 Timestamp:
 Feb 12, 2008, 4:55:35 PM (15 years ago)
 Location:
 branches/packed
 Files:

 1 added
 4 edited
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branches/packed/eml/stage_separators/column.mso
r453 r455 1264 1264 1265 1265 Model Section_Column_Packed 1266 ATTRIBUTES 1267 Pallete = true; 1268 Icon = "icon/SectionColumn"; 1269 Brief = "Model of a column section."; 1270 Info = 1271 "== Model of a column section containing == 1272 * NTrays trays. 1273 1274 == Specify == 1275 * the feed stream of each tray (Inlet); 1276 * the Murphree eficiency for each tray Emv; 1277 * the InletL stream of the top tray; 1278 * the InletV stream of the bottom tray. 1279 1280 == Initial Conditions == 1281 * the trays temperature (OutletL.T); 1282 * the trays liquid level (Level) OR the trays liquid flow (OutletL.F); 1283 * (NoComps  1) OutletL (OR OutletV) compositions for each tray. 1284 "; 1285 1286 PARAMETERS 1287 outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); 1288 outer NComp as Integer; 1289 NTrays as Integer(Brief="Number of trays", Default=2); 1266 1267 PARAMETERS 1268 outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); 1269 outer NComp as Integer; 1270 NStages as Integer(Brief="Number of trays", Default=2); 1290 1271 topdown as Integer(Brief="Trays counting (1=topdown, 1=bottomup)", Default=1); 1291 1272 top as Integer(Brief="Number of top tray"); … … 1293 1274 H as length (Brief="Height of packing"); 1294 1275 1295 SET 1296 top = (NTrays1)*(1topdown)/2+1; 1297 bot = NTrays/top; 1298 1299 VARIABLES 1300 stage(NTrays) as packedStage; 1301 1302 EQUATIONS 1303 stage.hs = H/NTrays; 1304 1276 VARIABLES 1277 stage(NStages) as packedStage_BilletSchultes; 1278 1279 SET 1280 top = (NStages1)*(1topdown)/2+1; 1281 bot = NStages/top; 1282 stage.hs = H/NStages; 1283 stage.V = stage.hs * stage.Ap; 1284 1305 1285 CONNECTIONS 1306 1286 stage([top+topdown:topdown:bot]).OutletV to stage([top:topdown:bottopdown]).InletV; … … 1316 1296 top as Integer(Brief="Number of top tray"); 1317 1297 bot as Integer(Brief="Number of bottom tray"); 1318 1319 SET 1320 top = (NStages1)*(1topdown)/2+1; 1321 bot = NStages/top; 1322 1323 VARIABLES 1324 stage(NStages) as packedStage; 1298 H as length (Brief="Height of packing"); 1299 K as Real (Brief="Reboiler flow constant", Unit='mol*s^0.5/kg^0.5/m'); 1300 1301 VARIABLES 1302 stage(NStages) as packedStage_BilletSchultes; 1325 1303 cond as condenser; 1326 1304 reb as reboiler; 1327 1305 sptop as splitter; 1328 1306 pump1 as pump; 1307 1308 SET 1309 top = (NStages1)*(1topdown)/2+1; 1310 bot = NStages/top; 1311 stage.hs = H/NStages; 1312 stage.V = stage.hs * stage.Ap; 1329 1313 1330 1314 CONNECTIONS … … 1340 1324 stage([top:topdown:bottopdown]).OutletL to stage([top+topdown:topdown:bot]).InletL; 1341 1325 stage(bot).OutletL to reb.InletL; 1342 1343 EQUATIONS 1344 reb.OutletV.F = stage(bot).OutletV.F; 1345 end 1326 end 
branches/packed/eml/stage_separators/tray.mso
r454 r455 357 357 Cpo as Real (Brief="Constant for resitance equation"); # Billet and Schultes, 1999. 358 358 Mw(NComp) as molweight (Brief = "Component Mol Weight"); 359 359 hs as length (Brief="Height of the packing stage"); 360 360 361 VARIABLES 361 362 miL as viscosity (Brief="Liquid dynamic viscosity", DisplayUnit='kg/m/s'); … … 365 366 uL as velocity (Brief="volume flow rate of liquid, m^3/m^2/s", Default = 0.007); 366 367 uV as velocity (Brief="volume flow rate of vapor, m^3/m^2/s", Default = 1.14); 367 hs as length (Brief="Height of the packing stage");368 368 dp as length (Brief="Particle diameter"); 369 369 K as Real (Brief="Wall factor"); … … 389 389 uV * Ap = OutletV.F * vV; 390 390 391 #"Liquid holdup and Liquid flow"392 #vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap;391 "Liquid holdup and Liquid flow" 392 vL * ML = (12*miL*a^2*uL/rhoL/g)^1/3 * hs * Ap; 393 393 394 394 "Particle diameter" … … 396 396 397 397 "Wall Factor" 398 1 = K * 1+(2*dp/(3*ds*(1e)));398 1 = K * (1 + (2*dp/(3*ds*(1e)))); 399 399 400 400 "Reynolds number of the vapor stream" … … 402 402 403 403 #"Resistance Coefficient" 404 #Qsio = Cpo * (64/Rev )+ 1.8/Rev^0.08);404 #Qsio = Cpo * (64/Rev + 1.8/Rev^0.08); 405 405 #Qsio = Cpo * (64/Rev);# + 1.8/Rev^0.08); 406 406 407 407 "Pressure drop and Vapor flow" 408 (InletV.P  OutletV.P)/hs = Qsio*a*uV^2*rhoV / (2*e^2*K); 408 (InletV.P  OutletV.P)/hs * 'm'/'Pa' = Qsio*a*uV^2*rhoV / (2*e^3*K) * 's^2'*'m^2'/'kg'; 409 410 "Efficiency" 411 Emv = 1; 409 412 end 410 413 
branches/packed/sample/stage_separators/sample_column.mso
r453 r455 508 508 PP as Plugin(Brief="Physical Properties", 509 509 Type="PP", 510 Components = [ "isobut ane", "benzene"],510 Components = [ "isobutene", "npentane", "propylene", "benzene", "isobutane"], 511 511 LiquidModel = "PR", 512 512 VapourModel = "PR" … … 525 525 526 526 CONNECTIONS 527 feed.Outlet to sec.stage(1 5).Inlet;528 529 zero to sec.stage( [1:14]).Inlet;530 zero to sec.stage([1 6:24]).Inlet;531 532 reb to sec.stage( 24).InletV;527 feed.Outlet to sec.stage(10).Inlet; 528 529 zero to sec.stage(1:9).Inlet; 530 zero to sec.stage([11:sec.NStages]).Inlet; 531 532 reb to sec.stage(sec.NStages).InletV; 533 533 cond to sec.stage(1).InletL; 534 535 VARIABLES 536 deltaP_TOP as Real (Unit='atm/m'); 537 deltaP_BOT as Real (Unit='atm/m'); 538 539 EQUATIONS 540 deltaP_TOP = (sec.stage(1).InletV.P  sec.stage(1).OutletV.P)/sec.stage(1).hs; 541 deltaP_BOT = (sec.stage(sec.NStages).InletV.P  sec.stage(sec.NStages).OutletV.P)/sec.stage(sec.NStages).hs; 534 542 535 543 SPECIFY … … 537 545 feed.Outlet.T = 291 * 'K'; 538 546 feed.Outlet.P = 168.3 * 'kPa'; 539 feed.Outlet.z = [0.5, 0.5];547 feed.Outlet.z = 1/NComp; 540 548 541 549 zero.F = 0 * 'kmol/h'; 542 550 zero.T = 300 * 'K'; 543 551 zero.P = 1 * 'atm'; 544 zero.z = [0.5, 0.5];552 zero.z = 1/NComp; 545 553 zero.v = 0; 546 554 zero.h = 0 * 'J/mol'; 547 555 548 cond.F = 68 * 'kmol/h'; 549 cond.P = 150 * 'kPa'; 550 cond.T = 281.75 * 'K'; 551 cond.z = [0.6664, 0.3336]; 552 553 reb.F = 153 * 'kmol/h'; 554 reb.P = 185 * 'kPa'; 555 reb.T = 328.12 * 'K'; 556 reb.z = [0.001848, 0.9982]; 557 558 sec.stage.Emv = 1; 559 # sec.stage(1).OutletV.F = 150 * 'kmol/h'; 560 561 SET 562 sec.NTrays = 24; 563 564 # sec.stage.PressureDropModel = "Leva"; 565 # sec.stage.PackingType = "random"; 566 567 sec.stage.V = 4 * 'ft^3'; 556 cond.F = 85 * 'kmol/h'; 557 cond.P = 2.2 * 'atm'; 558 cond.T = 273 * 'K'; 559 cond.z = [0.26682, 0.19950, 0.26682, 0.000051, 0.26680]; 560 561 reb.F = 143.4 * 'kmol/h'; 562 reb.P = 5 * 'atm'; 563 reb.T = 361 * 'K'; 564 reb.z = [0.0001611, 0.51834, 0.00000076, 0.48115, 0.00035]; 565 566 #sec.stage.Qsio = 1; 567 568 SET 569 sec.H = 4 * 'm'; 570 sec.NStages = 16; 568 571 sec.stage.Q = 0 * 'kW'; 569 sec.stage.Ap = 3.94 * 'ft^2'; 572 sec.stage.Ap = 1.5 * 'm^2'; 573 sec.stage.ds = 1.009 * 'm'; 574 sec.stage.Cpo = 0.763; 575 sec.stage.e = 0.951; 576 sec.stage.a = 112.6 * 'm^2/m^3'; 570 577 571 578 INITIAL 572 sec.stage.OutletL.T = [2 90:(330290)/(sec.NTrays1):330] *'K';573 sec.stage. Level = 0.5 * 'ft';574 sec.stage.OutletL.z( 1) = 0.5;579 sec.stage.OutletL.T = [273:(360273)/(sec.NStages1):360] *'K'; 580 sec.stage.ML = 0.5 * 'kmol'; 581 sec.stage.OutletL.z([1:4]) = 1/NComp; 575 582 576 583 OPTIONS 577 InitialFile = "/home/paula/SectionColumn_Test_with8tray.rlt"; 578 TimeStep = 1; 579 TimeEnd = 100; 580 #GuessFile="SectionColumn_Test_with8tray.rlt"; 581 #Dynamic = false; 584 DAESolver(File="dassl"); 585 TimeStep = 0.01; 586 TimeEnd = 1; 582 587 end 583 588 584 FlowSheet Packed_kettle_cond_Test 589 FlowSheet Packed_kettle_cond_Test_1 585 590 PARAMETERS 586 591 PP as Plugin(Brief="Physical Properties", … … 630 635 Qc.OutletQ.Q = 700 * 'cal/min'; 631 636 col.pump1.dP = 0.1 * 'atm'; 632 col.stage.Emv = 1; 633 col.stage.hs = 100 * 'mm'; 634 635 SET 636 col.NStages = 10; 637 col.stage.Qsio = 0.05; 638 639 EQUATIONS 640 col.reb.OutletV.F = col.K * sqrt(Qr.OutletQ.Q); 641 642 SET 643 col.NStages = 5; 637 644 col.cond.V = 1 * 'l'; 638 645 col.cond.Across = 100 * 'cm^2'; 646 col.K = 0.2 * 'mol*min^0.5/kg^0.5/m'; 639 647 col.reb.V = 2 * 'l'; 640 648 col.reb.Across = 200 * 'cm^2'; 641 col.stage.V = 576.4 * 'cm^3';642 649 col.stage.Q = 0 * 'kW'; 643 650 col.stage.Ap = 56.74 * 'cm^2'; 644 651 col.stage.ds = 85 * 'mm'; 645 col.stage.d = 20 * 'mm';646 col.stage.C = 2.18;647 col.stage.Cp = 1.329;648 652 col.stage.e = 0.662; 649 653 col.stage.a = 185.4 * 'm^2/m^3'; 650 654 col.H = 1 * 'm'; 655 col.stage.Cpo = 0.763; 656 651 657 INITIAL 652 658 # condenser 653 659 col.cond.OutletL.T = (63.5+273.15) *'K'; 654 660 col.cond.Level = 2 * 'cm'; 655 col.cond.OutletL.z(1) = 0. 16;661 col.cond.OutletL.z(1) = 0.8; #0.16; 656 662 657 663 # reboiler … … 662 668 # column stages 663 669 col.stage.OutletL.T = [(63.5+273.15):((82+273.15)(63.5+273.15))/(col.NStages1):(82+273.15)] * 'K'; 664 col.stage.Level = 1 * 'cm'; 665 col.stage.OutletL.z(1) = 0.16; 670 col.stage.Level = 2 * 'cm'; 671 #col.stage.ML = 0.2 * 'mol'; 672 col.stage.OutletL.z(1) = 0.5; #0.16; 666 673 667 674 OPTIONS 668 675 TimeStep = 0.1; 669 676 TimeEnd = 50; 670 #GuessFile = "/home/paula/SectionColumn_Test_with8tray.rlt";671 #GuessFile="Distillation_kettle_cond_Test.rlt";672 #Dynamic = false;673 677 end 
branches/packed/sample/stage_separators/sample_tray.mso
r454 r455 218 218 inV.z = [0.0584, 0.9416]; 219 219 220 t1.Emv = 1;221 220 t1.hs = 0.4 * 'm';#0.075 * 'm'; 222 221 # t1.OutletV.F = 147.1 * 'kmol/h'; 223 t1.OutletL.F = 229.5 * 'kmol/h';224 t1.Qsio = 0.8;222 # t1.OutletL.F = 229.5 * 'kmol/h'; 223 # t1.Qsio = 2.2; 225 224 226 225 SET … … 235 234 236 235 INITIAL 237 t1.OutletL.T = 3 50 *'K';236 t1.OutletL.T = 310 *'K'; 238 237 t1.ML = 0.5 * 'mol'; 239 t1.OutletL.z(1) = 0. 2;238 t1.OutletL.z(1) = 0.05; 240 239 241 240 OPTIONS 242 #InitialFile = "/home/paula/tray_Test.rlt"; 243 InitialFile = "/home/paula/packedStage_Test.rlt"; 241 InitialFile = "packedStage_BilletSchultes_Test.rlt"; 244 242 TimeStep = 2; 245 243 TimeEnd = 50;
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