It is assumed that (1) the pressure is constant on all trays; (2) the vapor and liquid leaving each tray are in equilibrium (i.e., tray efficiency is 100%); and (3) the column is adiabatic. A treatment where variable pressure is considered is given by Choe and Luyben (1987).

The column feed, a saturated liquid, is composed of 2.5% ethane, 35% propane, 60% -butane, and 2.5% -pentane at 347.8 K. Feed flow rate is set equal to 300 kmol/hr. The feed is entered at the stage. You can choose the reflux ratio and reboiler heat duty. By default, they are set to 3.073 and kJ/hr, respectively.

Composition profiles in the column are given for ethane, propane, -butane, and -pentane in red, green, cyan, and blue, respectively. You can also see the temperature profile in Kelvin (blue curve), the equilibrium constants (for ethane, propane, -butane, and -pentane, given in red, green, cyan, and blue, respectively), and liquid and vapor flow rates in kmol/hr (liquid and vapor flow rates are the green and red curves, respectively).

The vapor and liquid molar flow rates are not constant in both the stripping and rectifying sections of the column. This justifies rigorously calculating both mass and energy balances and not assuming the usual constant molar overflow hypothesis (CMO).

The distillate bubble-point temperature is equal to 301.21 K (for the default values of the reflux ratio and reboiler heat duty), which allows the use of cold water utility in the condenser and justifies a posteriori the use of a column pressure of 16.212 bar. The condenser heat duty is determined to be equal to kJ/hr (for the default values of the reflux ratio and reboiler heat duty).

The bottom and distillate rate are 268.17 kmol/hr and 31.83 kmol/hr, respectively (for the default values of the reflux ratio and reboiler heat duty).