- Timestamp:
- Sep 23, 2008, 7:20:38 PM (14 years ago)
- Location:
- trunk/eml
- Files:
-
- 16 edited
Legend:
- Unmodified
- Added
- Removed
-
trunk/eml/heat_exchangers/Heatex.mso
r529 r632 15 15 *-------------------------------------------------------------------- 16 16 * Author: Gerson Balbueno Bicca 17 * $ 17 * $Id: Heatex.mso 574 2008-07-25 14:18:50Z rafael $ 18 18 *--------------------------------------------------------------------*# 19 19 20 20 using "heat_exchangers/HEX_Engine"; 21 22 Model Basic_Pdrop23 24 ATTRIBUTES25 Pallete = false;26 Brief = "to be documented";27 Info =28 "to be documented";29 30 VARIABLES31 32 Pdrop as press_delta (Brief="Pressure Drop",Default=0.01, Lower=0,DisplayUnit='kPa' , Symbol ="\Delta P");33 FPdrop as Real (Brief="Pressure Drop : Fraction of Inlet",Lower=0,Upper=0.8);34 35 end36 37 Model Main_Simplified38 39 ATTRIBUTES40 Pallete = false;41 Brief = "to be documented";42 Info =43 "to be documented";44 45 VARIABLES46 47 PressureDrop as Basic_Pdrop (Brief="Pressure Drop", Symbol=" ");48 Properties as Physical_Properties_Heatex (Brief="Physical Properties", Symbol=" ");49 50 end51 21 52 22 Model Heatex_Basic … … 54 24 ATTRIBUTES 55 25 Pallete = false; 56 Brief 26 Brief = "Basic Model for Simplified Heat Exchangers"; 57 27 Info = 58 "to be documented."; 28 "Model of a simplified heat exchanger. 29 This model perform only material and heat balance. 30 31 == Assumptions == 32 * Steady-State operation; 33 * No heat loss to the surroundings. 34 35 == Specify == 36 * The Inlet streams: Hot and Cold; 37 "; 59 38 60 39 PARAMETERS 61 outer PP as Plugin (Brief="External Physical Properties", Type="PP");40 outer PP as Plugin (Brief="External Physical Properties", Type="PP"); 62 41 outer NComp as Integer (Brief="Number of Components"); 63 42 … … 66 45 VARIABLES 67 46 68 in InletHot as stream(Brief="Inlet Hot Stream", PosX=0, PosY=0.4915, Symbol="^{inHot}");47 in InletHot as stream (Brief="Inlet Hot Stream", PosX=0, PosY=0.4915, Symbol="^{inHot}"); 69 48 out OutletHot as streamPH (Brief="Outlet Hot Stream", PosX=1, PosY=0.4915, Symbol="^{outHot}"); 70 in InletCold as stream(Brief="Inlet Cold Stream", PosX=0.5237, PosY=1, Symbol="^{inCold}");49 in InletCold as stream (Brief="Inlet Cold Stream", PosX=0.5237, PosY=1, Symbol="^{inCold}"); 71 50 out OutletCold as streamPH (Brief="Outlet Cold Stream", PosX=0.5237, PosY=0, Symbol="^{outCold}"); 72 51 73 xh(NComp) as fraction (Brief = "Liquid Molar Fraction in Hot Side",Hidden=true); 74 yh(NComp) as fraction (Brief = "Vapour Molar Fraction in Hot Side",Hidden=true); 75 vh as fraction (Brief = "Vapour Fraction in Hot Side",Hidden=true); 76 77 xc(NComp) as fraction (Brief = "Liquid Molar Fraction in Cold Side",Hidden=true); 78 yc(NComp) as fraction (Brief = "Vapour Molar Fraction in Cold Side",Hidden=true); 79 vc as fraction (Brief = "Vapour Fraction in Cold Side",Hidden=true); 80 81 Details as Details_Main (Brief="Heat Exchanger Details", Symbol=" "); 82 HotSide as Main_Simplified (Brief="Heat Exchanger Hot Side", Symbol="_{hot}"); 83 ColdSide as Main_Simplified (Brief="Heat Exchanger Cold Side", Symbol="_{cold}"); 52 A as area (Brief="Exchange Surface Area"); 53 Q as power (Brief="Duty", Default=7000, Lower=1e-6, Upper=1e10); 54 U as heat_trans_coeff (Brief="Overall Heat Transfer Coefficient",Default=1,Lower=1e-6,Upper=1e10); 55 56 PdropHotSide as press_delta (Brief="Pressure Drop Hot Side",Default=0.01, Lower=0,DisplayUnit='kPa' , Symbol ="\Delta P_{hot}"); 57 PdropColdSide as press_delta (Brief="Pressure Drop Cold Side",Default=0.01, Lower=0,DisplayUnit='kPa' , Symbol ="\Delta P_{cold}"); 84 58 85 59 SET … … 90 64 EQUATIONS 91 65 92 "Flash Calculation in Hot Side"93 [vh, xh, yh] = PP.Flash(InletHot.T, InletHot.P, InletHot.z);94 95 "Flash Calculation in Cold Side"96 [vc, xc, yc] = PP.Flash(InletCold.T, InletCold.P, InletCold.z);97 98 "Hot Stream Average Molecular Weight"99 HotSide.Properties.Mw = sum(M*InletHot.z);100 101 "Cold Stream Average Molecular Weight"102 ColdSide.Properties.Mw = sum(M*InletCold.z);103 104 "Cold Stream Average Heat Capacity"105 ColdSide.Properties.Cp = (1-InletCold.v)*PP.LiquidCp(0.5*InletCold.T+0.5*OutletCold.T,0.5*InletCold.P+0.5*OutletCold.P,xc)+106 InletCold.v*PP.VapourCp(0.5*InletCold.T+0.5*OutletCold.T,0.5*InletCold.P+0.5*OutletCold.P,yc);107 108 "Cold Stream Inlet Mass Density"109 ColdSide.Properties.Inlet.rho = (1-InletCold.v)*PP.LiquidDensity(InletCold.T,InletCold.P,xc)+110 InletCold.v*PP.VapourDensity(InletCold.T,InletCold.P,yc);111 112 "Cold Stream Outlet Mass Density"113 ColdSide.Properties.Outlet.rho = (1-OutletCold.v)*PP.LiquidDensity(OutletCold.T,OutletCold.P,OutletCold.x)+114 OutletCold.v*PP.VapourDensity(OutletCold.T,OutletCold.P,OutletCold.y);115 116 "Hot Stream Average Heat Capacity"117 HotSide.Properties.Cp = (1-InletHot.v)*PP.LiquidCp(0.5*InletHot.T+0.5*OutletHot.T,0.5*InletHot.P+0.5*OutletHot.P,xh)+118 InletHot.v*PP.VapourCp(0.5*InletHot.T+0.5*OutletHot.T,0.5*InletHot.P+0.5*OutletHot.P,yh);119 120 "Hot Stream Inlet Mass Density"121 HotSide.Properties.Inlet.rho = (1-InletHot.v)*PP.LiquidDensity(InletHot.T,InletHot.P,xc)+122 InletHot.v*PP.VapourDensity(InletHot.T,InletHot.P,yc);123 124 "Hot Stream Outlet Mass Density"125 HotSide.Properties.Outlet.rho = (1-OutletHot.v)*PP.LiquidDensity(OutletHot.T,OutletHot.P,OutletHot.x)+126 OutletHot.v*PP.VapourDensity(OutletHot.T,OutletHot.P,OutletHot.y);127 128 66 "Energy Balance Hot Stream" 129 Details.Q = InletHot.F*(InletHot.h-OutletHot.h);67 Q = InletHot.F*(InletHot.h-OutletHot.h); 130 68 131 69 "Energy Balance Cold Stream" 132 Details.Q =-InletCold.F*(InletCold.h-OutletCold.h); 133 134 "Flow Mass Inlet Cold Stream" 135 ColdSide.Properties.Inlet.Fw = sum(M*InletCold.z)*InletCold.F; 136 137 "Flow Mass Outlet Cold Stream" 138 ColdSide.Properties.Outlet.Fw = sum(M*OutletCold.z)*OutletCold.F; 139 140 "Flow Mass Inlet Hot Stream" 141 HotSide.Properties.Inlet.Fw = sum(M*InletHot.z)*InletHot.F; 142 143 "Flow Mass Outlet Hot Stream" 144 HotSide.Properties.Outlet.Fw = sum(M*OutletHot.z)*OutletHot.F; 70 Q =-InletCold.F*(InletCold.h-OutletCold.h); 145 71 146 72 "Molar Balance Hot Stream" … … 151 77 152 78 "Hot Stream Molar Fraction Constraint" 153 OutletHot.z 79 OutletHot.z = InletHot.z; 154 80 155 81 "Cold Stream Molar Fraction Constraint" … … 157 83 158 84 "Pressure Drop Hot Stream" 159 OutletHot.P = InletHot.P - HotSide.PressureDrop.Pdrop;85 OutletHot.P = InletHot.P - PdropHotSide; 160 86 161 87 "Pressure Drop Cold Stream" 162 OutletCold.P = InletCold.P - ColdSide.PressureDrop.Pdrop; 163 164 "Fraction of Inlet Pressure : Hot Stream" 165 HotSide.PressureDrop.Pdrop = InletHot.P*HotSide.PressureDrop.FPdrop; 166 167 "Fraction of Inlet Pressure : Cold Stream" 168 ColdSide.PressureDrop.Pdrop = InletCold.P*ColdSide.PressureDrop.FPdrop; 169 170 end 171 172 Model Heatex_LMTD as Heatex_Basic 88 OutletCold.P = InletCold.P - PdropColdSide; 89 90 end 91 92 Model Heatex_LMTD as Heatex_Basic 173 93 174 94 ATTRIBUTES 175 95 Pallete = true; 176 96 Icon = "icon/HeatExchanger_LMTD"; 177 Brief 97 Brief = "Simplified model for Heat Exchangers"; 178 98 Info = 179 "to be documented."; 99 "This model perform material and heat balance using the Log Mean Temperature Difference Approach. 100 This shortcut calculation does not require exchanger configuration or geometry data. 101 102 == Assumptions == 103 * Steady-State operation; 104 * No heat loss to the surroundings. 105 106 == Specify == 107 * The Inlet streams: Hot and Cold. 108 109 == References == 110 [1] E.A.D. Saunders, Heat Exchangers: Selection, Design and 111 Construction, Longman, Harlow, 1988. 112 113 [2] Taborek, J., Shell-and-tube heat exchangers, in Heat Exchanger Design Handbook, Vol. 3 114 Hemisphere Publishing Corp., New York, 1988. 115 116 [3] Fakheri, A. , Alternative approach for determining log mean temperature difference correction factor 117 and number of shells of shell and tube heat exchangers, Journal of Enhanced Heat Transfer, v. 10, p. 407- 420, 2003. 118 "; 180 119 181 120 PARAMETERS … … 186 125 VARIABLES 187 126 188 Method as LMTD_Basic (Brief="LMTD Method of Calculation", Symbol =" ");127 Method as LMTD_Basic (Brief="LMTD Method of Calculation", Symbol =" "); 189 128 R as positive (Brief="Capacity Ratio for LMTD Correction Fator",Lower=1e-6,Hidden=true); 190 129 P as positive (Brief="Non - Dimensional Variable for LMTD Correction Fator ",Lower=1e-6,Hidden=true); 191 Rho as positive (Brief="Non - Dimensional Variable for LMTD Correction Fator in Fakheri Equation",Lower=1e-6,Hidden=true);130 Rho as positive (Brief="Non - Dimensional Variable for LMTD Correction Fator in Fakheri Equation",Lower=1e-6,Hidden=true); 192 131 Phi as positive (Brief="Non - Dimensional Variable for LMTD Correction Fator in Fakheri Equation",Lower=1e-6, Symbol ="\phi",Hidden=true); 193 132 … … 195 134 196 135 "Duty" 197 Details.Q = Details.Ud*Details.A*Method.LMTD*Method.Fc;136 Q = U*A*Method.LMTD*Method.Fc; 198 137 199 138 switch ExchangerType … … 317 256 end 318 257 319 Model Heatex_NTU 258 Model Heatex_NTU as Heatex_Basic 320 259 321 260 ATTRIBUTES 322 261 Pallete = true; 323 262 Icon = "icon/HeatExchanger_NTU"; 324 Brief 263 Brief = "Simplified model for Heat Exchangers"; 325 264 Info = 326 "to be documented."; 265 "This model perform material and heat balance using the NTU-Effectiveness Approach. 266 This shortcut calculation does not require exchanger configuration or geometry data. 267 268 == Assumptions == 269 * Steady-State operation; 270 * No heat loss to the surroundings. 271 272 == Specify == 273 * The Inlet streams: Hot and Cold. 274 275 == References == 276 [1] E.A.D. Saunders, Heat Exchangers: Selection, Design and 277 Construction, Longman, Harlow, 1988. 278 279 "; 327 280 328 281 PARAMETERS … … 334 287 Method as NTU_Basic (Brief="NTU Method of Calculation", Symbol =" "); 335 288 289 xh(NComp) as fraction (Brief = "Liquid Molar Fraction in Hot Side",Hidden=true); 290 yh(NComp) as fraction (Brief = "Vapour Molar Fraction in Hot Side",Hidden=true); 291 vh as fraction (Brief = "Vapour Fraction in Hot Side",Hidden=true); 292 293 xc(NComp) as fraction (Brief = "Liquid Molar Fraction in Cold Side",Hidden=true); 294 yc(NComp) as fraction (Brief = "Vapour Molar Fraction in Cold Side",Hidden=true); 295 vc as fraction (Brief = "Vapour Fraction in Cold Side",Hidden=true); 296 336 297 EQUATIONS 337 298 299 "Flash Calculation in Hot Side" 300 [vh, xh, yh] = PP.Flash(InletHot.T, InletHot.P, InletHot.z); 301 302 "Flash Calculation in Cold Side" 303 [vc, xc, yc] = PP.Flash(InletCold.T, InletCold.P, InletCold.z); 304 338 305 "Number of Units Transference" 339 Method.NTU*Method.Cmin = Details.Ud*Details.A;306 Method.NTU*Method.Cmin = U*A; 340 307 341 308 "Minimum Heat Capacity" … … 349 316 350 317 "Duty" 351 Details.Q = Method.Eft*Method.Cmin*(InletHot.T-InletCold.T); 352 353 "Hot Stream Heat Capacity" 354 Method.Ch = InletHot.F*HotSide.Properties.Cp; 355 356 "Cold Stream Heat Capacity" 357 Method.Cc = InletCold.F*ColdSide.Properties.Cp; 318 Q = Method.Eft*Method.Cmin*(InletHot.T-InletCold.T); 319 320 "Hot Stream Average Heat Capacity" 321 Method.Ch = InletHot.F*((1-InletHot.v)*PP.LiquidCp(0.5*InletHot.T+0.5*OutletHot.T,0.5*InletHot.P+0.5*OutletHot.P,xh)+ 322 InletHot.v*PP.VapourCp(0.5*InletHot.T+0.5*OutletHot.T,0.5*InletHot.P+0.5*OutletHot.P,yh)); 323 324 "Cold Stream Average Heat Capacity" 325 Method.Cc = InletCold.F*((1-InletCold.v)*PP.LiquidCp(0.5*InletCold.T+0.5*OutletCold.T,0.5*InletCold.P+0.5*OutletCold.P,xc)+ 326 InletCold.v*PP.VapourCp(0.5*InletCold.T+0.5*OutletCold.T,0.5*InletCold.P+0.5*OutletCold.P,yc)); 358 327 359 328 "Effectiveness Correction" … … 393 362 394 363 "TEMA E Shell Effectiveness" 395 Method.Eft = 2*(1+Method.Cr+sqrt(1+Method.Cr^2)*((1+exp(-Method.NTU*sqrt(1+Method.Cr^2)))/(1-exp(-Method.NTU*sqrt(1+Method.Cr^2)))) )^-1; 396 397 end 398 399 400 end 401 402 end 403 364 Method.Eft = 2*(1+Method.Cr+sqrt(1+Method.Cr^2)*((1+exp(-Method.NTU*sqrt(1+Method.Cr^2)))/(1-exp(-Method.NTU*sqrt(1+Method.Cr^2)))) )^(-1); 365 366 end 367 368 369 end 370 371 end -
trunk/eml/heat_exchangers/heater.mso
r546 r632 29 29 30 30 PARAMETERS 31 outer PP as Plugin(Brief="Physical Properties", Type="PP");31 outer PP as Plugin (Brief="Physical Properties", Type="PP"); 32 32 outer NComp as Integer (Brief="Number of Components"); 33 Ninlet as Integer (Brief="Number of Inlet Streams"); 34 Kvalues as Switcher (Brief="Option for Display Phase Equilibrium K-values",Valid=["yes","no"], Default="yes"); 33 Kvalues as Switcher (Brief="Option for Display Phase Equilibrium K-values",Valid=["yes","no"], Default="yes"); 35 34 36 35 VARIABLES 37 QDuty as power (Brief = "Actual Duty",Symbol="Q_{Duty}"); 38 Vfrac as fraction (Brief = "Vapor fraction Outlet Stream",Symbol="V_{frac}"); 39 Lfrac as fraction (Brief = "Liquid fraction Outlet Stream",Symbol="L_{frac}"); 40 Kvalue(NComp) as Real (Brief = "Phase Equilibrium K-values",Symbol="K_{value}"); 41 Pratio(Ninlet ) as positive (Brief = "Pressure Ratio for each stream", Symbol ="P_{ratio}"); 42 Pdrop(Ninlet ) as press_delta (Brief = "Pressure Drop for each stream", DisplayUnit = 'kPa', Symbol ="\Delta P"); 43 in Inlet(Ninlet ) as stream (Brief = "Inlet Streams", PosX=0, PosY=0.4833, Symbol="^{in}"); 44 out Outlet as streamPH (Brief = "Outlet Stream", PosX=1, PosY=0.4782, Symbol="^{out}"); 36 Duty as power (Brief = "Actual Duty",Symbol="Q_{Duty}"); 37 Vfrac as fraction (Brief = "Vapor fraction Outlet Stream",Symbol="V_{frac}"); 38 Lfrac as fraction (Brief = "Liquid fraction Outlet Stream",Symbol="L_{frac}"); 39 Kvalue(NComp) as Real (Brief = "Phase Equilibrium K-values",Lower=1E-30,Upper=1E30,Symbol="K_{value}"); 40 Pratio as positive (Brief = "Pressure Ratio", Symbol ="P_{ratio}"); 41 Pdrop as press_delta (Brief = "Pressure Drop", DisplayUnit = 'kPa', Symbol ="\Delta P"); 42 43 in Inlet as stream (Brief = "Inlet Stream", PosX=0, PosY=0.45, Symbol="^{in}"); 44 out Outlet as streamPH (Brief = "Outlet Stream", PosX=1, PosY=0.45, Symbol="^{out}"); 45 45 46 46 EQUATIONS 47 47 48 48 "Flow" 49 Outlet.F = sum(Inlet.F);49 Outlet.F = Inlet.F; 50 50 51 for j in [1 : NComp] 51 for j in [1 : NComp] 52 52 53 53 "Composition" 54 Outlet.F*Outlet.z(j) = sum(Inlet.F*Inlet.z(j));54 Outlet.F*Outlet.z(j) = Inlet.F*Inlet.z(j); 55 55 56 56 end … … 63 63 64 64 "Heat Duty" 65 QDuty = Outlet.F*Outlet.h - sum(Inlet.F*Inlet.h);65 Duty = Outlet.F*Outlet.h - Inlet.F*Inlet.h; 66 66 67 67 "Pressure Drop" … … 72 72 73 73 switch Kvalues # Fix for better convergence !!! 74 74 75 case "yes": 75 76 "K-values Phase Equilibrium" … … 81 82 82 83 end 84 83 85 end 84 86 … … 93 95 94 96 == Specify == 95 * The Inlet stream s: Any Number97 * The Inlet stream 96 98 * Specify: 97 99 **The outlet temperature and the outlet pressure or … … 102 104 VARIABLES 103 105 104 in InletQas energy_stream (Brief ="Inlet Heat Stream", PosX=0.5, PosY=1, Symbol="_{out}");106 in Heat as energy_stream (Brief ="Inlet Heat Stream", PosX=0.5, PosY=1, Symbol="_{out}"); 105 107 106 108 EQUATIONS 107 "Net Duty" 108 InletQ.Q = QDuty; 109 110 "Duty Specification" 111 Heat.Q = Duty; 109 112 110 113 end … … 120 123 121 124 == Specify == 122 * The Inlet stream s: Any Number125 * The Inlet stream 123 126 * Specify: 124 127 **The outlet temperature and the outlet pressure or … … 129 132 VARIABLES 130 133 131 in InletQas energy_stream (Brief ="Inlet Heat Stream", PosX=0.5, PosY=1, Symbol="_{out}");134 in Heat as energy_stream (Brief ="Inlet Heat Stream", PosX=0.5, PosY=1, Symbol="_{out}"); 132 135 133 136 EQUATIONS 134 "Net Duty" 135 InletQ.Q = -QDuty; 137 138 "Duty Specification" 139 Heat.Q = -Duty; 136 140 137 141 end -
trunk/eml/heat_exchangers/icon/Shell_and_Tubes_LMTD.svg
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