DistillationSummaryThis report describes the steps taken to separate a side stream of ethanol and isopropanol at 50:50 by volume. The resulting separation should contain no more than 3% alcohol impurities in each product. A laboratory column, operating at total reflux, was used to achieve a column forty feet high by one foot in diameter. The lab column allowed the team to determine vapor velocities and HETP values ​​for the 0.24-inch Pro-Pakq packing. HETP is defined as the packing height divided by the number of theoretical stages in the column. The column consisted of four main sections: packing, controls, reboiler, and condenser. To complete the vapor velocity/HETP relationship, the vapor velocity must be found. The steam velocity was determined using an energy balance of the system. The nominal steam velocity was determined to be 4.85 feet/hour. However, this steam velocity did not result in 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% of the flood rate. The HETP column was found using the Fenske equation and was determined to have an average of 4.55 inches. Due to the design parameters of the experimental column, the following design is proposed: The column will operate at a steam velocity of 4.85 ft/hr and will have a HETP of 4.30 inches. This will result in a packaging height of 38.7 feet. The reboiler will have an area of ​​113.52 ft2 and the area of ​​the condenser will have a value of 45.54 ft2 in which the heat exchange will take place.IntroductionA chemical plant spends approximately 50-90% of its capital investment on separation equipment (1,1) Therefore, the ability to use a small laboratory column and scale 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 must separate a 50:50 mixture of ethanol and isopropanol into a distillate stream containing no more than 3% by weight isopropanol and a bottoms stream containing no more than 3% by weight ethanol . The design of the full-scale column was based on a laboratory simulation column. This column allowed the team to determine the steam velocities and HETP values ​​for the 0.24-inch Pro-Pakq packing. Once the simulation vapor velocities are determined, they can ...... middle of paper ....../h)/ *(1/0.0154 kmol/L)*(1/(p(. 25)2ft2)*(0.0159 kmol/L)(p(1)2(ft)) = 6.857567 kmol/hMWAVG,D = 46.493 kg/kmolVD = (6.857567 kmol/h) * (46.493 kg /kmol)VD = 318.82886 kg/h*Upper operational line equation = (L/V)x + (1-(L/V))xD = (RACT / RACT + 1)x + (1/ RACT +1)(0.97)= 0.912779x + 0.084605*Distillate flow rateR = (VD)/D = 10.4651318.82886 (kg/h) - D = 10.4651DD = 27.808642 (kg/ h)R = L/D = 10.4651 * 27.808642 (kg/h) = LL = 291.02022 (kg/h)*Background flowL/V = R (z -xB) + q (xD - xB )R(z -xB) + q (xD-xB) -(xD-z)z= Mole fraction of feed ethanolq= 1 (feed is assumed to be 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 .05L/V = (VB + 1)/ VB = 1.05VB = 20B = V/ VB = (318.82886 kg/h)/20 = 15.941443 (kg/h)*Feed rateF = D + B = 15.941443 (kg/h) + 318.82886 (kg/h) = 334.7703 kg/h*Lower operating line = (L/V)x - ((L/V)- 1) xB = 1.05x - 0.0015* Condenser heat loadQCOND = V * DHVAPDHVAP = xETOH * DHVAP,ETOH + xISOP * DHVAP,ISOPQCOND =