please help me!!

please help me in part (e) and (g)

A mixture of ethane, propane, n-butane, n-pentane, and n-hexane is to be separated to relatively pure components. a. Using heuristics propose a sequence to separbse the mixture. b. If the first column used is to recover 96% of propane in distillate and 98% of n butane as bottoms, what is the n-hexane split in this column? (Hint: Use Fenske equation and assume relative volatility for each component is constant throughout the column.) c. For the first column, what is the reboiler rate (V) if the feed is saturated vapor and reflux ratio (L/D) is 3.0 ? d. If the split fractions (referring to top product) for each component in the table are to be 1,0.96,0.02,0,0, respectively, determine the flow rates of the distillate (D) and bottoms (W), and the distillate compositions. e. If the column should operate at R/Rmin=1.5(Rmin=2.095) and N/Nmin=1.78 to meet the specifications for the previous question, determine the number of actual stages. (Hint: Use Gilliland Equation) f. Plot Reflux Ratio (RR) versus Number of Actual Trays (ACTSTAGE), Condenser Duty (CONDUTY) and Reboiler Duty (REBDUTY) in MW. g. How do the total cost (TC), capital cost (FC), and operating cost (VC) in $/yr change with respect to RR? What is the optimum RR to minimize total cost? You can use CHEMCAD to answer some parts of this question! Use the additional information below for cost analysis: For Distillation Columns, the capital cost of the whole column is considered as FC and the operating cost of the column through condenser and reboiler duties is the VC. Total Cost (TC)= Fixed Cost (FC)+ Variable Cost (VC) Purchased Equipment Cost: Cs=a+bSn where a,b : cost constants; S: size parameter; n: exponent for that type of equipment (Towler and Sinnot, 2nd Ed., 2013) - Operating Cost ($/yr)=(2.0(TotalDutyinMW)0.65)10,000 Table 7.2 Purchased Equipment Cost for Common Plant Equipment Equipment Units for Sire, S Note Dnyers Direct contact Rotary 1 Atmoepheric tray batch Spray dryer m2 arca,m2 evap rate kgh 113.0400180204,00015,00010,000410,00010,5007,9002,2000.90.50.7 Eupponators Vertical fube anca, m2 Agitated falling film 11 0.5 2 Euchampers U-tube shell and rube Floating head shell and tube Double pipe Themosiphon rcboiler U-tube Kettle reboiler Plate and frame \begin{tabular}{|lll|l|l|} 10 & 1,000 & 28,000 & 54 & 1.2 \\ 10 & 1,000 & 32,000 & 70 & 1.2 \\ 1.0 & 80 & 1,900 & 2.500 & 1.0 \\ 10 & 500 & 30,400 & 122 & 1.1 \\ 10 & 500 & 29,000 & 400 & 0.9 \\ 1.0 & 500 & 1.600 & 210 & 0.95 \end{tabular} Filters 2 Plate and frame capacity, m3 Vactum drum arca, m2 0.4 10 1.4180128,00073,00089,00093,0000.50.3 Furnaces Cylindrical Box duty, MW duty, MW Packingra 304 ss Rachig rings Coramic intalox saddles 304 ss Pall nings PVC structured packing 304 ss structured packing Pressure veuels 0.23060120000080.00043,0008.0002.0008.500109,000111,0001.01.01.01.00.80.8 Vertical, Cs Horipontal, es 1. Phent hratrd 2. Type 304 maimiers siect 3. Wich aturdice ared 350m2h '. 5. Cont per trap. bused on a shack of 30 mrive. 6. Firhar aumbly A mixture of ethane, propane, n-butane, n-pentane, and n-hexane is to be separated to relatively pure components. a. Using heuristics propose a sequence to separbse the mixture. b. If the first column used is to recover 96% of propane in distillate and 98% of n butane as bottoms, what is the n-hexane split in this column? (Hint: Use Fenske equation and assume relative volatility for each component is constant throughout the column.) c. For the first column, what is the reboiler rate (V) if the feed is saturated vapor and reflux ratio (L/D) is 3.0 ? d. If the split fractions (referring to top product) for each component in the table are to be 1,0.96,0.02,0,0, respectively, determine the flow rates of the distillate (D) and bottoms (W), and the distillate compositions. e. If the column should operate at R/Rmin=1.5(Rmin=2.095) and N/Nmin=1.78 to meet the specifications for the previous question, determine the number of actual stages. (Hint: Use Gilliland Equation) f. Plot Reflux Ratio (RR) versus Number of Actual Trays (ACTSTAGE), Condenser Duty (CONDUTY) and Reboiler Duty (REBDUTY) in MW. g. How do the total cost (TC), capital cost (FC), and operating cost (VC) in $/yr change with respect to RR? What is the optimum RR to minimize total cost? You can use CHEMCAD to answer some parts of this question! Use the additional information below for cost analysis: For Distillation Columns, the capital cost of the whole column is considered as FC and the operating cost of the column through condenser and reboiler duties is the VC. Total Cost (TC)= Fixed Cost (FC)+ Variable Cost (VC) Purchased Equipment Cost: Cs=a+bSn where a,b : cost constants; S: size parameter; n: exponent for that type of equipment (Towler and Sinnot, 2nd Ed., 2013) - Operating Cost ($/yr)=(2.0(TotalDutyinMW)0.65)10,000 Table 7.2 Purchased Equipment Cost for Common Plant Equipment Equipment Units for Sire, S Note Dnyers Direct contact Rotary 1 Atmoepheric tray batch Spray dryer m2 arca,m2 evap rate kgh 113.0400180204,00015,00010,000410,00010,5007,9002,2000.90.50.7 Eupponators Vertical fube anca, m2 Agitated falling film 11 0.5 2 Euchampers U-tube shell and rube Floating head shell and tube Double pipe Themosiphon rcboiler U-tube Kettle reboiler Plate and frame \begin{tabular}{|lll|l|l|} 10 & 1,000 & 28,000 & 54 & 1.2 \\ 10 & 1,000 & 32,000 & 70 & 1.2 \\ 1.0 & 80 & 1,900 & 2.500 & 1.0 \\ 10 & 500 & 30,400 & 122 & 1.1 \\ 10 & 500 & 29,000 & 400 & 0.9 \\ 1.0 & 500 & 1.600 & 210 & 0.95 \end{tabular} Filters 2 Plate and frame capacity, m3 Vactum drum arca, m2 0.4 10 1.4180128,00073,00089,00093,0000.50.3 Furnaces Cylindrical Box duty, MW duty, MW Packingra 304 ss Rachig rings Coramic intalox saddles 304 ss Pall nings PVC structured packing 304 ss structured packing Pressure veuels 0.23060120000080.00043,0008.0002.0008.500109,000111,0001.01.01.01.00.80.8 Vertical, Cs Horipontal, es 1. Phent hratrd 2. Type 304 maimiers siect 3. Wich aturdice ared 350m2h '. 5. Cont per trap. bused on a shack of 30 mrive. 6. Firhar aumbly