ࡱ>  ~  !"#$%&'()*+,-./0123456789:;<=>?@ABCDEFGHIJKLMNOPQRSTUVWXYZ[\]^_`abcdefghijklmnopqrstuvwxyz{|}~Root Entry F`8+>`Workbook]{N_VBA_PROJECT_CUR"[;َ?`?VBAَ?I?  !#$%&'()*+,-/0123456789:;<=>?@ABCDEFGHIJKLMNOPQRSTUVWXYZ[\]^`abcdeghjklmnopqrstuvwxyz{|}~ ,"4@ ,!"0@  $@  @  "0@ , $@ ,!"0@ *  * $ @ * $ * $ "|@ @ ,  (@@  (@  (@  ( " "0  ` " "   " "+ "    ` !0@  ` "0  @ "8 "8"@ @ "8"@ "8"@ "0" @ "0"@ @  (@ !0@@ "x@ @ , "x@ @, "x@ , "|@ , "p + "p+  `@  `  @   "p  "t+ ! " " "x "8@@ "8@ "8"@ @ "0 @ "0 "8@ " !" "x ,"4@ ,"4@ 83ffff̙3f3fff3f3f33333f33333\`' LPS ColumnD MPS Columnb HPS ColumnLPS ExchangersݮMPS ExchangersHPS Exchangers  Summary LPSI! Summary MPS7 Summary  I\pChristopher Haslego [Ba=  ThisWorkbook=hL,<"@"1Arial1Arial1Arial1Arial1Arial1Arial1Arial1Arial1Arial1.Times New Roman1.Times New Roman1.Times New Roman1.Times New Roman1.Times New Roman1Symbol1.Times New Roman1.Times New Roman1.Times New Roman1.Times New Roman1.Times New Roman1Arial1Arial1Arial1Arial1Arial1Arial1.Times New Roman"$"#,##0_);\("$"#,##0\)!"$"#,##0_);[Red]\("$"#,##0\)""$"#,##0.00_);\("$"#,##0.00\)'""$"#,##0.00_);[Red]\("$"#,##0.00\)7*2_("$"* #,##0_);_("$"* \(#,##0\);_("$"* "-"_);_(@_).))_(* #,##0_);_(* \(#,##0\);_(* "-"_);_(@_)?,:_("$"* #,##0.00_);_("$"* \(#,##0.00\);_("$"* "-"??_);_(@_)6+1_(* #,##0.00_);_(* \(#,##0.00\);_(* "-"??_);_(@_)0.0 "$"#,##0#,##0.0_);\(#,##0.0\)GB_("$"* #,##0.000000_);_("$"* \(#,##0.000000\);_("$"* "-"??_);_(@_)=8_("$"* #,##0.0_);_("$"* \(#,##0.0\);_("$"* "-"??_);_(@_) 0.000 0.0000                + ) , *      (@@  @   @  @   "0 "8 "0@ "4   @   "p   " "4 "4 #0@  @@ "t  @0 "t 0  @ "t  0 "t 1  ! "  "  "  " " "| "| !" "\ "x  "x  "x "x@ @, "x "x@ , "x@ , "|  "x "|  "| !"t   # ,  ,!  !  #  A  ,  A 8@ @ 8@ @ 8@ @  @ @ , $@ @  "0@ @  "0@@  @ , $@  "0@  "0@ HPS 8 jb( 3  @@  i Heat ExchangersHPS ExchangersUnitTypeEquipment Design Shell SideUtilityCWReboilerFloatingHeat Duty (MJ/h)Temperature In (C)Medium LPSHPSTemperature Out (C)Phase gasMPSPressure (kPa) Cost ($/GJ) Area (m)Utility Cost ($)liquidCost ($) Condenser Fixed T/SC1C2C3Fixed T/S & Floating HeadShell >10 bargShell <10 bargLPS Exchangers(Distillation Column Pricing (LPS Column)"Inputs that vary with each column:)Inputs that vary with each run of column: Ttop (0C) Tbot (0C)Theoretical tray= Actual trays=Vapor Velocity (m/s)=Vapor Flow (kg/h)=Vapor Flow (m3/s)= Reboiler Duty (MJ/h)=IRelative Volatility of Key Component=(top volatility x bot volatility)0.5FCond Duty (MJ/h)=Reb. Area (m2)=  Viscosity of Feed (cp)=Cond. Area (m2)=  Efficiency= Reflux Ratio=Density of Vapor (kg/m3)= Diameter (m)="Reboiler Utility Inlet Temp. (0C)=Tray Spacing (in)=check floodingCond. Utility Inlet Temp. (0C)= Length (m)=K1=K2=K3=Column Press (barg)=Flooding Calculations Data:Feed Density (kg/m3)=Liq Density at bottom (kg/m3)=NPV=Flowrate of Distillate (kg/hr)=Flowrate of Bottoms (kg/hr)=Flowrate of Feed (kg/h)=Cost of ManufacturingFCI = COL =CUT =CWT =CRM =COMd =NPV =Year InvestmentdkFCIL-SdkRCOMd  Cash FlowCumulative Cash Flow--(Distillation Column Pricing (MPS Column)(Distillation Column Pricing (HPS Column)$calculate this value for your systemReturned Values3Green cells are entered, white cells are calculated4Yellow cells are entered, white cells are calculatedCoefficient forMaterial Factors:Column: SS Clad=2.5SS = 4.0 Ni Clad = 4.5Ni = 9.8 Ti Clad = 4.9 Ti = 10.6 Enter number:Trays:SS = 2.0Ni-alloy = 5.0Installed Cost of Vessel=Installed Cost of Trays=Installed Cost of Reboiler=Installed Cost of Condenser=Annual Cost of Steam=Annual Cost of CW=Net Present Value = Cond. Utility Outlet Temp. 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(? "?0?? "(7> ,!8R7687"87P8(87 7  $6 , #,H -48-1-4P-4h-*1-N-,1.N-(18.N`.*1x.N.*1.N.,1/N8/(1P/Nx/ 1/N/ 1/N/$11N00&181N`1*1x1N1(11N1*12N02 1H2Nh2*12N2.12N2&13N83$1P3Nx3(13N3(13N3 &8H94091H94h94919(1 :N9$1H:N:$1p:N:$1:N:"1:N;*10;N`;(1x;N;,1;N;.1<N0<(1H<Np<01<N<$1<N< G9G9G-G0 >> ( "  ""8+4@N`NxeP+e+'(N0NHN`NxN '1'8'10@'H8`x'8'8'8  '(1H`'h1'1 .N> @+H08>`>X+x>0=N@>X(+pN>,+ N > ,+8 h Np > (+  N > &+!(!T@6+PAAN0!>H!:+`!!N!>!,+!"N">(",+@"p"Nx">"(+0"N">"(+"#N#>(#.+@#p# x# M#&j#&j#&j$&j($(jP$(jx$(j$(j$(j$(j%(j@% h%"  "0"884@N(N`e P+  e8 +H'NxNNNN '1'8 '18H'08h'P8'H8'8 '`1('10'1 .N> @+0 >=X+>(=N(>( (+x p N@>@ ,+ X N> ,+0 ` NX> (+` h N> &+h  T@6+??Np> :+  N>@ ,+( N> ,+XX N>@(+X` N>(+ N>.+  M &j@&j &j&j (j(j (j(j(j(jX (jp  "  "0  ""8,4NN0eHP+hhe+&NNNN N8 'P1p'8'1('8'8(@'H8`x'8 '1'1('01H` .hN>@+0>=X+==N>(+(N0>H,+`N>,+N>(+0XN`>x&+T`@6+@@N>:+0N8>P,+hN>,+N> (+8N@>X(+pN>.+  M(&j@&jh&j&j(j(j(j0(jX(j(j(j  "`? "  +x+++++0+H   8+H+h+x 8,-P, h,4, ,  " P? Axll v!fb6+2 LPS Column %hB@J x!fC6+2B@0 z!fD12+2 |!fD15+2P ( !fF16+2 !fF18+2 !fD13+2IlH Row 1, Col 1 B@umn.Ad Row 1, Col 2 ,  (ol 3SS Clad B@l ( (oft Carbon Steel ( Carbon Steel , Carbon Steel B@ Row 2, Col 2 , Row 2, Col 3 ,D Row 3, Col 1 B@rro Row 3, Col 2 ,Populate MOCColumn ComboBox ( Carbon Steel B@osoft SS Clad B@ (Ti Clad B@m Ti B@lll Carbon Steel B@l0SS Clad B@ll(Ni Clad B@m  (umn.SS B@Populate MOCTrays ComboBox (tem Carbon Steel B@olumn.SS B@Ni-alloy B@n.` LPS Column !fD18+2 e !fSS Cladj7+2hX !fSS@j7+2h hhj7+2h !fNi:\WI@j7+2lbhh#@j7+2yh !fTi@j7+2DOhX333333%@j7+2h(  !f Carbon Steel@ !fNi Clad !fTi Clad !f Carbon SteelP&Jj15+2 !fSSj15+2 !fNi-alloyj15+2'Place values for each run of the columnPlace values for each column !fJ28+2Di !fN5+2 !fN10+2t !fN11+2ra !fN14+210 !fN16+2 !fN21+2tNi B@SS Clad B@ !fJ25+26 !fJ26+21llphlImport Results to FormN15$2Fixed$ 8(f h` !fJ27+2Te !fJ29+2 Carbon Steel B@arbon SS B@Ni Clad B@adNi B@Ti Clad B@adTi B@ N6$2 2(f") =0  N13$2Fixed$ 6(f$$N17$2Fixed$ :(fE22$2Currency$ >(fc6$2d16$2 fE26$2Currency$ `(f b6$2c6$2 @CThe top temperature entered is greater than the bottom temperature!A@h D18$2hx j25$2j26$2umhhhh( Please Enter a Feed Density!A@j27$2umj28$2Please Enter a Bottoms Density!A@j29$2$hhhPlease Enter a Distillate Flow!A@Please Enter a Bottoms Flow!A@3There seems to be a error in your material balance!A@h j28$2j27$2 j29$2 3There seems to be a error in your material balance!A@n10$2tohhPlease Enter a Feed Flow!A@n11$2tohhn5$2-Please Enter the Number of Theoretical Trays!A@Please Enter the Reboiler Duty!A@n14$2to Please Enter the Condenser Duty!A@n16$2toPlease Enter a Reflux Ratio!A@Please Enter a Tray Spacing!A@n21$2!Please Enter the Column Pressure!A@XN12$2Fixed$ 4(f hE27$2Currency$ R(fhE25$2Currency$ \(fhE24$2Currency$ F(fhE23$2Currency$ B(fhPlease Enter a Reflux Ratio!A@Please Enter a Reflux Ratio!A@X MPS Column v!fb6+2lE21$2Currency$ <(fPlace values for each column MPS Column %hB@J x!fC6+2b6$2c6$2 CThe top temperature entered is greater than the bottom temperature!A@c6$2d16$2 z!fD12+2 |!fD15+2 !fF16+2 !fF18+2 !fD13+2 !f Carbon Steelj7+2 !fSS Clad@j7+2 !fSSj7+2 !fNi Clad@j7+2hH !fNi#@j7+2h !fTi Clad@j7+2h !fTi333333%@j7+2h !f Carbon Steelj15+2h` !fSSj15+2h( !fNi-alloyj15+2h 'Place values for each run of the column !fD18+2D18$2hX !fJ25+2j25$2Please Enter a Feed Density!A@h !fJ26+2j26$2Please Enter a Bottoms Density!A@h !fJ27+2j27$2Please Enter a Distillate Flow!A@h( !fJ28+2j28$2Please Enter a Bottoms Flow!A@h !fJ29+2j29$2Please Enter a Feed Flow!A@hh !fN5+2n5$2-Please Enter the Number of Theoretical Trays!A@h !fN10+2n10$2Please Enter the Reboiler Duty!A@h !fN11+2n11$2 Please Enter the Condenser Duty!A@h !fN14+2n14$2h !fN16+2n16$2Please Enter a Tray Spacing!A@hX !fN21+2n21$2!Please Enter the Column Pressure!A@hImport Results to FormN6$2 2(fN12$2Fixed$ 4(fN13$2Fixed$ 6(fN15$2Fixed$ 8(fN17$2Fixed$ :(fE21$2Currency$ <(fE22$2Currency$ >(fE23$2Currency$ B(fE24$2Currency$ F(fE25$2Currency$ \(fE26$2Currency$ `(fE27$2Currency$ R(flX HPS ColumnPlace values for each column HPS Column %hB@J v!fb6+2 x!fC6+2b6$2c6$2 CThe top temperature entered is greater than the bottom temperature!A@hc6$2d16$2 hH z!fD12+2 |!fD15+2 !fF16+2 !fF18+2 !fD13+2 !f Carbon Steelj7+2h !fSS Clad@j7+2h` !fSSj7+2h0 !fNi Clad@j7+2h !fNi#@j7+2h !fTi Clad@j7+2h !fTi333333%@j7+2hP !f Carbon Steelj15+2h !fSSj15+2h !fNi-alloyj15+2h'Place values for each run of the column !fD18+2D18$2h !fJ25+2j25$2Please Enter a Feed Density!A@h !fJ26+2j26$2Please Enter a Bottoms Density!A@h@ !fJ27+2j27$2Please Enter a Distillate Flow!A@h" !fJ28+2j28$2Please Enter a Bottoms Flow!A@h! !fJ29+2j29$2Please Enter a Feed Flow!A@hX! !fN5+2n5$2-Please Enter the Number of Theoretical Trays!A@h !fN10+2n10$2Please Enter the Reboiler Duty!A@hx !fN11+2n11$2 Please Enter the Condenser Duty!A@h !fN14+2n14$2h !fN16+2n16$2Please Enter a Tray Spacing!A@hH !fN21+2n21$2!Please Enter the Column Pressure!A@hImport Results to FormN6$2 2(fN12$2Fixed$ 4(fN13$2Fixed$ 6(fN15$2Fixed$ 8(fN17$2Fixed$ :(fE21$2Currency$ <(fE22$2Currency$ >(fE23$2Currency$ B(fE24$2Currency$ F(fE25$2Currency$ \(fE26$2Currency$ `(fE27$2Currency$ R(fl'A@x'  %!TowersC@ p!B@ FB@0 Calculations UserForm_OpenC@-C@&HelpShowHelpC@ &Examples CopyExamplesC@n@&n8&Towers7!&The bottom temperature you've specified is too high the the type of reboiler utility you have chosen! Column should be priced using a higher reboiler utilityA@The bottom temperature you've specified is too high the the type of reboiler utility you have chosen! Column should be priced using a higher reboiler utilityA@The bottom temperature you've specified is too high the the type of reboiler utility you have chosen! Column should be priced using a higher reboiler utilityA@(hl8) !!XAdding a new Workbook !!.( p!hB@Jbo p!B@P) Tower Results (F0* Tower Results (0  Tower Results$( 0   Tower Results$( 0! Tower Resultslt 0  s 0 we 0! Tower ResultsiThere is already an output sheet named Tower Results, what would you like to name the next results sheet?$ '  0(hThere is already an output sheet named Tower Results, what would you like to name the old results sheet?$ '((XAdding a new Workbook !!. Tower Results (l++,Tower Pricing.xla$B@fTower Pricing.xla$B@f,Open a workspace !!XAdding a new Workbook !!.,`, Prepare WorksheetPlace data on Worksheet pB@fInputsa1$2(.(0a1$2!.(0nt Ta1$2(@ Va2:a30$2(@ hb2:b30$2(@ v!fb2$2( x!fb3$2(,Top Temperature (0C)=a2$2(d2:d30$2!fB@4Bottom Temperature (0C)=a3$2(Relative Volatility=a4$2( z!fb4$2(Vapor Density (kg/m3)=a5$2( |!fb5$2(Reboiler HTC (W/m2 K)=a6$2( !fb6$2(Condenser HTC (W/m2 K)=a7$2( !fb7$2(Feed Viscosity (cP)=a8$2( !fb8$2( Column MOC=a9$2( !fb9$2( Tray MOC=a10$2( !fb10+2H,e2:e30$2!fB@40 !fb11+2n 4Please Enter a Condenser Utiltiy Outlet Temperature!A@4Please Enter a Condenser Utility Outlet Temperature!A@4Please Enter a Condenser Utility Outlet Temperature!A@0Feed Flow (kg/h)=a11+2DC-1Bottoms Flow (kg/h)=a12+2Ca !fb12+2rFDistillate Flow (kg/h)=a13+2entLef !fb13+2ntFeed Density (kg/m3)=a14+2 !fb14+2tiBottom Density (kg/m3)=a15+2MSForm !fb15+2z Reflux Ratio=a16+2 !fb16+2#CColumn Pressure (barg)=a17+2ms 2.0 !fb17+2Cond Utility Out Temp (0C)=a18+2E0 !fb18+245Theorectical Trays=a19+2Fo !fb19+2s Tray Spacing (in)=a20+2M !fb20+2OReboiler Duty (MJ/h)=a21+2 !fb21+22.Condenser Duty (MJ/h)=a22+2 !fb22+2ftX. pB@fJB@ 0! Tower ResultshThere is already an output sheet named Tower Results, what would you like to name the old results sheet?$ '  Tower Results$(33 0! Tower ResultshThere is already an output sheet named Tower Results, what would you like to name the old results sheet?$ '  Tower Results$(2  Tower Results$(hThere is already an output sheet named Tower Results, what would you like to name the old results sheet?$ ' 0! Tower Results 0! Tower Results Tower Results (heets. z (1 pB@f 0! Tower Results p!B@lr p!B@J s Tower Results (what w p!B@JtihThere is already an output sheet named Tower Results, what would you like to name the old results sheet?$ 's"Z \! z p!B@'Enter a name for the results worksheet:$ 'zAThere is already a sheet by that name, please enter another name:$ 'z48(Tower Pricing.xla$B@fla").A9 !B@9 \ h`9 Place output values on worksheetd1$2!.(0 Td1$2(@Inputsd1$2( Vd2:d30$2(@ he2:e30$2(@a2:a30$2!fB@4b2:b30$2!fB@4Outputsd1+2 2!fe2+2ual 4!fe3+2Actual Number of Trays=d2+2Reboiler Area (m2)=d3+2Condenser Area (m2)=d4+2 6!fe4+2Column Diamter (m)=d5+2 8!fe5+2Column Length (m)=d6+2 :!fe6+2Installed Cost of Vessel=d7+2 <!fe7+2Installed Cost of Trays=d8+2 >!fe8+2Installed Cost of Reboiler=d9+2 B!fe9+2Installed Cost of Condenser=d10+2 F!fe10+2Annual Cost of Steam=d11+2 \!fe11+2Annual Cost of Cooling Water=d12+2 `!fe12+2Net Present Value=d13+2 R!fe13+24h=hh*Unidentified Error, Please Re-Enter ValuesA@A@<D18$2- r(LThe Condenser Utility Outlet Temperature Must Not Exceed 45 degrees Celsius!A@D18$2- LThe Condenser Utility Outlet Temperature Must Not Exceed 45 degrees Celsius!A@D18$2- LThe Condenser Utility Outlet Temperature Must Not Exceed 45 degrees Celsius!A@(<>> 0!lB@>&l FB@%l>d B@F(> 0B@F EnterZ3 15772aE B@A@  112874082778>H)Error in Material Balance, Please RecheckA@Rahj29$2j27$2N14$2j27$2 j28$2 0?j29$2j27$2N14$2j27$2 j28$2 )Error in Material Balance, Please RecheckA@Ih?j29$2j27$2N14$2j27$2 j28$2 )Error in Material Balance, Please RecheckA@h0?(?Attribute VB_Name = "Tow er" Basp0{C8C4C7A4-AB48-11D2-B302-703352C10}J 60J CreatabliFalse PredeHclaIdTru "Expose@TemplateDeriv%CustomizD P# Sub Coefficients_Click() Estims.Show8End Sh@utdownndOutputDim TiBtAs Sng On Error GoTo Reset 'p Workshe Exc@el.ActCWC%(uUtZi? t2F =K1CEJ1`)gore@rcal % ST 20+*Spacin`g (inZ DT'-d+ReDCDuty (MJ/+2sR-+'B?ikb2C8pour 8sqv~jd o$jto>od2:dlhtoe2:eߊo!svdT~Bup NumbVo*f!eA!"d ?A (m2 !eCRd4?("eSCd>6Diam(mCCe ,<"$Length 3C>InstallAeCost `Vessel5eIl;"oRYI"d=OyIg wyI<"Ann&5SteamzsA=+;CoolaHW0>rt++NevtZV CNT#utoFi.?>@JQ: .LPS.SetFocQБ  HPS'@QTQec 1s(3png.xlaPThi~s Sel hVb36϶VCBTemperature.Text If Range("b6") >4c4ThenMsg@Box ("$ top t entered i@s grea thane b ottom \!")SEnd If xd1[ you've specifitoo highGthe type of reboiler ut ility hachosen! Column should be pric+using a+ $ qD12= RVola95VDelnsHFCoeffici8CD13BFVisco `MO@A< = "Carbon SteelL" ,j7B1 EsRSS Clad2.5W4Ni4DNi9.8 T  9 10.6ErTrays&r1#O.9SSd2MkNi-alloy8@ 'Place values for each runwycs gӤ_]D1"IFPlease Eá@|Condq|U@vtiy Outlet | > 45(hJ a Must Not Exce de #Cel0sius$#J2;F j""F = B/Bs ÒFDis`6`ySj2`g FlowcKFdpj2PP9ú2Ta}, (&+N14p *U) + p)O1("ErBr?in Mial Balance, RecheckvҌN/T'H=nFpNumb @P0poretic0  N102RDuty? n??pR_U1RC_4n1__PIo!DRo 0_W(Refluxp"8tioCTSxpac_RE ӿ^Aa  _T2PressߴSnTOOBr%pImport Results@ Form Ab( ;`qAat:N, "FixedQ4CPDiame@g@NLenxgth`XIVelECurrency I{E2@4/#*v0?3-lA`amGWNNVC9 Sub Priv LPS_Click(ߐِ&PO@WorkbooksowRp8xla").Actb This.Sheet SelecPc+= TC.@8.pre>;ەo0 iv핵have chosen! Column should be priced using a higher reboil utility") End If Range("D12") = RVolaR.T(ext@5@VDensG F16>CoefficPient !8!C!D13!FViscoc Ifx MO9x+T"Carbon Steel" ThLenlhj7&1 u"SS Clad 2.5!4Ni?4?DNi9.8 T  9 10.6ErTrays&r1CNrKSSQ!20Ni-alloyX 'Place values for each run of thBHDTemperature?@ ""MsgBox ("Please Enteza@ndq`UCv Outlet: ! ~ > |45(h j @ Must Not` Exce degre#Cel0siusJ2;F늫j"F BBottom s ÒFDis`6`@j2`g FlowcKFdPj2PP9ú2T#`; MF <> (M#*+N14* ) + ")bErr~in Mapial Balance, sRechecjkTN^TGn#!FNumb @G:oretic0  ~N102`RDuty?n?~HNRU_5U1RC_Dn1__@VCoOoקRo = ~a R efluxp"tioCTSpac_RE ^^] _T2Press/fSnTOBr%pI mportsults to Form A?b(d `qArLeaat:N, "FixezdQ4CPDiame@g@NLength`XIVlelEC@urrencI{E2@4/#*v0?3-lA`amG>WNNVC9 "qSubPriv& xt1_=icQ_D*to(p t erqPis 0cancbr>kfd"   you'Psp ecifi3 toodtype ___i___x1_-__ӕ_>_ If MOCColumn.Text = "Carbon Steel" Then  Range@("j7")1 End If SS Clad2.5=R4;Ni~4~Ni?9.8@T@9!@10.6ATrays&1f5KSSQ!20Ni-all oyX 'Place values for each run of the cª D180CTemperature?@ ""MsgBox ("Please Enter a CondensUtility Outlet H!")EÁ> 45H" Must Not Exceeddegre@GCelsius!, (M#*+N14* ) + )bErr~in M7rial Balance, sRechXeck-o$ N^T;Gn#!BNumb@uore8tic` 5AN10b2RDutyr2n$bRebo\il 1C#ROo~= RRativon$_W Refluxp"ÇN1CTSpacing_RE ^^ _T2Press/f}SnTlS %pImportsults to Form A(2eaqAreaQat;N12"), "Fixed4C3DiamegNqLength'XIVelECurrency I{E2s5/#*0?3Nl AyamPHW!ONVC9 SSub#Priv  U`q_IniBt@Wize(Dimde AsH VaXnt'pPopuuÀmFP%p'`%:%"$ p,)tp6`P1:%t'`%:%"$ t,t5`Nt! t l>FP%p'`%:%"$ p,)tp6`P1:%t'`%:%"$ t,t5`Nt! t l>FP%p'`%:%"$ p,)tp6`P1:%t'`%:%"$ t,t5`Nt! t l>FP%p'`%:%"$ p,)tp6`P1:%t'`%:%"$ t,t5`Nt! t l>FP%p'`%: %"$ p,)tp6`P1:!%t'`%:"%"$ t,t5`Nt! t l>FP%p'`%:#%"$ p,)tp6`P1:$%t'`%:%%"$ t,t5`Nt! t l>FP%p'`%:&%"$ p,)tp6`P1:'%t'`%:(%"$ t,t5`Nt! t )>FP%p'`%:*%"$ p,)tp6`P1:+%t'`%:,%"$ t,t5`Nt! t )>FP%p'`%:-%"$ p,)tp6`P1:.%t'`%:/%"$ t,t5`Nt! t l>FP%p'`%:0%"$ p,)tp6`P1:1%t'`%:2%"$ t,t5`Nt! t l>FP%p'`%:3%"$ p,)tp6`P1:4%t'`%:5%"$ t,t5`Nt! t l>FP%p'`%:6%"$ p,)tp6`P1:7%t'`%:8%"$ t,t5`Nt! t l>FP%p'`%:9%"$ p,)tp6`P1::%t'`%:;%"$ t,t5`Nt! t l>FP%p'`%:<%"$ p,)tp6`P1:=%t'`%:>%"$ t,t5`Nt! t l>FP%p'`%:?%"$ p,)tp6`P1:@%t'`%:A%"$ t,t5`Nt! t l>FP%p'`%:B%"$ p,)tp6`P1:C%t'`%:D%"$ t,t5`Nt! t l>FP%p'`%:E%"$ p,)tp6`P1:F%t'`%:G%"$ t,t5`Nt! $t l>FP%p'`%:H%"$ p,)tp6`P1:I%t'`%:J%"$ t,t5`Nt! ,t l>FP%p'`%:K%"$ p,)tp6`P1:L%t'`%:M%"$ t,t5`Nt! 4t l>FP%p'`%:N%"$ p,)tp6`P1:O%t'`%:P%"$ t,t5`Nt! <t l>FP%p'`%:Q%"$ p,)tp6`PHc%t'`%:R%"$ taP pp,`)tp6`P4%t'`%:R%"$ t,t5`1: %t'`%:R%"$ t,t5`4%t'`%:S%"$ t,t5`4%t'`%:T%"$ t,t5`1:U%t'`%:R%"$ t,t5`1:V%t'`%:W%"$ t,t5`Nt! 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VBAProjectF=C:\PROGRAM FILES\COMMON FILES\MICROSOFT SHARED\VBA\VBA332.DLLVBA  PF 3C:\Program Files\Microsoft Office\Office\EXCEL8.OLBExcel )`0FC:\WINDOWS\SYSTEM\stdole2.tlbstdole 1ypDDESTC:\WINDOWS\SYSTEM\MSForms.TWDMSForms ) !Q& !Q I 1 p- !Q3 !Q. !Q2 !Q/ !Q i 1 RDutyMOCColumn_Active6 !Q; !Q7 !Q: !Q8 !Q 1 MOCColumn_Open> !QD !Q? !QC !Q@ !Q !" 1  SS Ni Clad Ni Ti Clad TiH !QN !QT !QY !QU !QX !QV !Q Y$ 1 P LPS_Intializeb !Qg !Qc !Qf !Qd !Q % 1 j !Qp !Qk !Qo !Ql !Q & 1 MOCColumn_Intializes !Qy !Qt !QLabel22x !Qu !Q 1( 1 | !Q  !Q  !Q  !Q  !Q  !Q  !Q ) 1 0LPS_Initialize  !Q  !Q  !Q  !Q  !Q * 1 h  !Q  !Q  !Q  !Q  !Q , 1 UserForm_InitializeUserForm_Click  !Q  !Q  !Q  !Q  !QLabel9Label10MOCTrays  !Q - 1 MOCTrays_Change  Ni-alloy  !Q C6 D12 D15 F16 F18 D13 j7  !Q 2.5  !Q  !Q  !Q  !Q j15Tower  !Qp  !Q  !Qo  !QLabel11Label12FFeedLabel13FBottomsLabel14 FDistillateLabel15FDensityLabel16BDensityLabel17RRatioLabel18 CPressureLabel19 CTemperatureLabel20TTraysLabel21TSpacingLabel25n  !Q !4 1 Label27Label28Label29Label31Label30ATraysRAreaCArea CDiameterCLengthIVesselITraysLabel32 IReboilerLabel33 ICondenserLabel34CSteamLabel35CWaterLabel36NValueCommandButton2Label26 ATrays_Change Label28_Click Label31_Click ` D18 J25 J26 J27 J28 J29 N5 N10 N11 N14 N16 N21 N6Text N12 N13 N15 N17v  !Qu  !Q LPS_Click  !Q  !Q  !Q  !Q  !Q  !Q !; 1 pHPS  !Q  !Q  !Q  !Q  !Q Y< 1   !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q  !Q E21 E22 E23 E24 E25 E27  !Q  !Q  !Q  !Q  !Q A 1 H)  !Q/  !Q*  !Q.  !Q-  !Q )B 1 8  !Q<  !Q9  !Q;  !Q:  !Q IC 1 +e@ !QSheet939e@ !QRangeFe@ !QƏYl|Le@ !QUe@ !QMe@ !Q e@ !QTe@ !QNe@ !Q iE 1 Xe@ !Q ATrays CArea CDiameterme@ !Q ASteamue@ !Q|e@ !Qve@ !Q{e@ !Qze@ !Q n11&f@ !Q G 1 0ASteamAWatere@ !Qe@ !Q VBA332.DLL H @ &&&&.&e@ !Q &&&.& '$'&&&&&e@ !Q $&&&&&e@ !Q $&&&&&&&e@ !Q c6 HS X Please Enter a Distillate Flow!# CThe top temperature entered is greater than the bottom temperature!e@ !Qe@ !Q  "Please Enter a Column Temperature!e@ !Q j25 Please Enter a Feed Density! j26 Please Enter a Bottoms Density! j27 j28Sheet92 Please Enter a Bottoms Flow! j29 3There seems to be a error in your material balance!e@ !Qe@ !Q Please Enter a Feed Flow! n5 -Please Enter the Number of Theoretical Trays! n10 Please Enter the Reboiler Duty!Sheet91 Please Enter the Condenser Duty! n14 Please Enter a Refluex Ratio! n16 Please Enter a Tray Spacing! n21 !Please Enter the Column Pressure!e@ !Q $&&&&&&&&&&&& $&&&&&&&&&&&e@ !Q d16%f@ !Q+f@ !Q4 eThe bottom temperature you've specified is too high the the type of reboiler utility you have chosen!f@ !Q &&&& &&&f@ !Qf@ !Qf@ !Qf@ !Qf@ !Q Z 1  Label17_Click Currencyf@ !Q FixedSheet90*f@ !Q'f@ !Q 1\ 1  HPS_Click MPS_Click MPS Column HPS ColumnX]_ !QW]_ !QThisWorkbook_OpenK]_ !QV]_ !QL]_ !Q@]_ !QU]_ !QN]_ !Q ^ 1 0  AddMenuItemf]_ !Qe]_ !Qj]_ !Qi]_ !QFdFeF TowersfFgF Calculations UserForm_Open Windowp]_ !Qo]_ !QTowerFormb]_ !Qr]_ !Qc]_ !Qq]_ !Qd]_ !Q b 1 Module1 \)c!Q[)c!QK)c!Q`)c!QQ The bottom temperature you've specified 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Column should be priced using a higher reboiler utilityn)c!Qu)c!Qo)c!Q@)c!Qt)c!QOutputs)c!QSheet89 g 1  Output_Click d Tower Results{)c!Q Please Enter a Reflux Ratio!SheetsAdd WorkbooksCount Adding a new WorkbookFSheet10Sheet11)c!Q)c!QNameSheet12)c!Q)c!QSheet13)c!Q)c!Q)c!Q)c!Q)c!Q)c!Q,*c!Q+*c!Q0*c!Q/*c!Q:*c!Q9*c!QE*c!QD*c!Q=*c!QH*c!Q>*c!QG*c!Q?*c!Q n 1 0 L*c!QK*c!QW*c!QV*c!Qo*c!Q|*c!Q{*c!Q*c!Q*c!Q New worksheet added*c!Q*c!Q*c!Q*c!Q*c!Q HT 0 6 iThere is already an output sheet named Tower Results, what would you like to name the next results sheet?Sheet20*c!Q*c!Q*c!Q*c!Q*c!Q*c!Q*c!Q NewName*c!Q*c!Q*c!Q*c!Q+c!Q+c!Q+c!Q+c!Q*c!Q+c!Q+c!Q+c!Qv+c!Q+c!Q+c!Q w 1 6 hThere is already an output sheet named Tower Results, what would you like to name the old results sheet?+c!Q+c!Q#+c!Q,+c!Q++c!Q6+c!Q5+c!QW+c!QV+c!Q Workbook_Openc+c!Qe+c!Q y{ 1  Label20_Click+c!Q+c!Qe!Q Tower Pricing.xlse!Qe!Qe!Qe!Q Tower PricingActivate Tower Pricing.xla+e!Q!Q!Q !Q!Q!Q !Q !Q  1 x.!Q!Q!Q!Q a1MF Specifications for Column Spec InputsFontBold!Q!Q!Q !Q!Q!Q ɂ 1  Center TextAlign TextAlignment b9Center Alignment a2:a30 Top Temperature a2 ExpandToFit!Q!Q!Q!Q!Q م 1 0 a b2:b30 Top Temperature (0C)=!!Q b2*!Q3!Q Column MOC= a9 Bottom Temperature (0C)= a3 b3 Relative Volatility= a4 b4 Vapor Density (kg/m3)= a5 b5 Reboiler HTC (W/m2 K)= a6 Condenser HTC (W/m2 K)= a7 b7 Feed Viscosity (cP)= a8 b8 Tray MOC= a10 b10=!Q 4Please Enter a Condenser Utility Outlet Temperature! 4Please Enter a Condenser Utiltiy Outlet Temperature! Feed Flow (kg/h)= a11 b11 Bottoms Flow (kg/h)= a12 b12!Q!Q Distillate Flow (kg/h)= a13 b13 Feed Density (kg/m3)= a14 b14 Bottom Density (kg/m3)= a15 b15 Reflux Ratio= a16 b16 Column Pressure (barg)= a17 b17 Cond Utility Out Temp (0C)= a18 b18 Theorectical Trays= a19 b19 Tray Spacing (in)= a20 b20 Reboiler Duty (MJ/h)= a21 b21 Condenser Duty (MJ/h)= a22 b22Sheet14Q!QSheet15]!Q\!Q_!QSheet16Sheet17Sheet18 SheetNameSheet19!QSheet21!Q!QSheet22 ActiveSheetsSheet23!QSheet24!QSheet25Sheet26!Q!Q!QSheet27!QSheet28!QSheet29Sheet30!Q!Q!Q!Q!Q!Q!Q!Q !Q!Q !Q !Q !Q !Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!!QSheet88 !Q*!Q)!Q&!QSheet31Sheet32Sheet33Sheet34Sheet35Sheet36Sheet37Sheet38Sheet39Sheet40Sheet41Sheet42Sheet43Sheet44Sheet45Sheet46Sheet47Sheet48Sheet49Sheet50Sheet51Sheet52Sheet53Sheet54Sheet55Sheet56Sheet57Sheet58Sheet59Sheet60Sheet61Sheet62l!Qk!Qu!QSheet63Sheet64!Q 'Enter a name for the results worksheet: %There is already a sheet by that nameSheet65Sheet66Sheet67Sheet68Sheet69Sheet70Sheet71Sheet72Sheet73Sheet74Sheet75Sheet76Sheet77Sheet78Sheet79Sheet80Sheet81Sheet82Sheet83Sheet84Sheet85Sheet86Sheet87Sheet94Sheet95Sheet96Sheet97Sheet98Sheet99Sheet100Sheet101Sheet102Sheet103Sheet104Sheet105Sheet106Sheet107Sheet108Sheet109Sheet110Sheet111Sheet112Sheet113Sheet114Sheet115Sheet116Sheet117Sheet118Sheet119Sheet120Sheet121Sheet122Sheet123Sheet124Sheet125Sheet126Sheet127Sheet128Sheet129Sheet130R!QSheet131Sheet132!Q!Q!QSheet133!Q!Q!QSheet134!Q!QSheet135!Q!Q!QSheet136!Q!Q!Q!Q!Q!Q 1 Sheet137!Q!QSheet138!Q!QSheet139!Q!QModule2Macro3 Sheet59!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q !Q !Q !Q !Q!Q !Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q!Q !Q!Q"!Q!!Q$!Q#!Q&!Q%!Qh!Qg!Qr!Q+ƣQ7RfƣQ7R,ƣQ7R ƣQ7ReƣQ7R-ƣQ7R a 1 iƣQ7RhƣQ7RlƣQ7RkƣQ7RoƣQ7RnƣQ7RrƣQ7RqƣQ7RxƣQ7RwƣQ7RzƣQ7RƣQ7RƣQ7RƣQ7RƣQ7RƣQ7R" AThere is already a sheet by that name, please enter another name:ƣQ7Rn{'R d1 d2:d30 e2:e30 Outputs Actual Number of Trays= d2 e2 Reboiler Area (m2)= d3 e3 Condenser Area (m2)= d4 e4 Column Diamter (m)= d5 e5 Column Length (m)= d6 e6 Installed Cost of Vessel= d7 e7 Installed Cost of Trays= d8 e8 Installed Cost of Reboiler= d9 e9 Installed Cost of Condenser= d10 e10 Annual Cost of Steam= d11 e11 Annual Cost of Cooling Water= d12 e12 Net Present Value= d13 e13n{'Rn{'Rn{'Rn{'Rn{'Rn{'Rn{'R 1 0Errorn{'Rn{'Rn{'Rn{'Rn{'R( LThe Condenser Utility Outlet Temperature Must Not Exceed 45 degrees Celsius!˒='RTower_Sizing_and_Pricing Estimates3;RȲ3;R3;R3;RDz3;R3;R 1 Estimates_Click h#=h8+3q Estimatesز3;Rݲ3;Rٲ3;Rܲ3;R Coefficients۲3;R 1 Coefficients_ClickG?,2qL3;R߲3;R3;R3;R޲3;RƲ3;R 1 8 p3;R3;R3;R3;R3;R3;R  1  Estimate_Open 3;R3;R 3;R3;RShutdown3;R y 1 Shutdown_Click l InstructionsMenuItms Instructions for use Instructions33;R23;R63;R53;R(3;R83;R)3;R%3;R73;R,3;R 1 p ;R ;R ;R ;R ;R ;R 1  Tower_Open Instructions_Open Tower_OpenInstructions_Open2sv;R2sv;R2sv;R2sv;R2sv;R2sv;R 9 1 CommandButton2_Click LSpecifications3sv;R3sv;R3sv;R3sv;R3sv;R3sv;R 1 H Label1_ClickShowAbout Specifications Specifications_Open About About_OpenSpecifications_Open About_Open6\ ;Rs3sv;RY3sv;RU3sv;Rr3sv;R6\ ;R  1 YL&i eImage1 Tfdk6\ ;R7\ ;R6\ ;R Y 1 6\ ;R7\ ;R6\ ;R6\ ;R7\ ;R6\ ;R 1   Please Enter Registration Code: 157727\ ;R6\ ;R  1 X &7\ ;R Registration Code07\ ;R7\ ;R7\ ;R7\ ;R6\ ;R7\ ;R 7\ ;R 1 57\ ;R 112874082778P83R Agreement agreementagreeagreeikֺ2'Rkֺ2'Rjkֺ2'Rfkֺ2'Rkֺ2'Rkֺ2'R Q 1 TextBox1 UserAgreementh?'Rh?'RUserAgreement_Open6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R 1 !6㮤'R6㮤'R q 1 !6㮤'R6㮤'R  1 ("6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R 1 "6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R6㮤'R٨ 3R E26(٨ 3R )Error in Material Balance, Please Recheck־j_ p3Rվj_ p3RRegQueryValueEx advapi32.dll RegQueryValueExA H%RegCreateKeyEx RegCreateKeyExA `% RegSetValueEx RegSetValueExA Qx% RegCloseKey RegCloseKeyA % RegOpenKeyEx RegOpenKeyExA % CheckNumberɾj_ p3R a 1 &þj_ p3R 1Software\VB and VBA Program Settings\Tower Sizing H % Registrationپj_ p3Rؾj_ p3R۾j_ p3Rھj_ p3R GetRegNumber /Unsuccessful in Opening key to search for valuej_ p3Rj_ p3R I 1 P&Ǿj_ p3Ržj_ p3R 1 &ݾj_ p3Rܾj_ p3R $Software\VB and VBA Program Settingsj_ p3Rj_ p3R Tower Sizing Registration Required &Please Enter Your Registration Number: Registration Successful Unable to Open Key Incorrect Registration Number! 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I"  $  % ( & 8 Y( H ) X + h 1, x !.  I4  I;  <  1A  QB  qC  E  H  Z  Y\ ( ^ 8 c H .Macro recorded 12/12/98 by Christopher Haslego 14 h X n h { x w       1  .Macro recorded 12/15/98 by Christopher Haslegod 14  APerforms sizing and pricing calculations for distillation columnsKey    9 ( 8 H 1 X a h 1 x A      )  !  y    A  (hKey lpValueName dwReservedlpTypelpDatalpcdDatelpSubKeydwOption samDesiredlpSecurityAttributes phkResult + lpdwDispositiondwTypecbData ulOptions q 8 H 1 X ulReservedlpClass Y h  x   Q       A    Y      9 Pathentryvalue  ( ) 8  H )! X ! h # x $  !)  i*  ,  A.  0  I5  6  8  Q9 ( : 8_(H  M@}}7A1R KQDB Arial NarrowK (2PLabel1@(2HLabel2@"( 8TTemperatureg O(2LLabel3@( 8BTemperatureg (fk o<>pCompObj?aVBFrame0 @Arial NarrowH,qa5 Arial Narrow,(Installed Cost of Condenser @Arial NarrowH,qa5 Arial Narrow$(Annual Cost of Steam @Arial NarrowH,qa5 Arial Narrow,(Annual Cost of Cooling Water] @Arial NarrowH,qa5 Arial Narrow,(Net Present Value ( i = 8% ) @Arial NarrowH,qa5 Arial Narrow<,&Calculate Medium Pressure Steam Column u Arial Narrow8,$Calculate High Pressure Steam Column u Arial NarrowAA\, {5 Arial Narrow4,Output Results to Spreadsheet@F u Arial Narrow8,#Estimate Heat Transfer Coefficients u Arial Narrow,Exit u Arial Narrow2HLabel4@ ( 8RVolatilityg E(2LLabel5@ $ 8VDensityg  \-LPSu#( 2h Label6@( 8 RCoefficientg ( 2h Label7@( 8 CCoefficientg (2H Label8@( 8FViscosityOg (2TLabel9@$DMOCTraysg !(2TLabel10? 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The "Inputs for Each Column Data" should be entered for each geometric change in the tower. The "Inputs for Each Run of Column" are variables that can change with upstream conditions. Once the data is entered, you can press the "Calculate" button at the bottom that corresponds to the type of reboiler utility that your column would require. (See 'Specifications' for Steam conditions). The calculated results, along with inputs, can then be exported to a worksheet for further analysis or charting. The Net Present Value function can be used for optimization when several configurations or parametric possibilities exist. I hope you enjoy this product brought to you by The Chemical Engineers' Resource Page./0 5Times New Roman( Get Started #u Arial Narrow(Exit #u Arial Narrowel1@,@CommandButton1I,8CommandButton2I  Microsoft Forms 2.0 FormEmbedded Object9qVERSION 5.00 Begin {C62A69F0-16DC-11CE-9E98-00AA00574A4F} Instructions Caption = "Instructions for Use" ClientHeight = 3885 ClientLeft = 45 ClientTop = 390 ClientWidth = 7260 StartUpPosition = CompObjIaVBFrame1SpecificationsLM? ?f 1 'CenterOwner TypeInfoVer = 5 End (H  @}_0? R KQDBTahoma(2Label1@(Cooling Water in Condenser is available at 30 0C and must be returned at a temperature no higher than 45 0C LPS (Low Pressure Steam) is at 5 barg and 160 0C oKMlCompObjNaVBFrame5About TQ ? ? MPS (Medium Pressure Steam) is at 10 barg and 184 0C HPS (High Pressure Steam) is at 41 barg and 254 0C Utility Costs: LPS ($3.17/GJ), MPS ($3.66/GJ), HPS ($5.09/GJ), Water ($0.16/GJ) Condenser is priced as a Fixed Head, Shell and Tube Exchanger Reboiler is priced as a Floating Head Shell and Tube Exchanger Prices are calculated using correlations developed by G.D. Ulrich in "A Guide to Chemical Engineering Process Design and Economics", Wiley, New York 1984. Net Present Value is calculated using a taxation rate of 40% and an interest rate of 8% over a 10 year time span. Flooding and other tray behavior should be investigated by user. This program also assumes constant vapor velocity and tray efficiently. 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