The distillation column in this example is built from a number of pre-existing model objects. The model objects used in this example include the distillation stage, feed, flash, mixer, splitter, stream lag, and vessel. These basic models are connected to form the multicomponent distillation tower.

This distillation column is a separation of cyclohexane and n-heptane. The two components are separated over 30 theoretical trays. In general, distillation column models are generally good test cases for nonlinear model reduction and identification. The concentrations at each stage or tray are highly correlated. The dynamics of the distillation process can be described by a relatively few number of underlying dynamic states.

This model was published in:

Hahn, J. and T.F. Edgar, An improved method for nonlinear model reduction using balancing of empirical gramians, Computers and Chemical Engineering, 26, pp. 1379-1397, (2002)

The figure below displays the system response after a step change in the reflux ratio from 3.0 to 1.5. Each trajectory represents the mole fraction of cyclohexane at each tray. The top reflux material becomes less pure (more n-heptane) due to the increased draw from the top of the column.

! APMonitor Modeling Language ! http://www.apmonitor.com ! Binary Distillation Column from ! ! Hahn, J. and T.F. Edgar, An improved method for ! nonlinear model reduction using balancing of ! empirical gramians, Computers and Chemical ! Engineering, 26, pp. 1379-1397, (2002) ! ! Liquid mole fraction of component A ! at reflux ratio = 2 ! ! Condenser 0.93541941614016 ! Tray 1 0.90052553715795 ! Tray 2 0.86229645132283 ! . 0.82169940277993 ! . 0.77999079584355 ! . 0.73857168629759 ! . 0.69880490932694 ! . 0.66184253445732 ! . 0.62850777645505 ! . 0.59925269993058 ! . 0.57418567956453 ! . 0.55314422743545 ! . 0.53578454439850 ! . 0.52166550959767 ! . 0.51031495114413 ! . 0.50127509227528 ! . 0.49412891686784 ! . 0.48544992019184 ! . 0.47420248108803 ! . 0.45980349896163 ! . 0.44164297270225 ! . 0.41919109776836 ! . 0.39205549194059 ! . 0.36024592617390 ! . 0.32407993023343 ! . 0.28467681591738 ! . 0.24320921343484 ! . 0.20181568276528 ! . 0.16177269003094 ! Tray 29 0.12514970961746 ! Tray 30 0.09245832612765 ! Reboiler 0.06458317697321 Model binary Parameters ! reflux ratio rr = 0.7 ! Feed Flowrate (mol/min) Feed = 2.0 ! 24.0/60.0 ! Mole Fraction of Feed x_Feed = 0.5 ! Relative Volatility = (yA/xA)/(yB/xB) = KA/KB = alpha(A,B) vol=1.6 ! Total Molar Holdup in the Condenser atray=0.25 ! Total Molar Holdup on each Tray acond=0.5 ! Total Molar Holdup in the Reboiler areb=0.1 End Parameters Variables ! mole fraction of component A x[1:32] = 0.3 End Variables Intermediates ! Distillate Flowrate (mol/min) D=0.5*Feed ! Flowrate of the Liquid in the Rectification Section (mol/min) L=rr*D ! Vapor Flowrate in the Column (mol/min) V=L+D ! Flowrate of the Liquid in the Stripping Section (mol/min) FL=Feed+L ! Vapor Mole Fractions of Component A ! From the equilibrium assumption and mole balances ! 1) vol = (yA/xA) / (yB/xB) ! 2) xA + xB = 1 ! 3) yA + yB = 1 y[1:32] = x[1:32]*vol/(1+(vol-1)*x[1:32]) End Intermediates Equations ! condenser acond * $x[1] = V*(y[2]-x[1]) ! 15 column stages atray * $x[2:16] = L*(x[1:15]-x[2:16]) - V*(y[2:16]-y[3:17]) ! feed tray atray * $x[17] = Feed*x_Feed + L*x[16] - FL*x[17] - V*(y[17]-y[18]) ! 14 column stages atray * $x[18:31] = FL*(x[17:30]-x[18:31]) - V*(y[18:31]-y[19:32]) ! reboiler areb * $x[32] = FL*x[31] - (Feed-D)*x[32] - V*y[32] End Equations End Model

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