Changeset 505 for branches/rate/eml/stage_separators/tray.mso
 Timestamp:
 Apr 18, 2008, 6:47:45 PM (15 years ago)
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 1 edited
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branches/rate/eml/stage_separators/tray.mso
r503 r505 471 471 "Liquid holdup" 472 472 hl = (12*miL*a^2*uL/rhoL/g)^1/3; 473 474 473 475 end 474 476 475 Model trayRate 477 #* 478 * Nonequilibrium Model 479 *# 480 Model interface 481 476 482 ATTRIBUTES 477 483 Pallete = false; … … 479 485 Brief = "Basic equations of a tray column model."; 480 486 Info = 481 "This model contains only the main equations of a column tray equilibrium model without 487 "This model contains only the main equations of a column tray nonequilibrium model without 488 the hidraulic equations."; 489 490 PARAMETERS 491 outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); 492 outer NComp as Integer; 493 outer NC1 as Integer; 494 495 VARIABLES 496 NL(NComp) as flux_mol (Brief = "Stream Molar Flux Rate on Liquid Phase"); 497 NV(NComp) as flux_mol (Brief = "Stream Molar Flux Rate on Vapour Phase"); 498 T as temperature (Brief = "Stream Temperature"); 499 P as pressure (Brief = "Stream Pressure"); 500 x(NComp) as fraction (Brief = "Stream Molar Fraction on Liquid Phase"); 501 y(NComp) as fraction (Brief = "Stream Molar Fraction on Vapour Phase"); 502 a as area (Brief = "Interface Area"); 503 htL as heat_trans_coeff (Brief = "Heat Transference Coefficient on Liquid Phase"); 504 htV as heat_trans_coeff (Brief = "Heat Transference Coefficient on Vapour Phase"); 505 E_liq as heat_flux (Brief = "Liquid Energy on interface"); 506 E_vap as heat_flux (Brief = "Vapour Energy on interface"); 507 hL as enth_mol (Brief = "Liquid Molar Enthalpy"); 508 hV as enth_mol (Brief = "Vapour Molar Enthalpy"); 509 ConcL as conc_mol (Brief = "Liquid Molar Concentration"); 510 ConcV as conc_mol (Brief = "Vapour Molar Concentration"); 511 kL(NC1,NC1) as velocity (Brief = "Mass Transfer Coefficients"); 512 kV(NC1,NC1) as velocity (Brief = "Mass Transfer Coefficients"); 513 514 EQUATIONS 515 "Liquid Enthalpy" 516 hL = PP.LiquidEnthalpy(T, P, x); 517 518 "Vapour Enthalpy" 519 hV = PP.VapourEnthalpy(T, P, y); 520 521 end 522 523 Model trayRate 524 ATTRIBUTES 525 Pallete = false; 526 Icon = "icon/Tray"; 527 Brief = "Basic equations of a tray column model."; 528 Info = 529 "This model contains only the main equations of a column tray nonequilibrium model without 482 530 the hidraulic equations. 483 531 484 532 == Assumptions == 485 533 * both phases (liquid and vapour) exists all the time; 486 * thermodymanic equilibrium with Murphree plate efficiency;487 534 * no entrainment of liquid or vapour phase; 488 535 * no weeping; … … 493 540 outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); 494 541 outer NComp as Integer; 542 NC1 as Integer; 495 543 V as volume(Brief="Total Volume of the tray"); 496 544 Q as heat_rate (Brief="Rate of heat supply"); … … 499 547 VARIABLES 500 548 in Inlet as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}"); 549 in InletFV as stream (Brief="Feed stream", PosX=0, PosY=0.4932, Symbol="_{in}"); 501 550 in InletL as stream (Brief="Inlet liquid stream", PosX=0.5195, PosY=0, Symbol="_{inL}"); 502 551 in InletV as stream (Brief="Inlet vapour stream", PosX=0.4994, PosY=1, Symbol="_{inV}"); … … 504 553 out OutletV as vapour_stream (Brief="Outlet vapour stream", PosX=0.8043, PosY=0, Symbol="_{outV}"); 505 554 506 M(NComp) as mol (Brief="Molar Holdup in the tray"); 555 M_liq(NComp) as mol (Brief="Liquid Molar Holdup in the tray"); 556 M_vap(NComp) as mol (Brief="Vapour Molar Holdup in the tray"); 507 557 ML as mol (Brief="Molar liquid holdup"); 508 558 MV as mol (Brief="Molar vapour holdup"); 509 E as energy (Brief="Total Energy Holdup on tray"); 559 E_liq as energy (Brief="Total Liquid Energy Holdup on tray"); 560 E_vap as energy (Brief="Total Vapour Energy Holdup on tray"); 510 561 vL as volume_mol (Brief="Liquid Molar Volume"); 511 562 vV as volume_mol (Brief="Vapour Molar volume"); 512 563 Level as length (Brief="Height of clear liquid on plate"); 513 yideal(NComp) as fraction; 514 Emv as Real (Brief = "Murphree efficiency"); 564 interf as interface; 515 565 516 566 EQUATIONS 517 567 "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; 568 diff(M_liq)=Inlet.F*Inlet.z + InletL.F*InletL.z 569  OutletL.F*OutletL.z + interf.a*interf.NL; 570 571 diff(M_vap)=InletFV.F*InletFV.z + InletV.F*InletV.z 572  OutletV.F*OutletV.z  interf.a*interf.NV; 520 573 521 574 "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 ); 575 diff(E_liq) = Inlet.F*Inlet.h + InletL.F*InletL.h 576  OutletL.F*OutletL.h + Q + interf.a*interf.E_liq; 577 578 diff(E_vap) = InletFV.F*InletFV.h + InletV.F*InletV.h 579  OutletV.F*OutletV.h  interf.a*interf.E_vap; 524 580 525 581 "Molar Holdup" 526 M = ML*OutletL.z + MV*OutletV.z; 582 M_liq = ML*OutletL.z; 583 584 M_vap = MV*OutletV.z; 527 585 528 586 "Energy Holdup" 529 E = ML*OutletL.h + MV*OutletV.h  OutletL.P*V; 587 E_liq = ML*(OutletL.h  OutletL.P*vL); 588 589 E_vap = MV*(OutletV.h  OutletV.P*vV); 590 591 "Energy on interface" 592 interf.E_liq = interf.htL*(interf.TOutletL.T)+sum(interf.NL)*interf.hL; 593 594 interf.E_vap = interf.htV*(OutletV.Tinterf.T)+sum(interf.NV)*interf.hV; 595 596 "Mass Conservation" 597 interf.NL=interf.NV; 598 599 "Energy Conservation" 600 interf.E_liq = interf.E_vap; 601 530 602 531 603 "Mol fraction normalisation" 532 604 sum(OutletL.z)= 1.0; 533 605 sum(OutletL.z)= sum(OutletV.z); 606 sum(interf.x)=1.0; 607 sum(interf.x)=sum(interf.y); 534 608 535 609 "Liquid Volume" … … 539 613 540 614 "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; 549 615 PP.LiquidFugacityCoefficient(interf.T, interf.P, interf.x)*interf.x = 616 PP.VapourFugacityCoefficient(interf.T, interf.P, interf.y)*interf.y; 617 618 "Geometry Constraint" 619 V = ML*vL + MV*vV; 620 621 "Level of clear liquid over the weir" 622 Level = ML*vL/Ap; 623 624 "Total Mass Transfer Fluxes" 625 interf.NL(1:NC1)=interf.ConcL*sumt(interf.kL*(interf.x(1:NC1)OutletL.z(1:NC1)))+ 626 OutletL.z(1:NC1)*sum(interf.NL); 627 628 interf.NV(1:NC1)=interf.ConcV*sumt(interf.kV*(OutletV.z(1:NC1)interf.y(1:NC1)))+ 629 OutletV.z(1:NC1)*sum(interf.NV); 630 550 631 "Mechanical Equilibrium" 551 632 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; 633 interf.P=OutletL.P; 634 635 SET 636 NC1=NComp1; 558 637 end 559 638
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