Changeset 721 for branches/gui/eml/stage_separators/condenser.mso
- Timestamp:
- Feb 25, 2009, 7:51:53 PM (14 years ago)
- File:
-
- 1 edited
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branches/gui/eml/stage_separators/condenser.mso
r719 r721 162 162 Model condenserReact 163 163 ATTRIBUTES 164 Pallete = true;164 Pallete = false; 165 165 Icon = "icon/Condenser"; 166 166 Brief = "Model of a Condenser with reaction in liquid phase."; … … 183 183 "; 184 184 185 186 outer PP as Plugin(Type="PP");185 PARAMETERS 186 outer PP as Plugin(Type="PP"); 187 187 outer NComp as Integer; 188 V as volume (Brief="Condenser total volume"); 189 Across as area (Brief="Cross Section Area of reboiler"); 190 191 stoic(NComp) as Real(Brief="Stoichiometric matrix"); 192 Hr as energy_mol; 193 194 VARIABLES 195 in InletV as stream(Brief="Vapour inlet stream", PosX=0.1164, PosY=0, Symbol="_{inV}"); 196 out OutletL as liquid_stream(Brief="Liquid outlet stream", PosX=0.4513, PosY=1, Symbol="_{outL}"); 197 out OutletV as vapour_stream(Brief="Vapour outlet stream", PosX=0.4723, PosY=0, Symbol="_{outV}"); 198 InletQ as power (Brief="Cold supplied", PosX=1, PosY=0.6311, Symbol="_{in}"); 199 200 M(NComp) as mol (Brief="Molar Holdup in the tray"); 201 ML as mol (Brief="Molar liquid holdup"); 202 MV as mol (Brief="Molar vapour holdup"); 203 E as energy (Brief="Total Energy Holdup on tray"); 204 vL as volume_mol (Brief="Liquid Molar Volume"); 205 vV as volume_mol (Brief="Vapour Molar volume"); 206 Level as length (Brief="Level of liquid phase"); 207 Vol as volume; 208 r3 as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s'); 209 C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1); 210 211 EQUATIONS 212 "Molar Concentration" 188 189 V as volume (Brief="Condenser total volume"); 190 Across as area (Brief="Cross Section Area of reboiler"); 191 192 stoic(NComp) as Real (Brief="Stoichiometric matrix"); 193 Hr as energy_mol; 194 Initial_Level as length (Brief="Initial Level of liquid phase"); 195 Initial_Temperature as temperature (Brief="Initial Temperature of Condenser"); 196 Initial_Composition(NComp) as fraction (Brief="Initial Liquid Composition"); 197 198 VARIABLES 199 200 in InletV as stream (Brief="Vapour inlet stream", PosX=0.1164, PosY=0, Symbol="_{inV}"); 201 out OutletL as liquid_stream (Brief="Liquid outlet stream", PosX=0.4513, PosY=1, Symbol="_{outL}"); 202 out OutletV as vapour_stream (Brief="Vapour outlet stream", PosX=0.4723, PosY=0, Symbol="_{outV}"); 203 InletQ as power (Brief="Cold supplied", PosX=1, PosY=0.6311, Symbol="_{in}"); 204 205 M(NComp) as mol (Brief="Molar Holdup in the tray"); 206 ML as mol (Brief="Molar liquid holdup"); 207 MV as mol (Brief="Molar vapour holdup"); 208 E as energy (Brief="Total Energy Holdup on tray"); 209 vL as volume_mol (Brief="Liquid Molar Volume"); 210 vV as volume_mol (Brief="Vapour Molar volume"); 211 Level as length (Brief="Level of liquid phase"); 212 Vol as volume; 213 r3 as reaction_mol (Brief="Reaction Rates", DisplayUnit = 'mol/l/s'); 214 C(NComp) as conc_mol (Brief="Molar concentration", Lower = -1); 215 216 INITIAL 217 218 Level = Initial_Level; 219 OutletL.T = Initial_Temperature; 220 OutletL.z(1:NComp-1) = Initial_Composition(1:NComp-1)/sum(Initial_Composition); 221 222 EQUATIONS 223 "Molar Concentration" 213 224 OutletL.z = vL * C; 214 225 215 226 "Reaction" 216 227 r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4)) * 'l/mol/s'; 217 228 218 "Component Molar Balance" 219 diff(M) = InletV.F*InletV.z - OutletL.F*OutletL.z 220 - OutletV.F*OutletV.z + stoic*r3*ML*vL; 221 222 "Energy Balance" 223 diff(E) = InletV.F*InletV.h - OutletL.F*OutletL.h 224 - OutletV.F*OutletV.h + InletQ + Hr * r3 * ML*vL; 225 226 "Molar Holdup" 229 "Component Molar Balance" 230 diff(M) = InletV.F*InletV.z - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL; 231 232 "Energy Balance" 233 diff(E) = InletV.F*InletV.h - OutletL.F*OutletL.h- OutletV.F*OutletV.h + InletQ + Hr * r3 * ML*vL; 234 235 "Molar Holdup" 227 236 M = ML*OutletL.z + MV*OutletV.z; 228 237 229 238 "Energy Holdup" 230 239 E = ML*OutletL.h + MV*OutletV.h - OutletV.P*V; 231 240 232 241 "Mol fraction normalisation" 233 242 sum(OutletL.z)=1.0; 234 243 235 244 "Liquid Volume" 236 245 vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z); 237 "Vapour Volume" 246 247 "Vapour Volume" 238 248 vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); 239 249 240 250 "Thermal Equilibrium" 241 251 OutletL.T = OutletV.T; 242 252 243 253 "Mechanical Equilibrium" 244 254 OutletV.P = OutletL.P; 245 255 246 256 "Geometry Constraint" 247 257 V = ML*vL + MV*vV; 248 258 249 259 Vol = ML*vL; 250 260 251 261 "Level of liquid phase" 252 262 Level = ML*vL/Across; 253 263 254 264 "Chemical Equilibrium" 255 265 PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 256 266 PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z;
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