Changeset 503 for branches/rate/eml/stage_separators/tray.mso
 Timestamp:
 Apr 15, 2008, 5:48:57 PM (15 years ago)
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branches/rate/eml/stage_separators/tray.mso
r498 r503 472 472 hl = (12*miL*a^2*uL/rhoL/g)^1/3; 473 473 end 474 475 Model trayRate 476 ATTRIBUTES 477 Pallete = false; 478 Icon = "icon/Tray"; 479 Brief = "Basic equations of a tray column model."; 480 Info = 481 "This model contains only the main equations of a column tray equilibrium model without 482 the hidraulic equations. 483 484 == Assumptions == 485 * both phases (liquid and vapour) exists all the time; 486 * thermodymanic equilibrium with Murphree plate efficiency; 487 * no entrainment of liquid or vapour phase; 488 * no weeping; 489 * the dymanics in the downcomer are neglected. 490 "; 491 492 PARAMETERS 493 outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); 494 outer NComp as Integer; 495 V as volume(Brief="Total Volume of the tray"); 496 Q as heat_rate (Brief="Rate of heat supply"); 497 Ap as area (Brief="Plate area = Atray  Adowncomer"); 498 499 VARIABLES 500 in Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}"); 501 in InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}"); 502 in InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}"); 503 out OutletL as liquid_stream (Brief="Outlet liquid stream", PosX=0.8277, PosY=1, Symbol="_{outL}"); 504 out OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}"); 505 506 M(NComp) as mol (Brief="Molar Holdup in the tray"); 507 ML as mol (Brief="Molar liquid holdup"); 508 MV as mol (Brief="Molar vapour holdup"); 509 E as energy (Brief="Total Energy Holdup on tray"); 510 vL as volume_mol (Brief="Liquid Molar Volume"); 511 vV as volume_mol (Brief="Vapour Molar volume"); 512 Level as length (Brief="Height of clear liquid on plate"); 513 yideal(NComp) as fraction; 514 Emv as Real (Brief = "Murphree efficiency"); 515 516 EQUATIONS 517 "Component Molar Balance" 518 diff(M)=Inlet.F*Inlet.z + InletL.F*InletL.z + InletV.F*InletV.z 519  OutletL.F*OutletL.z  OutletV.F*OutletV.z; 520 521 "Energy Balance" 522 diff(E) = ( Inlet.F*Inlet.h + InletL.F*InletL.h + InletV.F*InletV.h 523  OutletL.F*OutletL.h  OutletV.F*OutletV.h + Q ); 524 525 "Molar Holdup" 526 M = ML*OutletL.z + MV*OutletV.z; 527 528 "Energy Holdup" 529 E = ML*OutletL.h + MV*OutletV.h  OutletL.P*V; 530 531 "Mol fraction normalisation" 532 sum(OutletL.z)= 1.0; 533 sum(OutletL.z)= sum(OutletV.z); 534 535 "Liquid Volume" 536 vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z); 537 "Vapour Volume" 538 vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); 539 540 "Chemical Equilibrium" 541 PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = 542 PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, yideal)*yideal; 543 544 "Murphree Efficiency" 545 OutletV.z = Emv * (yideal  InletV.z) + InletV.z; 546 547 "Thermal Equilibrium" 548 OutletV.T = OutletL.T; 549 550 "Mechanical Equilibrium" 551 OutletV.P = OutletL.P; 552 553 "Geometry Constraint" 554 V = ML* vL + MV*vV; 555 556 "Level of clear liquid over the weir" 557 Level = ML*vL/Ap; 558 end 559
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