties.Hot.Average.T+Properties.Cold.Average.T)/2;
    617 
    618 "ColdWall Temperature"
    619         Properties.Cold.Wall.Twall  = (Properties.Hot.Average.T+Properties.Cold.Average.T)/2;
    620 
    621 "Tube Side Velocity"
    622         Tubes.HeatTransfer.Vtube        = Properties.Cold.Inlet.Fw*Tpass/((Pi*Ditube*Ditube/4)*Properties.Cold.Average.rho*Ntt);
    623 
    624 "Tube Side Reynolds Number"
    625         Tubes.HeatTransfer.Re           = (Properties.Cold.Average.rho*Tubes.HeatTransfer.Vtube*Ditube)/Properties.Cold.Average.Mu;
    626        
    627 "Tube Side Prandtl Number"
    628         Tubes.HeatTransfer.PR           = ((Properties.Cold.Average.Cp/Properties.Cold.Average.Mw)*Properties.Cold.Average.Mu)/Properties.Cold.Average.K;
    629 
    630 "Tube Side Prandtl Number at Wall Temperature"
    631         Tubes.HeatTransfer.PRw          = ((Properties.Cold.Wall.Cp/Properties.Cold.Average.Mw)*Properties.Cold.Wall.Mu)/Properties.Cold.Wall.K;
    632 
    633 "Tube Side Film Coefficient"
    634         Tubes.HeatTransfer.htube        = HE.TubeFilmCoeff(Tubes.HeatTransfer.Re,Tubes.HeatTransfer.PR,Properties.Cold.Average.K)*Tubes.HeatTransfer.Phi;
    635 
    636 "Shell Side Prandtl Number"
    637         Shell.HeatTransfer.PR           = ((Properties.Hot.Average.Cp/Properties.Hot.Average.Mw)*Properties.Hot.Average.Mu)/Properties.Hot.Average.K;
    638 
    639 "Shell Side Prandtl Number at Wall Temperature"
    640         Shell.HeatTransfer.PRw          = ((Properties.Hot.Wall.Cp/Properties.Hot.Average.Mw)*Properties.Hot.Wall.Mu)/Properties.Hot.Wall.K;
    641 
    642 
    643         else
    644 
    645669"Hot Wall Temperature"
    646670        Properties.Hot.Wall.Twall  = (Properties.Hot.Average.T+Properties.Cold.Average.T)/2;
     
    662686
    663687"Tube Side Film Coefficient"
    664         Tubes.HeatTransfer.htube= HE.TubeFilmCoeff(Tubes.HeatTransfer.Re,Tubes.HeatTransfer.PR,Properties.Hot.Average.K)*Tubes.HeatTransfer.Phi;
    665        
     688        Tubes.HeatTransfer.htube= (Tubes.HeatTransfer.Nu*Properties.Hot.Average.K/Ditube)*Tubes.HeatTransfer.Phi;
     689
    666690"Shell Side Prandtl Number"
    667691        Shell.HeatTransfer.PR = ((Properties.Cold.Average.Cp/Properties.Cold.Average.Mw)*Properties.Cold.Average.Mu)/Properties.Cold.Average.K;
     
    672696end
    673697
    674 
    675698"Tube Resistance"       
    676699        Resistances.Rtube*(Tubes.HeatTransfer.htube*Ditube) = Dotube;
     
    699722end
    700723
    701 Model Heatex_Detailed_NTU       as Heatex_Detailed
     724Model Heatex_Detailed_NTU                               as Heatex_Detailed
    702725
    703726ATTRIBUTES
     
    717740end
    718741
    719 Model Heatex_Detailed_LMTD as Heatex_Detailed
     742Model Heatex_Detailed_LMTD                      as Heatex_Detailed
    720743
    721744ATTRIBUTES
     
    767790end
    768791
    769 Model E_Shell_NTU_Det                   as Heatex_Detailed_NTU
     792Model Shell_and_Tubes_NTU_Det                   as Heatex_Detailed_NTU
    770793
    771794ATTRIBUTES
    772795        Pallete = true;
    773         Brief = "Shell and Tubes Heat Exchanger with 1 shell pass - NTU Method";
     796        Brief = "Shell and Tubes Heat Exchanger with 1 or 2 shell passes - NTU Method";
    774797        Info =
    775798        "write some information";
    776799       
    777800#+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
    778 #       Shell and Tubes Heat Exchanger with 1 shell pass - LMTD Method
    779 #+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
     801#       Shell and Tubes Heat Exchanger with 1 or 2 shell passes - LMTD Method
     802#+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++#
     803PARAMETERS
     804
     805        HotSide                 as Switcher     (Brief="Hot Side in the Exchanger",Valid=["shell","tubes"],Default="shell");
     806        ShellType        as Switcher    (Brief="TEMA Designation",Valid=["Eshell","Fshell"],Default="Eshell");
     807       
     808VARIABLES
     809
     810        Eft1    as positive (Brief="Effectiveness Correction",Lower=0.01,Upper=1,Default=0.5);
     811       
    780812EQUATIONS
    781813
     814switch ShellType
     815       
     816        case "Fshell":
     817       
     818"Effectiveness Correction for 2 pass shell side"
     819        Eft1 = 2*(1+Details.Cr+sqrt(1+Details.Cr^2)*((1+exp(-Details.NTU*sqrt(1+Details.Cr^2)))/(1-exp(-Details.NTU*sqrt(1+Details.Cr^2)))) )^-1;
     820
     821"TEMA F Shell Effectiveness"
     822        Eft = ( ((1-Eft1*Details.Cr)/(1-Eft1))^2 -1  )*( ((1-Eft1*Details.Cr)/(1-Eft1))^2 - Details.Cr )^-1;
     823
     824        case "Eshell":
     825       
    782826"TEMA E Shell Effectiveness"
    783 #       Eft = 2*(1+Details.Cr+sqrt(1+Details.Cr^2)*((1+exp(-Details.NTU*sqrt(1+Details.Cr^2)))/(1-exp(-Details.NTU*sqrt(1+Details.Cr^2)))) )^-1;
    784         Eft = HE.EshellEffectiveness(Details.Cr,Details.NTU);
     827        Eft     = 2*(1+Details.Cr+sqrt(1+Details.Cr^2)*((1+exp(-Details.NTU*sqrt(1+Details.Cr^2)))/(1-exp(-Details.NTU*sqrt(1+Details.Cr^2)))) )^-1;
     828
     829"Variable not in use when 1 Pass Shell Side"
     830        Eft1    = Eft;
     831       
     832end
     833
    785834
    786835"Js Factor"     
    787836        Shell.HeatTransfer.Js = HE.JsFactor(Shell.HeatTransfer.Re,Baffles.Lsi,Baffles.Lso,Baffles.Ls);
    788837
    789 if side equal 1
    790        
    791         then
     838switch HotSide
     839       
     840        case "shell":
    792841       
    793842"Shell Side Reynolds Number"
     
    807856
    808857
    809         else
     858        case "tubes":
    810859
    811860"Shell Side Reynolds Number"
     
    829878end
    830879
    831 Model F_Shell_NTU_Det                   as Heatex_Detailed_NTU
    832 
    833 ATTRIBUTES
    834         Pallete = true;
    835         Brief = "Shell and Tubes Heat Exchanger with 2 shell pass - NTU Method";
    836         Info =
    837         "write some information";
    838 
    839 VARIABLES
    840 
    841 Eft1    as positive (Brief="Effectiveness Correction",Lower=0.01,Default=0.5);
    842 
    843 EQUATIONS
    844 
    845 "Effectiveness Correction"
    846         Eft1 = 2*(1+Details.Cr+sqrt(1+Details.Cr^2)*((1+exp(-Details.NTU*sqrt(1+Details.Cr^2)))/(1-exp(-Details.NTU*sqrt(1+Details.Cr^2)))) )^-1;
    847 
    848 "TEMA F Shell Effectiveness"
    849         Eft = ( ((1-Eft1*Details.Cr)/(1-Eft1))^2 -1  )*( ((1-Eft1*Details.Cr)/(1-Eft1))^2 - Details.Cr )^-1;
    850 
    851 "Js Factor"     
    852         Shell.HeatTransfer.Js = HE.JsFactor(Shell.HeatTransfer.Re,Baffles.Lsi,Baffles.Lso,Baffles.Ls);
    853 
    854 if side equal 1
    855        
    856         then
    857        
    858 "Shell Side Reynolds Number"
    859         Shell.HeatTransfer.Re=(Dotube*Properties.Hot.Inlet.Fw/Shell.HeatTransfer.Sm)/Properties.Hot.Average.Mu;
    860 
    861 "Shell Heat Transfer Coefficient"
    862         Shell.HeatTransfer.hshell= Shell.HeatTransfer.Ji*(Properties.Hot.Average.Cp/Properties.Hot.Average.Mw)*(Properties.Hot.Inlet.Fw/Shell.HeatTransfer.Sm)*(Shell.HeatTransfer.PR^(-2/3))*Shell.HeatTransfer.Jtotal*Shell.HeatTransfer.Phi;
    863 
    864 "Shell Pressure Drop Cross Flow"
    865         Shell.PressureDrop.PdCross              = HE.DeltaPcross(Shell.HeatTransfer.Re,Baffles.Ls,Baffles.Lso,Baffles.Lsi,Properties.Hot.Inlet.Fw,Shell.HeatTransfer.Phi,Properties.Hot.Average.rho);
    866 
    867 "Shell Pressure Baffle Window"
    868         Shell.PressureDrop.Pdwindow             = HE.DeltaPwindow(Properties.Hot.Inlet.Fw,Shell.HeatTransfer.Sm,Properties.Hot.Average.rho,Properties.Hot.Average.Mu,Baffles.Ls);
    869 
    870 "Shell Pressure End Zones"
    871         Shell.PressureDrop.PdEndZones  = HE.DeltaPendZones(Shell.HeatTransfer.Re,Baffles.Ls,Baffles.Lso,Baffles.Lsi,Properties.Hot.Inlet.Fw,Shell.HeatTransfer.Phi,Properties.Hot.Average.rho);
    872 
    873 
    874         else
    875 
    876 "Shell Side Reynolds Number"
    877         Shell.HeatTransfer.Re=(Dotube*Properties.Cold.Inlet.Fw/Shell.HeatTransfer.Sm)/Properties.Cold.Average.Mu;
    878 
    879 "Shell Heat Transfer Coefficient"
    880         Shell.HeatTransfer.hshell=Shell.HeatTransfer.Ji*(Properties.Cold.Average.Cp/Properties.Cold.Average.Mw)*(Properties.Cold.Inlet.Fw/Shell.HeatTransfer.Sm)*(Shell.HeatTransfer.PR^(-2/3))*Shell.HeatTransfer.Jtotal*Shell.HeatTransfer.Phi;
    881 
    882 "Shell Pressure Drop Cross Flow"
    883         Shell.PressureDrop.PdCross      = HE.DeltaPcross(Shell.HeatTransfer.Re,Baffles.Ls,Baffles.Lso,Baffles.Lsi,Properties.Cold.Inlet.Fw,Shell.HeatTransfer.Phi,Properties.Cold.Average.rho);
    884 
    885 "Shell Pressure Baffle Window"
    886         Shell.PressureDrop.Pdwindow     = HE.DeltaPwindow(Properties.Cold.Inlet.Fw,Shell.HeatTransfer.Sm,Properties.Cold.Average.rho,Properties.Cold.Average.Mu,Baffles.Ls);
    887 
    888 "Shell Pressure End Zones"
    889         Shell.PressureDrop.PdEndZones  = HE.DeltaPendZones(Shell.HeatTransfer.Re,Baffles.Ls,Baffles.Lso,Baffles.Lsi,Properties.Cold.Inlet.Fw,Shell.HeatTransfer.Phi,Properties.Cold.Average.rho);
    890 
    891 
    892 end
    893 
    894 
    895 end
     880
     881
     882
     883
    896884
    897885Model Multipass_NTU_Det
     
    13061294        Info =
    13071295        "write some information";
     1296       
     1297PARAMETERS
     1298
     1299                HotSide         as Switcher     (Brief="Hot Side in the Exchanger",Valid=["shell","tubes"],Default="shell");
    13081300
    13091301EQUATIONS
     
    13211313        Shell.HeatTransfer.Js = HE.JsFactor(Shell.HeatTransfer.Re,Baffles.Lsi,Baffles.Lso,Baffles.Ls);
    13221314
    1323 if side equal 1
    1324        
    1325         then
     1315switch HotSide
     1316       
     1317        case "shell":
    13261318       
    13271319"Shell Side Reynolds Number"
     
    13411333
    13421334
    1343         else
     1335        case "tubes":
    13441336
    13451337"Shell Side Reynolds Number"
     
    13711363        "write some information";
    13721364
     1365PARAMETERS
     1366
     1367outer           HotSide         as Switcher     (Brief="Hot Side in the Exchanger",Valid=["shell","tubes"],Default="shell");
     1368
    13731369EQUATIONS
    13741370
     
    13851381        Shell.HeatTransfer.Js = HE.JsFactor(Shell.HeatTransfer.Re,Baffles.Lsi,Baffles.Lso,Baffles.Ls);
    13861382
    1387 if side equal 1
    1388        
    1389         then
     1383switch HotSide
     1384       
     1385        case "shell":
    13901386       
    13911387"Shell Side Reynolds Number"
     
    14051401
    14061402
    1407         else
     1403        case "tubes":
    14081404
    14091405"Shell Side Reynolds Number"
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