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Questions and Answers of
Chemical Engineering
Structured packings work very well in vacuum and atmospheric pressure distillation columns, but sometimes structured packings do not work well in high-pressure columns. What is different about
The original publication of Figure 10-15 (Fair and Matthews, 1958) did not cite any equations, and equations probably were not available, but when the curves were fit statistically, Eqs (10-10) were
Refer to Table 10-4.a. Which is more desirable, a high or low packing factor, \(\mathrm{F}\) ?b. As packing size increases, does \(\mathrm{F}\) increase or decrease? What is the functional form of
Distillation columns have been installed on ships. What are the likely effects of the ship's motion on the performance of the distillation column? Would you recommend use of random packing,
One type of valve is shown in Figure 10-1. Brainstorm alternative ways in which valves could be designed.Figure 10-1
Generate other ways of contacting in packed columns.
a. A farmer friend of yours is going to build his own distillation system to purify ethanol made by fermentation. He wants to make his own packing. Suggest 30 different things he could make or buy
If trays are good, random packing is good, and structured packing is good, why not combine them? Think of at least ten ways you might do this.
Develop a spreadsheet for a simple binary Rayleigh distillation that uses Eq. (9-13) but can be used for systems where \(\alpha\) is not constant. Because \(\alpha\) is not constant, calculate the
Solve Example 9-2 with a spreadsheet using Eq. (9-18) over the following ranges of methanol mole fraction: 1.0 to \(0.9,0.9\) to \(0.7,0.7\) to \(0.5,0.5\) to 0.3 , and 0.3 to 0.1 . *Answers are in
We wish to do a constant mole batch distillation of 100 moles of feed that is pure water \(\left(x_{W}=1\right)\) to exchange the solvent to obtain the nonvolatile solute in a mixture that is 0.01
Challenging! Develop a spreadsheet with VBA to solve the following problem. A simple batch distillation of the system n-butane, n-pentane, and n-hexane is planned. \(1.0 \mathrm{kmol}\) of a feed
We are doing a single-stage, batch steam distillation of 1-octanol. The unit operates at \(760 \mathrm{~mm} \mathrm{Hg}\). The batch steam distillation is operated with liquid water present. The
We are separating 100 moles of a feed that is \(60.0 \mathrm{~mol} \%\) methanol and \(40.0 \mathrm{~mol} \%\) water by batch distillation in a system with a still pot and a column that has one
In inverted batch distillation (Diwekar, 1995; Robinson and Gilliland, 1950; Sorensen, 2014) the charge of feed is placed in the accumulator at the top of the column (Figure 9-9). Liquid is fed to
A nonvolatile solute is dissolved in \(1.0 \mathrm{kmol}\) of methanol. We wish to switch the solvent to water. Because the solution is already concentrated, a first batch distillation to concentrate
A simple batch distillation is used to process \(1.0 \mathrm{kmol}\) of methanol-water feed into three distillate fractions and a waste. The initial feed has \(\mathrm{x}_{F, \mathrm{M}}=\) 0.50 mole
A simple batch distillation separates \(0.6 \mathrm{kmol}\) of a binary feed that is 70.0 \(\mathrm{mol} \%\) methanol and \(30.0 \mathrm{~mol} \%\) water. The final still pot is \(10.0 \mathrm{~mol}
A simple batch still (one equilibrium stage) separates 100 moles of a 10.0 \(\mathrm{mol} \%\) methanol and \(90.0 \mathrm{~mol} \%\) water feed. The final bottoms concentration is \(1.0
A distillation system with a still pot plus a column with one equilibrium stage is used to batch distill \(1.0 \mathrm{kmol}\) of a \(57.0 \mathrm{~mol} \%\) methanol and 43.0 \(\mathrm{mol} \%\)
A simple batch distillation (Figure 9-1) is separating \(8.00 \mathrm{kmol}\) of a feed that is \(40.0 \mathrm{~mol} \%\) water and \(60.0 \mathrm{~mol} \% \mathrm{n}\)-butanol. The batch
\(3.0 \mathrm{kmol}\) of feed containing \(52.0 \mathrm{~mol} \%\) water and \(48.0 \mathrm{~mol} \% \mathrm{n}\)-butanol is charged to the still pot of a simple batch distillation system (Figure
A simple batch still is separating a feed that is \(60.0 \mathrm{~mol} \% 1,2\) dichloroethane and \(40.0 \mathrm{~mol} \%\) 1,1,2-trichloroethane. Pressure is \(1 \mathrm{~atm}\). The relative
A batch distillation system with a still pot and one equilibrium stage (two equilibrium contacts total) distills a feed that is \(10.0 \mathrm{~mol} \%\) water and \(90.0 \mathrm{~mol} \%
\(10.0 \mathrm{kmol}\) of a feed with \(\mathrm{x}_{\mathrm{F}}=0.4\) (mole fraction methanol) and the remainder water is sent to a batch distillation system with a large still pot that is an
We wish to batch distill a mixture of 1-butanol and water. This system has a heterogeneous azeotrope (see Chapter 8), so we use the system shown in Figure 9-10. The bottom liquid layer from the
4.0 kmoles of a feed that is 0.60 mole fraction acetone and 0.40 mole fraction ethanol is batch distilled in a system with a still pot (an equilibrium contact), a column that acts as one equilibrium
A constant-mole batch distillation is used to change from a pure nbutanol solvent to a solvent that is \(60.0 \mathrm{~mol} \% \mathrm{n}\)-butanol and \(40.0 \mathrm{~mol} \%\) water. If the initial
A nonvolatile pharmaceutical is dissolved in a solution that is \(90.0 \mathrm{~mol} \%\) acetone and \(10.0 \mathrm{~mol} \%\) ethanol. A constant volume batch distillation is used to switch the
Repeat Problem 9.D4 except use Figure 9-10 as long as the distillate is in the two-phase region and then convert to simple batch distillation by bypassing the liquid-liquid settler. Compare the
Suppose you are doing a batch steam distillation of a mixture that has two volatile organic compounds, n-octane and \(n\)-decane, that are immiscible in water plus a nonvolatile organic compound that
\(12.0 \mathrm{kmole}\) of a mixture \(40 \mathrm{~mol} \%\) water and \(60 \mathrm{~mol} \% \mathrm{n}\)-butanol at 1.0 atm pressure is batch distilled in a system with an equilibrium still pot and
\(10.0 \mathrm{kmol}\) of a \(40.0 \mathrm{~mol} \%\) methanol and \(60.0 \mathrm{~mol} \%\) water mixture is processed in a normal batch distillation system with a still pot that acts as an
A nonvolatile solute is dissolved in \(1.0 \mathrm{kmol}\) of methanol. We wish to have the solute in \(1.0 \mathrm{kmol}\) of solution that is \(99.0 \mathrm{~mol} \%\) water and 1.0 \(\mathrm{mol}
A differential condensation [see Eq. ( \(9-15)\) ] is done for a binary mixture of ethanol and water. The feed is \(0.50 \mathrm{kmol}\) of vapor that is \(10.0 \mathrm{~mol} \%\) ethanol. The
\(1.5 \mathrm{kmol}\) of feed one that is \(40.0 \mathrm{~mol} \%\) methanol and \(60.0 \mathrm{~mol} \%\) water and \(1.0 \mathrm{kmol}\) of feed two that is \(20.0 \mathrm{~mol} \%\) methanol and
\(10.0 \mathrm{kmole}\) of a \(40.0 \mathrm{~mol} \%\) methanol and \(60.0 \mathrm{~mol} \%\) water mixture is batch distilled. The system consists of a column with two equilibrium stages, a still
Repeat Problem 9.D20 but for a distillation column with 30 stages. Think smart and this problem is less work than Problem 9.D20.Data From Problem 9.D20. D20. 10.0 kmole of a 40.0 mol% methanol and
\(5.0 \mathrm{kmol}\) of \(60.0 \mathrm{~mol} \%\) methanol and \(40.0 \mathrm{~mol} \%\) water are batch distilled in a system with a still pot and a column with one equilibrium stage (two
\(1.2 \mathrm{kmol}\) of a \(10.0 \mathrm{~mol} \%\) ethanol and \(90.0 \mathrm{~mol} \%\) water feed is processed in a simple batch distillation system that consists of a still pot, a total
Repeat all parts of Example 9-2, but determine \(\mathrm{S}\) by dividing Simpson's rule in two parts: from \(\mathrm{x}=1.0\) to \(\mathrm{x}=0.2\), and from \(\mathrm{x}=0.2\) to
In Problem 9.D23, fractions were collected from ethanol mole fractions \(\mathrm{x}_{\mathrm{F}}=0.10\) to \(\mathrm{x}_{\mathrm{W} 1}=0.07\), from \(\mathrm{x}_{\mathrm{W} 1}\) to
We want to use Eq. (9-14) to generate binary distillation residue curves for the system isopropanol (IPA)-water. The first step is to compare the fit of Eq. (9-14) ( \(\mathrm{a}\) and \(\mathrm{b}\)
Why is the still pot in Figure 9-2B much larger than the column?Figure 9-2B V+Y+1 DA -D,XD Ljxj QR W,XW
In the derivation of the Rayleigh equation:a. In Eq. (9-4a), why do we have \(-x_{D} d W\) instead of \(-x_{D} d D\) ?Eq (9-4a)b. In Eq. (9-4a), why is the left-hand side \(-x_{D} d W\) instead of
If you have a steam distillation system with immiscible organic and water phases plus a vapor phase, two volatile organic compounds plus a nonvolatile organic compound, at equilibrium how many
Suppose you have two feeds containing methanol and water that you want to batch distill. One feed is \(60.0 \mathrm{~mol} \%\) methanol, and the other is \(32.0 \mathrm{~mol} \%\) methanol. How do
If we are doing a batch distillation of a heterogeneous azeotrope system, when would we employ a system similar to Figure 9-1, and when would we employ a system similar to Figure 9-10 (in Problem
List all the different ways a binary batch or inverted batch problem can be specified. Which of these will be trial and error?
What can be done if an existing batch system cannot produce the desired values of \(\mathrm{x}_{\mathrm{D}}\) and \(\mathrm{x}_{\mathrm{W}}\) even at total reflux? Generate ideas for both operating
Develop ideas for how you would reprocess or utilize the offcuts from a batch distillation that collects fractions.
For a binary multistage batch distillation with constant \(\mathrm{x}_{\text {dist }}\), prove that the mass balances over the entire batch period and the Rayleigh equation both give Eq. (
Assume that holdup in the column and in the total reboiler is negligible in an inverted batch distillation (Figure 9-9).Figure 9-9a.* Derive the appropriate form of the Rayleigh equation.b. Derive
If relative volatility can be assumed constant over the change in concentration for each fraction, Eq. \((9-13)\) can be adapted to the collection of fractions from a simple binary batch
Suppose you want to do a constant mole distillation to change solvents. The solute is nonvolatile and the equilibrium between the two solvents is \(\mathrm{y}=\mathrm{x}\). Can you do a constant mol
A distillation column separates \(100.0 \mathrm{kmol} /\) day of a saturated liquid feed that is \(20.0 \mathrm{~mol} \%\) ethanol (E), \(35.0 \mathrm{~mol} \% \mathrm{n}\)-propanol (P), and \(45.0
We are separating \(100.0 \mathrm{kmol} / \mathrm{h}\) of a saturated liquid feed that is 45.0 \(\mathrm{mol} \%\) propane \((\mathrm{P}), 15.0 \mathrm{~mol} \%\) n-butane \((B)\), and \(40.0
We are separating a mixture of propylene, propane, and isobutane in a distillation column with a partial condenser and a partial reboiler at a pressure of 15.0 bar. We desire a 0.999 fractional
Separation of propylene from propane is a very important but expensive distillation. Your boss wants to know the effect of changing the column pressure on the number of stages and on the temperature
A special column acts as exactly three equilibrium stages. Operating at total reflux, we measure vapor composition leaving the top stage and the liquid composition leaving the bottom stage. The
Separate 1,2-dichloroethane from 1,1,2-trichloroethane at 1 atm. Distillate is \(99.15 \mathrm{~mol} \%\) 1,2-dichloroethane, and bottoms is 1.773 \(\mathrm{mol} \%\) 1,2-dichloroethane. Saturated
A distillation column will separate \(100.0 \mathrm{kmol} / \mathrm{h}\) of a saturated liquid feed at \(200 \mathrm{kPa}\) that is \(20.0 \mathrm{~mol} \%\) propane (Pro), \(35.0 \mathrm{~mol} \%\)
A mixture of acetone and ethanol is distilled at \(1.0 \mathrm{~atm}\) in a distillation column with a total condenser and a partial reboiler. We desire a distillate that is 0.999 mole fraction
Your boss wants some idea of how expensive it will be to distill 155.0 \(\mathrm{kmol} / \mathrm{h}\) of a saturated liquid feed that is \(5.0 \mathrm{~mol} \%\) methane, \(10.0 \mathrm{~mol} \%\)
We wish to separate a mixture of \(40.0 \mathrm{~mol} \%\) benzene and \(60.0 \mathrm{~mol} \%\) ethylene dichloride in a distillation column with a partial reboiler and a total condenser. The feed
We are separating a mixture of benzene, toluene, and xylene in a distillation rectifying column. The column has a total condenser and no reboiler. The feed is a saturated vapor that is fed into the
When is a non-key distributing, and when is it nondistributing? For almost all chemicals, five 9 s purity \{concentrations of impurity below \(10.0 \mathrm{ppm}\), mass (mass fraction \(
We simulate a distillation column and find we can obtain the desired separation with 31 stages plus a partial reboiler and a total condenser if we use an \(L / D=3\). With total reflux, we find that
A distillation column is separating toluene and xylene, \(\alpha=3.03\). The feed is a saturated liquid, and reflux is returned as a saturated liquid. \(p\) \(=1.0 \mathrm{~atm} . \mathrm{F}=100.0
We have a column separating benzene, toluene, and cumene. The column has a total condenser, a total reboiler, and nine equilibrium stages. The feed is \(25.0 \mathrm{~mol} \%\) benzene, \(30.0
A distillation column is separating \(100.0 \mathrm{kmol} / \mathrm{h}\) of a saturated vapor feed that is \(30.0 \mathrm{~mol} \%\) ethanol, \(25.0 \mathrm{~mol} \% \mathrm{i}\)-propanol, \(35.0
A distillation column operating at \(200 \mathrm{kPa}\) separates \(100 \mathrm{kmol} / \mathrm{h}\) of a saturated liquid feed at \(200 \mathrm{kPa}\) that is \(20 \mathrm{~mol} \%\) propane (Pro),
A distillation column is separating benzene ( \(\alpha=2.25\) ), toluene ( \(\alpha=\) \(1.00)\), and cumene ( \(\alpha=0.21\) ). The column is operating at \(101.3 \mathrm{kPa}\). The column has a
We are separating a mixture of ethanol and n-propanol. Ethanol is more volatile, and the relative volatility is approximately constant at 2.10. The feed flow rate is \(1000.0 \mathrm{kmol} /
A depropanizer has the following feed and constant relative volatilities:Methane \((M): z_{M}=0.229, \alpha_{M-P}=9.92\)Propane \((\mathrm{P}): \mathrm{z}_{\mathrm{P}}=0.368,
A distillation column with a partial reboiler and a total condenser operating at \(7.0 \mathrm{bar}\) is separating \(100.0 \mathrm{kmol} / \mathrm{h}\) of a saturated liquid feed that is \(25.0
Why is water often used as a solvent in extractive distillation?
Derive Eq. (8-14) for the two-column, binary heterogeneous azeotrope system.Equation (8-14) Ybut strip but in w -[(strip strip-1]Xbut in w,bot.strip
Separate a mixture of pyridine \(\left(\mathrm{C}_{5} \mathrm{H}_{5} \mathrm{~N}\right)\) and water, which form a homogeneous azeotrope, by using extractive distillation using bisphenol-A
Develop plots for vapor pressure of water and n-decane. For water, two plots are useful in the range of values in Table 8-1. A plot of VP versus T is convenient for rapid estimates but is not as
We wish to separate two organics that form a homogeneous azeotrope. This will be done in a two-column azeotropic system with water as the solvent. Sketch possible system arrangements to do this.
Generation of distillation curves for systems with constant relative volatility is fairly straightforward and an excellent learning experience. Generate distillation curves in Figure 8-10 for a
Set up a two-stage countercurrent continuous steam distillation as shown in Figure 8-7B, solve Example 8-2 for a two-stage countercurrent process, and determine the energy savings compared to a
The following statement is made after Eq. (8-21): "If \(\mathrm{D}_{2}\) is large, Eq. (8\(21 \mathrm{~A}\) ) indicates that \(\mathrm{D}_{1}\) must also be large." Why does \(\mathrm{D}_{2}\) and
Derive an equation for \(\alpha_{\text {org-w in w }}\) similar to Eq. (8-8). Compare the predicted equilibrium in water with the butanol-water equilibrium data given in Problem 8.D3. Comment on the
Your company plans to produce pure acetone from a mixture of acetone, methyl ethyl ketone, and methyl isobutyl ketone in an ordinary single-feed distillation column with a total condenser and a
We are conducting a reaction/separation in a distillation column for the reversible reaction \(\mathrm{A}+\mathrm{B}=\mathrm{C}+\mathrm{D}\) where \(\mathrm{A}\) and \(\mathrm{B}\) are reactants and
Nitromethane and water are separated in a stripping column that has a partial reboiler. There is no condenser and no liquid-liquid settler. The saturated liquid feed is \(8.0 \mathrm{~mol} \%\)
VLE data for water and n-butanol at \(1.0 \mathrm{~atm}\) are given in Table 8-5. The fresh feed is \(100.0 \mathrm{kmol} / \mathrm{h}\) of saturated liquid that is \(30.0 \mathrm{~mol} \%\) water.
Why is a cooler required in Figure 8-14? How can this energy be reused in the process?Figure 8-14 A Product Feed Solvent Recycle Cooler B B Make up Solvent 2 B Product
For a binary heterogeneous azeotrope separation, feed can be introduced into the liquid-liquid separator. In this case two stripping columns are used.a. Sketch the column arrangement.b. Draw the
We will use a system similar to Figure 8-5A, except both columns have direct reflux from their condensers in addition to reflux from a decanter. Distill a feed that is \(17.0 \mathrm{~mol} \%\) water
VLE data for water and n-butanol are given in Table 8-5. We have flash distillation systems separating \(100.0 \mathrm{kmol} / \mathrm{h}\) of two different water and \(\mathrm{n}-\) butanol
Produce pure water from seawater by boiling it with n-decane vapor (see figure). This is sort of the reverse of steam distillation. Seawater is roughly \(3.5 \mathrm{wt} \%\) salt, which can be
Explain the purpose of the liquid-liquid settler in Figures 8-3A, 8-5A, and 8-17.Figure 8-3AFigure 8-5AFigure 8-17 V in Feed V L Dry Organic Organic Phase A Water Phase
The following statement appears after Eq. (8-27): "Equation (8-27) also proves that the points representing bottoms, distillate, and the feed all lie on a straight line. . ." Prove that this
The system water-acetonitrile \(\left(\mathrm{C}_{2} \mathrm{H}_{3} \mathrm{~N}\right)\) forms an azeotrope. This system can be separated using a two-pressure distillation system. Both columns have
The VLE data for formic acid \(\left(\mathrm{CH}_{2} \mathrm{O}_{2}\right)\)-water are presented in Table 8-6.a. Determine the value of \(\alpha\) at each data point from
In this chapter, some of the operating lines pass through the equilibrium curve and are used on the outside of the equilibrium curve. Explain how this is possible.
Sketch the flowsheet for pressure-swing distillation of a binary system with a maximum boiling azeotrope. After you have finished, you can check your flowsheet with the simplified flowsheet
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