DistillationAbstractThis report describes the steps taken to separate a side stream of ethanol and isopropanol 50:50 by volume. The resulting separation must contain no more than 3% alcoholic impurities in each product. A laboratory column, operated at full reflux, was used to scale up to a column forty feet high and one foot in diameter. The laboratory column allowed the team to determine vapor velocities and HETP values ​​for the 0.24-inch Pro-Pakq packing. The HETP is defined as the packing height divided by the number of theoretical column stages. The column consisted of four main sections: packing, controls, a reboiler and a condenser. To complete the relationship between vapor velocity and HETP, you need to find the vapor velocity. The velocity of the steam was found using an energy balance of the system. The design steam velocity was determined to be 4.85 ft/hr. However, this vapor velocity did not cause flooding of the column; therefore the enlarged column is not designed to exploit its full potential. Ideally, distillation columns should be designed at 70-80% flooding rate. The HETP column was found using the Fenske equation and was determined to be an average of 4.55 inches. As a result of the design parameters of the experimental column, the following design is proposed: The column will operate at a vapor velocity of 4.85 ft/hr and have a HETP of 4.30 in. This will result in a packing height of 38.7 feet. The reboiler will have an area of ​​113.52 ft2 and the condenser area will have a value of 45.54 ft2 where heat exchange will take place. IntroductionA chemical plant spends approximately 50 to 90% of its invested capital on separation equipment (1,1) Therefore, the ability to use a small laboratory column and scale up a column is an important skill for a chemical engineer. This report will describe the steps taken to design a packed distillation column. The column shall separate a 50:50 mixture of ethanol and isopropanol into a distillate stream containing no more than 3 wt% isopropanol and a bottoms stream containing no more than 3 wt% ethanol. The full-scale column design was based on a laboratory-simulated column. This column allowed the team to determine vapor rates and HETP values ​​for the 0.24-inch Pro-Pakq packaging. Once the simulation vapor velocities are determined, you can ... half of paper ....../hour)/ *(1/0.0154 kmol/L)*(1/(p(.25)2ft2 )*(0.0159 kmol/L)(p(1)2(ft)) = 6.857567 kmol/hrMWAVG,D = 46.493 kg/kmolVD = (6.857567 kmol/hr) * (46.493 kg/kmol) VD = 318.82886 kg/hour*Upper operating line equation = (L/V)x + (1-(L/V))xD = (RACT / RACT + 1)x + (1/ RACT +1)( 0.97)= 0.912779x + 0.084605*Distillate rateR = (VD)/D = 10.4651318.82886 (kg/hour) - D = 10.4651DD = 27.808642 (kg/hour)R = L /D = 10.4651 * 27.808642 (kg/hour) = LL = 291.02022 (kg/hour)*Minimum flow rateL/V = R (z -xB) + q (xD - xB)R(z -xB) ) + q (xD-xB) -(xD-z)z= Mole fraction of ethanolq= 1 (feed assumes liquid)L/V = 10.4651(0.567-0.03) + 1(0.97 -0.03)10.4651(0.567-0.03) + 1(0.97-0.03) -(0.97-0.567)L/V = 1.05 L/V = (VB + 1) / VB = 1.05VB = 20B = V/ VB = (318.82886 kg/hour)/20 = 15.941443 (kg/hour)*Feed flow rateF = D + B = 15.941443 (kg/hour) + 318.82886 (kg/hr) = 334.7703 kg/hr*Lower Operating Line = (L/V)x - ((L/V)- 1) xB = 1.05x - 0.0015* Condenser Thermal ServiceQCOND = V * DHVAPDHVAP = xETOH * DHVAP,ETOH + xISOP * DHVAP,ISOPQCOND =