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engineering
chemical engineering
Questions and Answers of
Chemical Engineering
Equilibrium data for extraction of methylcyclohexane (A) from nheptane (D) into aniline (S) are given in Table 13-8. Compare batch extractions of \(20 \mathrm{~kg}\) of \(40 \mathrm{wt} \%\)
Your supervisor decides to test the newly hired engineer with a problem that you have not seen before. Recover p-xylene as the center cut (Figure 13-6) from a feed that is \(50.0 \mathrm{wt} \%
Do Lab 12 in this chapter's appendix, but for three-stage systems. Operation is at \(293 \mathrm{~K}, 1.0 \mathrm{~atm}, \mathrm{~F}=10 \mathrm{kmol} / \mathrm{h}\) and is \(10 \mathrm{~mol} \%\)
Input the DECHEMA coefficients in Aspen Plus from Table 13-A1 in the appendix. Then in Properties, have Aspen print out the triangular diagram for the triethylamine, carbon-tetrachloride, acetic-acid
Use Aspen Plus Analysis to develop and print out ternary diagrams for the system water-chloroform-acetone using NRTL as the LLE correlation. Compare results to experimental data in Table 13-A2 (mole
Although not absolutely necessary, a spreadsheet using nothing fancier than Goal Seek or Solver will reduce the calculation burden of this design problem significantly.Your boss requests a
Develop your key relations chart for this chapter. Remember that a key relations chart is not a core dump but is selective.
How do the ideas of a general McCabe-Thiele procedure and the concept of unit operation relate to each other?
Washing clothes is most similar to large-scale washing when (select the best answer)a. the clothes are washed by hand.b. the clothes are washed with detergent but no soap.c. the clothes are washed
In leaching, the final saturated raffinate often contains a significant amount of solvent. For example, this occurs in Example 14-2. How do you recover this solvent?Example 14-2 We wish to treat
How does solid enter into washing calculations? Where does solids flow rate implicitly appear in Figure 14-1? Feed U, xo A Mixer Settler B Underflow Stage I Overflow 0112 Stage 2 U | 2 N-1 N Uo,xo xj
The simulated countercurrent process for leaching is shown in Figure 14-6. Convert this figure to the appropriate nomenclature for washing. BI 0 Step N F A Extract Solvent 2 Load E D 1. Dump Step N +
Show how Figure 14-8 could be modified to use a temperature swing instead of a pressure swing. What might be advantages and disadvantages of doing this? Solid Bed PH Turbo- expander PL SCF Compressor
What are some of the properties you would look for in a good solvent for extraction, leaching, and supercritical extraction?
Would you expect stage efficiencies to be higher or lower in leaching than in supercritical extraction? Explain.
With any model (McCabe-Thiele, Kremser, triangular diagram, computer simulation, mass transfer analysis), you should ask how well the model captures key aspects of the physical situation. For staged
In Example 14-2 and Figure 14-5, we plotted solute mole fractions on the ordinate and solvent mole fractions on the abscissa (x-axis). Instead, we could have plotted solid mole fractions
Because the feed underflow in Example 14-1 was not the same as in the other stages, we had to do the feed stage calculation separately, but connected to, the calculation for the remainder of the
Derive Eq. (14-14) and the form of this equation if the system is very dilute. Y = (Fsolid/Fsolv) X+Y-(Fsolid /Fsolv)X0
Adapt the Kremser equation to leaching with constant flow rates.
Derive Eq. (14-15a) and the corresponding equation for \(\mathrm{x}_{\mathrm{D}, \mathrm{M}}\).(14--15a) XA.M EOYA,0 + FXA,N+1 EO+F 0+(1000) (0.2) 662+1000 = 0.120
Develop procedures for single-stage and crossflow systems for leaching using a triangular diagram. Hint: Study Section 13.9.
a.Sketch possible arrangements for the piping and valves for Figure 14-6. Note that every tank needs to be able to receive fresh washwater or overflow from the next higher letter tank, except for
A countercurrent system with three equilibrium stages is to be used for water-acetic acid-isopropyl ether extraction (see Table 13-7). Feed is \(40 \mathrm{wt} \%\) acetic acid and \(60 \mathrm{wt}
We want to solve Example 13-6 with a multicomponent computer program similar to absorption and stripping programs. Set up the tridiagonal matrix for the mass balances assuming there are six stages in
Plot equilibrium data from Table 13-A1 for tri-ethylamine (solvent), carbon tetrachloride (solute), acetic acid (diluent) on a right triangle diagram with ordinate \(=\) mole fraction
Find number of stages needed for a countercurrent extractor if 10 \(\mathrm{kmol} / \mathrm{h}\) feed that is \(10 \mathrm{~mol} \% \mathrm{CCl}_{4}\) and \(90 \mathrm{~mol} \%\) acetic acid is
The horizontal settler calculation in Example 13-7 was done for a settler diameter of \(\mathrm{D}_{\mathrm{s}}=1.023 \mathrm{~m}\) with the dispersion band assumed to be at the center of the circle.
Suppose in Example 13-7 that we decide to build the settler with a diameter of \(1.0 \mathrm{~m}\) and a length of \(4.0 \mathrm{~m}\). What safety factor are we employing?Example 13-7 Design a
For the toluene-water system in Example 13-7, we found toluene is the dispersed phase if \(\mathrm{Q}_{\text {solvent }} / \mathrm{Q}_{\text {feed }}=0.2\). Which phase is dispersed ifa.
In Example 13-1, we assumed we were going to use all available solvent. There are other alternatives. Determine if the following alternatives are capable of producing outlet water of desired acetic
A countercurrent extraction system extracts furfural from water into methyl-isobutyl ketone (MIBK) at \(25^{\circ} \mathrm{C}\). Aqueous feed contains 0.0011 wt. fraction furfural and has a feed rate
Use chloroform to extract acetone from water. Equilibrium data are given in Table 13-6. Find number of equilibrium stages required for a countercurrent cascade if feed is \(1000.0 \mathrm{~kg} /
We are extracting pyridine from \(500 \mathrm{~kg} / \mathrm{h}\) of a feed that is \(15.0 \mathrm{wt} \%\) pyridine and \(85.0 \mathrm{wt} \%\) water using \(225 \mathrm{~kg} / \mathrm{h}\) of pure
The equilibrium for extraction of acetic acid from water into 3heptanol at \(25^{\circ} \mathrm{C}\) is \(\mathrm{y}=0.828 \mathrm{x}\), where \(\mathrm{y}\) is weight fraction acetic acid in
Equilibrium for extraction of acetic acid from 3-heptanol into water at \(25^{\circ} \mathrm{C}\) is \(\mathrm{y}=1.208 \mathrm{x}\), where \(\mathrm{y}=\) weight fraction acetic acid in water and
We are extracting acetic acid from water into 3 -heptanol at \(25^{\circ} \mathrm{C}\) in an extraction column with 30 equilibrium stages. Equilibrium is \(y=0.828\) \(\mathrm{x}\), where
A crossflow extraction system is being used to extract furfural from water into methyl-isobutyl ketone (MIBK) at \(25^{\circ} \mathrm{C}\). The \(9000 \mathrm{~kg} / \mathrm{h}\) of aqueous feed
Solve part a of Example 13-2 with a form of the Kremser equation that has an \(x^{*}\) or \(y^{*}=0\), but do not use Eqs. (12-31) or (13-19).Equation (12-31) Equation (13-19)Example 13-2The last
a. Solve problem 13.D11 with a form of the Kremser equation.Data From 13.D11A fractional extraction system (Figure 13-5) is separating abietic acid from other acids. Solvent 1 , heptane, enters at
A fractional extraction system (Figure 13-5) is separating abietic acid from other acids. Solvent 1 , heptane, enters at \(\mathrm{E}-=1000 \mathrm{~kg} / \mathrm{h}\) and is pure. Solvent 2,
Recover pyridine from water using chlorobenzene as solvent in a countercurrent extractor. Feed is \(25.9 \mathrm{wt} \%\) pyridine and \(74.1 \mathrm{wt} \%\) water. Solvent is pure chlorobenzene,
Extract \(p\)-xylene and o-xylene from \(n\)-hexane diluent using \(\beta, \beta^{\prime}\) thiodipropionitrile as solvent. Solvent and diluent can be assumed to be immiscible. Feed rate is \(1000.0
Acetic acid is extracted from water with isopropyl ether at \(20^{\circ} \mathrm{C}\) and 1 \(\mathrm{atm}\) pressure in a column with three equilibrium stages. Equilibrium data are in Table 13-7.
A liquid feed that is \(48 \mathrm{wt} \% \mathrm{~m}\)-xylene and \(52 \mathrm{wt} \%\) o-xylene is separated in a fractional extractor (Figure \(13-5\) ) at \(25^{\circ} \mathrm{C}\) and \(101.3
\(500 \mathrm{~kg} / \mathrm{h}\) of a \(30 \mathrm{wt} \%\) pyridine, \(70 \mathrm{wt} \%\) water feed is extracted with \(300 \mathrm{~kg} / \mathrm{h}\) of pure chlorobenzene at \(1
Repeat Example 13-5, but use a McCabe-Thiele diagram with mass ratio units.Example 13-5 A solvent stream containing 10% by weight acetone and 90% by weight chloroform is used to extract acetone from
A \(60 \mathrm{vol} \%\) tributyl phosphate (TBP) in kerosene solvent extracts \(\mathrm{Zr}\left(\mathrm{NO}_{3}\right)_{4}\) from an aqueous solution. Entering solvent is recycled from a solvent
Many extraction systems are partially miscible at high concentrations of solute but close to immiscible at low solute concentrations. At relatively low solute concentrations both McCabe-Thiele and
The aqueous two-phase system in Example 13-3 will be used in a batch extraction. \(7.5 \mathrm{~kg}\) of PEG solution contains protein at mass fraction \(\mathrm{x}_{\mathrm{F}}\). Use \(6.0
We have \(100 \mathrm{~kg} / \mathrm{h}\) of a feed that is \(60 \mathrm{wt} \%\) methylcyclohexane (A) and \(40 \mathrm{wt} \% \mathrm{n}\)-heptane (D) and \(50 \mathrm{~kg} / \mathrm{h}\) of a
Derive Eq. (13-18b) starting with Eq. (13-18a). Yi,1E mi XiNR R () (13-18a) R/E=(mamg)1/2 (13-18b)
Single-stage systems \((\mathrm{N}=1)\) can be solved as countercurrent systems, Figure 13-4, or as crossflow systems, Figure 13-9. Develop the methods for both these designs. Which is easier? If the
Define \(\Delta\) and the coordinates of \(\Delta\) from Eqs. (13-38) and (13-39). Prove that points \(\Delta, \mathrm{E}_{\mathrm{j}}\), and \(\mathrm{R}_{\mathrm{j}+1}\) (passing streams) lie on a
Prove that the locations of streams \(\mathrm{M}, \mathrm{F}_{1}\), and \(\mathrm{F}_{2}\) in Figure 13-17 lie on a straight line. wt. frac. solute A M A XDF, XDM F2 B XDF2 wt. frac. diluent, D
Solve Problem 12.D22 with a mass balance and the Kremser equation.Data From Problem 12.D22We are adsorbing dichloromethane from air into water at \(25^{\circ} \mathrm{C}\) and \(10.0 \mathrm{~atm}\).
This problem is long and involves many calculations because it is a hand calculation of the matrix method for nonisothermal absorption. Suggestion: Set up everything on a spreadsheet. It makes
A laboratory steam stripper with 11 real stages is used to remove \(1000.0 \mathrm{ppm}\) (wt) nitrobenzene from an aqueous feed stream that enters at \(97.0^{\circ} \mathrm{C}\). Flow rate of liquid
Laboratory tests are being made prior to design of an absorption column to absorb bromine \(\left(\mathrm{Br}_{2}\right)\) from air into water. Tests were made in a laboratory packed column that is
Climate change is very much in the news. Engineers need to be heavily involved to control climate change. One approach is to capture carbon dioxide and sequester it. Write a two to three page
Feed gas is at \(1.0 \mathrm{~atm}\) and \(30.0^{\circ} \mathrm{C}\) and is \(90.0 \mathrm{~mol} \%\) air and \(10.0 \mathrm{~mol} \%\) ammonia. Flow rate is \(200.0 \mathrm{kmol} / \mathrm{h}\).
We wish to absorb two gas streams in an absorber. The main gas stream (stream A) is at \(15.0^{\circ} \mathrm{C}, 2.5 \mathrm{~atm}\), and has a flow rate of \(100.0 \mathrm{kmol} / \mathrm{h}\).
a. \(200.0 \mathrm{kmol} / \mathrm{h}\) of a liquid feed that is \(10.0 \mathrm{~mol} \%\) isopropyl alcohol and 90.0 \(\mathrm{mol} \%\) water is stripped in a column with five equilibrium stages.
We wish to absorb n-butane and n-pentane from a gas stream that is at \(25.0^{\circ} \mathrm{C}\) and \(1.0 \mathrm{~atm}\) and has a flow rate of \(100.0 \mathrm{kmol} / \mathrm{h}\). Feed is \(90.0
What is the designer trying to do in the extraction equipment shown in Figure 13-2 and listed in Table 13-1? Why are there so many types of extraction equipment and only two major types of equipment
Write your key relations chart for this chapter.
For Figure 13-24, suppose the raffinate concentration had to be obtained with exactly two equilibrium stages. This can be accomplished by changing amount of solvent used. Would we want to increase or
Extractors are analogous to strippers and absorbers; however, we ignore heat effects for concentrated extractors and assume they are isothermal, but concentrated absorbers and strippers typically
If extract and raffinate phases are totally immiscible, triangular diagrams can still be used. Explain how and describe what equilibrium diagrams will look like.
Based on their solubility parameters, do you think the following are miscible in water, ethanol, or diethyl ether?a. Furfuralb. Phenolc. Toluened. Epichlorohydrin
What situation in analysis of countercurrent extraction on triangular diagrams is superficially analogous to total reflux in distillation? How does it differ?
Study Figure 13-28. Explain what happens as S/F increases. What happens to \(\mathrm{M}\) ? What happens to \(\mathrm{E}_{\mathrm{N}}\) ? What happens to \(\Delta\) ? How do you find \(\Delta_{\min
Distillation systems rarely need pilot plant testing before design, but "design of the extraction column almost always requires pilot plant testing to provide data for accurate scale-up and design of
If an extraction column and a distillation column have the same feed rates, the extraction column will have a smaller diameter than the distillation column. Explain why.
In fractional extraction, what happens to solute \(\mathrm{C}\) ifa. \(\left(\frac{\mathrm{K}_{\mathrm{d}, \mathrm{c}} \mathrm{E}}{\mathrm{R}}\right)_{\text {top }}>1\) and
Sketch the two-stage countercurrent batch extraction process discussed in Section 13.6 after Eq. (13-27d).Equation (13-27d) Yfinal (FD,final /s,final) X final +(FS.initial Yinitial +FD.initial
How would you couple together crossflow and countercurrent cascades? What might be advantages of this arrangement?
The extract stream typically contains product (solute) dissolved in solvent. List as many ways as you can for recovering product and preparing solvent for recycle.
A five-stage countercurrent absorber is used to absorb acetone from air into water at \(3.0 \mathrm{~atm}\) pressure and \(20.0^{\circ} \mathrm{C}\). Total inlet gas flow rate is \(100.0
We are absorbing hydrogen sulfide at \(15.0^{\circ} \mathrm{C}\) into water. Entering water is pure. Feed gas contains \(0.12 \mathrm{~mol}_{2} \mathrm{H}_{2} \mathrm{~S}\). Recover \(97.0 \%\) of
Numerical instability of forms of the Kremser equation used to calculate \(\mathrm{N}\) can cause problems. Show that equations to calculate \(\mathrm{N}\) may have no answer because they would need
A steam stripper is operating isothermally at \(100.0^{\circ} \mathrm{C}\). Entering liquid stream contains \(0.02 \mathrm{~mol} \%\) nitrobenzene in water at \(100.0^{\circ} \mathrm{C}\). Flow rate
Absorb ammonia from air into water at \(20.0^{\circ} \mathrm{C}\) and \(1.5 \mathrm{~atm}\) pressure. Inlet water is recycled from a stripper and contains \(0.2 \mathrm{wt} \%\) ammonia. Gas flow
Design a stripping column to remove carbon dioxide from water by heating the water and passing it countercurrently to a nitrogen stream in a staged stripper. Operation is isothermal and isobaric at
We wish to absorb ammonia from an air stream using water at \(0^{\circ} \mathrm{C}\) and 1.3 atm. Entering water stream is pure water, and entering vapor is \(17.2 \mathrm{wt} \%\) ammonia. Recover
\(\mathrm{HCl}\) is being absorbed from two air streams into water in a countercurrent staged laboratory absorber at \(10.0^{\circ} \mathrm{C}\) and a pressure of \(2.0 \mathrm{~atm}\). Feed rate of
We are operating a stripper at \(0.75 \mathrm{~atm}\) pressure and \(25.0^{\circ} \mathrm{C}\) to strip \(1,2,3-\) trichloropropane from water using air as carrier gas. Inlet water contains 140.0 ppm
Dichloromethane and chloroform are being stripped from water into air at 1.2 \(\mathrm{atm}\) and \(25.0^{\circ} \mathrm{C}\). Feed water contains \(1000.0 \mathrm{ppm}(\mathrm{mol})\) of chloroform
An absorption column for laboratory use has been carefully constructed so that it has exactly four equilibrium stages and is being used to measure equilibrium data. Water is used as solvent to
Read Section 13.4 on crossflow in Chapter 13 before proceeding. We wish to strip \(\mathrm{CO}_{2}\) from a liquid solvent using air as carrier gas. Because air and \(\mathrm{CO}_{2}\) mixtures are
A water cleanup is stripping vinyl chloride from contaminated ground water at \(25.0^{\circ} \mathrm{C}\) and \(850.0 \mathrm{~mm} \mathrm{Hg}\) using a countercurrent, staged stripper. Feed is 5.0
A water stream is saturated with \(\mathrm{CCl}_{4}\) at \(25^{\circ} \mathrm{C}\) and contains \(155 \mathrm{ppm}\) (mol) of \(\mathrm{CHCl}_{3}\). The water stream is stripped with air at a
We plan to treat \(150.0 \mathrm{kmol} / \mathrm{h}\) of water that is saturated with carbon tetrachloride (the \(\mathrm{CCl}_{4}\) is at the solubility limit shown in Table \(12-2\) ) at
Argon and methane are absorbed from nitrogen into liquid ammonia at 252.3 \(\mathrm{K}\) and \(175.0 \mathrm{~atm}\) in an ammonia plant. Feed rate of gas is \(100.0 \mathrm{kmol} / \mathrm{h}\).
If the column uses sieve plates, what column diameter is required for the absorber in Problem 12.D16? Operate at \(75 \%\) of flood. Use \(0.6096 \mathrm{~m}\) tray spacing. Assume \(\eta=0.85\). The
A stripping column with 27 actual stages has an overall efficiency of 0.2 . Feed is \(100.0 \mathrm{kmol} / \mathrm{h}\) of liquid water that contains \(0.010 \mathrm{~mol}^{\%} \mathrm{CHCl}_{3}\).
Carbon dioxide dissolved in water makes the water slightly acidic. We desire to remove most of the \(\mathrm{CO}_{2}\) from \(10.00 \mathrm{kmol} / \mathrm{h}\) of water containing
0We need to remove \(\mathrm{H}_{2} \mathrm{~S}\) and \(\mathrm{CO}_{2}\) from \(1000.0 \mathrm{kmol} / \mathrm{h}\) of a water stream at \(0^{\circ} \mathrm{C}\) and \(15.5 \mathrm{~atm}\). 0Inlet
A gas-processing plant has an absorber and a stripper set up as shown in Figure \(12-2\), except both columns operate at \(25.0^{\circ} \mathrm{C}\) but are at different pressures. Absorber is at
We are adsorbing dichloromethane from air into water at \(25^{\circ} \mathrm{C}\) and \(10.0 \mathrm{~atm}\). pressure in a countercurrent absorber. The inlet vapor flow rate is 150 \(\mathrm{mol} /
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