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Questions and Answers of Chemical Engineering

An aqueous solution containing 10 mol% isopropanol is fed at its bubble point to the top of a continuous stripping column, operated at atmospheric pressure, to produce a vapor containing 40 mol%
Determine the optimal-stage location for each feed and the number of theoretical stages required for the distillation separation shown in Figure 7.42 using the following equilibrium data in mole
Determine the number of theoretical stages required and the optimal-stage locations for the feed and liquid side stream for the distillation process shown in Figure 7.43 assuming that methanol (M)
A mixture of n-heptane (H) and toluene (T) is separated by extractive distillation with phenol (P). Distillation is then used to recover the phenol for recycle as shown in Figure 7.44a, where the
A distillation column for the separation of n-butane from n-pentane was recently put into operation in a petroleum refinery. Apparently, an error was made in the design because the column fails to
In the production of chlorobenzenes by chlorination of benzene, two close-boiling isomers, para-dichlorobenzene (P) and ortho-dichlorobenzene (O), are separated by distillation. The feed to the
Relatively pure oxygen and nitrogen can be obtained by the distillation of air using the Linde double column, which, as shown in Figure, consists of a lower column operating at elevated pressure
The following performance data have been obtained for a distillation tower separating a 50/50 by weight percent mixture of methanol and water:Feed rate = 45,438 lb/h. Feed condition = bubble-point
For the conditions of Exercise 7.41, a laboratory Oldershaw column measures an average Murphree vapor-point efficiency of 65%. Estimate EMV and Eo.In Exercise 7.41The following performance data have
Conditions for the top tray of a distillation column are as shown in Figure 7.46. Determine the column diameter corresponding to 85% of flooding if a valve tray is used. Make whatever assumptions
A separation of propylene from propane is achieved by distillation as shown in Figure, where two columns in series are used because a single column would be too tall. The tray numbers refer to
Determine the height and diameter of a vertical flash drum for the conditions shown in Figure 7.48.
Determine the length and diameter of a horizontal reflux drum for the conditions shown inFigure.
Results of design calculations for a methanol-water distillation operation are given in Figure 7.50.(a) Calculate the column diameter at the top tray and at the bottom tray for sieve trays. Should
For the conditions given in Exercise 7.41, estimate for the top tray arid the bottom tray:(a) Percent of flooding,(b) Tray pres Weir sure drop in psi.(c) Whether weeping will occur.(d) Entrainment
If the feed rate to the tower of Exercise 7.41 is increased by 30% with all other conditions except for tower pressure drop remaining the same, estimate for the top and bottom trays:(a) Percent of
A mixture of benzene and dichloroethane is used to test the efficiency of a packed column that contains 10 ft of packing and operates adiabatically at atmospheric pressure. The liquid is charged to
Consider a distillation column for separating ethanol from water at 1 atm. The following specifications are set: Feed: 10 mol% ethanol (bubble-point liquid) Bottoms: 1 mol% ethanol Distillate: 80
An enthalpy-concentration diagram is given in Figure for a mixture of n-hcxanc (H). and n-octane (0) at 101 kPa. Using this diagram, determine the following:(a) The mole-fraction composition of the
Using the enthalpy'concentration diagram of Figure, determine the following for a mixture of n-hexane (H) and n-octane (0) at I atm:(a) The temperature and compositions of equilibrium liquid and
One hundred pound-moles per hour of a mixture of 60 mol% methanol in water at 30oC and 1 atm is to be separated by distillation at the same pressure into a liquid distillate containing 98 mol%
Explain why it is preferable to separate a dilute mixture of benzoic acid in water by liquid—liquid extraction rather than distillation.
Why is liquid—liquid extraction preferred over distillation for the separation of a mixture of formic acid and water?
Based on the information in Table 8.3 and the selection scheme in Figure 8.8, is the choice of an RDC appropriate for the extraction of acetic acid from water by ethyl acetate in the process
What is the major advantage of the ARD over the RDC? What is the disadvantage of the ARD compared to the RDC?
Under what conditions is a cascade of mixer-settler units probably the best choice of extraction equipment?
A petroleum reformate stream of 4,000 bbl/day is to be contacted with diethylene glycol to extract the aromatics from the paraflins. The ratio of solvent volume to refonnate volume is 5. It is
Using Table 8.4, select possible liquid ”liquid extraction solvents for separating the following mixtures:(a) Water”ethyl alcohol,(b) Water”aniline, and(c) Water”acetic acid. For each case,
Using Table 8.4, select possible liquid?liquid extraction solvents for removing the solute from the carrier in the following cases:
For the extraction of acetic acid (A) from a dilute solution in water (C) into ethyl acetate (5) at 25°C, estimate or obtain date for (KA)D,, (KC)D, (KS)D. and βAC. Does this system exhibit:(a)
lnterfacial tension can be an important factor in liquid— liquid extraction. Very low values of inierfacial tension result in stable emulsions that are difficult to separate, while very high values
One thousand kilograms per hour of a 45 wt% acetone in- water solution is to be extracted at 25?C in a Continuous, countercurrent system with pure 1,1 ,2-trichloroethane to obtain a raffinate
Solve Exercise 8.11 with a right-triangle diagram. In Exercise 8.11 One thousand kilograms per hour of a 45 wt% acetone in- water solution is to be extracted at 25?C in a Continuous, countercurrent
A distillate containing 45 wt% isopropyl alcohol, 50 wt% diisopropyl ether, and 5 wt% water is obtained from the heads column of an isopropyl alcohol finishing umt. The company desires to recover the
Benzene and trimethylamine (TMA) are to be separated in a three-stage liquid-liquid extraction column using water as the solvent. If the solvent-free extract and raffinate products are to contain,
The system docosane-diphenylhexane (DPH)-furfural is representative of more complex systems encountered in the solvent refining of lubricating oil. Five hundred kilograms per hour of a 40 wt% mixture
For each of the ternary systems shown in figure, indicate whether: (a) Simple, countercurrent extraction, or (b) Countercurrent extraction with extract reflux, or (c) Countercurrent extraction with
Two solutions, feed F at the rate of 7,500 kg/h containing 50 wt% acetone and 50 wt% water, and feed F' at the rate of 7,500 kg/h containing 25 wt% acetone and 75 wt% water, are to be extracted in a
The three-stage extractor shown in Figure 8.44 is used to extract the arnine from a fluid consisting of 40 wt% benzene (B) and 60 wt% trimethylamine (T). The solvent (water) flow to stage 3 is 5,185
The extraction process shown Figure 8.45 is conducted in a multiple-feed, countercurrent unit without extract or raffinate reflux. Feed F' is composed of solvent and solute, and is an extractphase
A mixture containing 50 wt% methylcyclohexane (MCH) in n-heptane is fed to a countercurrent, stage-type extractor at 25°C. Aniline is used as solvent. Reflux is used on both ends of the column. An
In its natural state, zirconium, which is an important material of construction for nuclear reactors, is associated with hafnium, which has an abnormally high neutron-absorption cross section and
At 45oC, 5,000 kg/h of a mixture of 65 wt% docosane, 7 wt% furfural, and 28 wt% diphenylhexane is to be extracted with pure furfural to obtain a raffinate with 12 wt% diphenylhexane in a continuous,
At 45oC, 1,000 kg/h of a mixture of 0.80 mass fraction docosane and 0.20 mass fraction diphenylhexane is to be extracted with pure furfural to remove some of the diphenylhexane from the feed.
A liquid mixture of 27 wt% acetone and 73 wt% water is to be separated at 25oC into a raffinate and extract by multistage, steady-state, countercurrent liquid-liquid extraction with a solvent of pure
A feed mixture containing 50 wt% n-heptane and 50 wt% methylcyclohexane (MCH) is to be separated by liquid-liquid extraction into one product containing 92.5 wt% methylcyclohexane and another
Two liquids, A and B, which have nearly identical boiling points, are to be separated by liquid-liquid extraction with solvent C. The following data represent the equilibrium between the two liquid
Solve Exercise 8.20 by the graphical method of Maloney and Schubert.In Exercise 8.20:A mixture containing 50 wt% methylcyclohexane (MCH) in n-heptane is fed to a countercurrent, stage-type extractor
Acetic acid is continuously extracted from a 3 wt% dilute solution in water with a solvent of isopropyl ether in a mixer-settler unit. The flow rates of the feed and solvent are 12,400 and 24,000
A cascade of six mixer-settler units is available, each unit consisting of a 10-ft-diameter by 10-ft-high mixing vessel equipped with a 20-hp agitator, and a 10-ft-diameter by 40-ft-long settling
Acetic acid is to be extracted from a dilute aqueous solution with isopropyl ether at 25oC in a countercurrent cascade of mixer-settler units. In one of the units, the following conditions
For the conditions of Exercise 8.30, estimate:(a) Sauter mean drop size,(b) Range of drop sizes, and(c) Interfacial area of the two-phase liquid-liquid emulsion.
For the conditions of Exercises 8.30 and 8.31, and the additional data given below, estimate:(a) The dispersed-phase mass-transfer coefficient,(b) The continuous-phase mass-transfer coefficient,(c)
For the conditions and results of Example 8.4, involving the extraction of benzoic acid, from a dilute solution in water with toluene, determine the following when using a six-flat-blade turbine
Estimate the diameter of an RDC column to extract acetic acid from water with isopropyl ether for the conditions and data of Exercises 8.28 and 8.30.
Estimate the diameter of a Karr column to extract benzoic acid from water with toluene for the conditions of Exercise 8.33.
Estimate the value of HETS for an RDC column operating under the conditions of Exercise 8.34.
Estimate the value of HETS for a Karr column operating under the conditions of Exercise 8.35
A mixture of propionic and n-butyric acids, which can be assumed to form ideal solutions, is to be separated by distillation into a distillate containing 95 mol% propionic acid and a bottoms product
A sequence of two distillation columns is to be used to produce the products indicated in figure. Establish the type of condenser and an operating pressure for each column for:(a) The direct sequence
For each of the two distillation separations (D-1 and 0-2) indicated in Figure 9.20, establish the type of condenser and an operatingpressure.
A deethanizer is to be designed for the separation indicated in figure. Estimate the number of equilibrium stages required, assuming it is equal to 2.5 times the minimum number of equilibrium stages
For the complex distillation operation shown in figure 9.22, use the Fenske equation to determine the minimum number of stages required between:(a) The distillate and feed,(b) The feed and the side
A 25 mol% mixture of acetone (A) in water (W) is to be separated by distillation at an average pressure of 130 kPa into a distillate containing 95 mol% acetone and a bottoms containing 2 mol%
For the distillation operation indicated in figure, calculate the minimum number of equilibrium stages and the distribution of the nonkey components by the Fenske equation,
For the distillation operation shown in figure, establish the type of condenser and an operating pressure, calculate the minimum number of equilibrium stages, and estimate the distribution of the
For 15 minimum equilibrium stages at 250 psia, calculate and plot the percent recovery of C3 in the distillate as a function of distillate flow rate for the distillation of 1,000 lbmol/h of a feed
Use the Underwood equations to estimate the minimum external-reflux ratio for the separation by distillation of 30 mol% propane in propylene to obtain 99 mol% propylene and 98 mol% propane, if the
For the conditions of Exercise 9.7, compute the minimum external-reflux rate and the distribution of the nonkey components at minimum reflux by the Underwood equation if the feed is a bubble-point
Calculate and plot the minimum-external-reflux ratio and the minimum number of equilibrium stages against percent product purity for the separation by distillation of an equimolar bubble-point liquid
Use the Fenske-Underwood-Gilliland shortcut method to determine the reflux ratio required to conduct the distillation operation indicated in figure if NI Nmin = 2.0, the average relative volatility =
A feed consisting of 62 mol% para-dichlorobenzene in ortho-dichlorobenzene is to be separated by distillation at near atmospheric pressure into a distillate containing 98 mol% para isomer and bottoms
Explain why the Gilliland correlation can give erroneous results for cases where the ratio of rectifying to stripping stages is small.
The hydrocarbon feed to a distillation column is a bubblepoint liquid at 300 psia with the mole fraction composition, C2 = 0.08, C3 = 0.15, nC4 = 0.20, nC5 = 0.27, nC6 = 0.20, and nC7 = 0.10.
The following feed mixture is to be separated by ordinary distillation at 120 psia so as to obtain 92.5 mol% of the nC4 in the liquid distillate and 82.0 mol% of the iC5 in the bottoms.(a) Estimate
Consider the separation by distillation of a chlorination effluent to recover C2H5Cl. The feed is a bubble-point liquid at the column pressure of 240 psia with the following composition and K-values
One hundred kilogram-moles per hour of a three-component bubble-point mixture to be separated by distillation has the following composition:(a) For a distillate rate of 60kmol/h, five theoretical
For the conditions of Exercise 9.6, determine the ratio of rectifying to stripping equilibrium stages by:(a) Fenske equation,(b) Kirkbride equation, and(c) McCabe—Thiele diagram. Discuss your
Starting with equations like (5-46) and (5-47), show that for two stages,
Determine by the Kremser group method the separation that can be achieved for the absorption operation indicated in figure for the following combinations of conditions:(a) Six equilibrium stages and
One thousand kilogram-moles per hour of rich gas at 70°F with 25% C1, 15% C2, 25% C3, 20% nC4, and 15% nC5 by moles is to be absorbed by 500 kmol/k of nC10 at 90°F in an absorber operating at 4
For the flashing and stripping operation indicated in figure, determine by the Kremser group method the kilogram-moles per hour of steam if the stripper is operated at 2 atm and has five
A stripper operating at 50 psia with three equilibrium stages is used to strip 1,000 kmol/h of liquid at 250°F having the following molar composition: 0.03% C1, 0.22% C2, 1.82% C3, 4.47% nC4, 8.59%
One hundred kilogram-moles per hour of an equimolar mixture of benzene (B), toluene (T), n-hexane (C6), and n-heptane (C7) is to be extracted at 150°C by 300 kmol/h of diethylene glycol (DEG) in a
A reboiled stripper in a natural-gas plant is to be used to remove mainly propane and lighter components from the feed shown in figure. Determine by the group method the compositions of the vapor and
A mixture of ethylbenzene and xy lenes is to be distilled as shown in figure 9.29. Assuming the applicability of Raoult's and Dalton's laws:(a) Use the Fenske-Underwood-Gilliland method to estimate
Show mathematically that (10-6) is not independent of (l0-1), (l0-3), and(10-4).
Revise the MESH equations to account for entrainment, occlusion, and chemical reaction.
Revise the MESH equations (10-1) to (10-6) to allow for pumparounds of the type shown in Figure and Combine the equations to obtain modified M equations similar to (10.7). Can these equations still
Use the Thomas algorithm to solve the following matrix equation for xI, x2, and x3.
Use the Thomas algorithm to solve the following tridiagonal matrix equation for the xvector.
Wang and Henke [1] claim that their method of solving the tridiagonal matrix for the liquid-phase mole fractions does not involve subtraction of nearly equal quantities. Prove or disprove their
Derive an equation similar to (10-7), but with vi, j = yi, jVj, as the variables instead of the liquid-phase mole fractions. Can the resulting equations still be partitioned into a series of C
In a computer program for the Wang—Henke bubble-point method, 10,100 storage locations are wastefully set aside for the four indexed coefficients of the tridiagonal-matrix solution of the component
Solve by the Newton'Raphson method the simultaneous, nonlinear equationsfor x, and x2 to within f 0.001. As initial guesses, assume(a) x1 = 2, x2 = 5.(b) xl = 4, x2 = 5.(c) xl = 1, x2 = 1.(d) x1 = 8,
Solve by the Newton-Raphson method the simultaneous, nonlinear equationsfor x1 and x2 to within + 0.001. As initial guesses, assume(a) x1 = 0.4, x2 = 0.9.(b) x1 = 0.6, x2 = 0.9.(c) x1 = 1.0, x2 =1.0.
One thousand kilogram-moles per hour of a saturated liquid mixture of 60 mol% methanol, 20 mol% ethanol and 20 mol% n-propanol is fed to the middle stage of a distillation column having three
Solve the following nine simultaneous linear equations, which have a block tridiagonal matrix structure, by the Thomasalgorithm.
Naphtali and Sandholm group the N(2C + 1) equations by stage. Instead, group the equations by type (i.e., enthalpy balances, component balances, and equilibrium relations). Using a three-component,
Derivatives of properties are needed in the Naphtali-Sandholm SC method. For the Chao-Seader correlation, determine analytical derivativesfor

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