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engineering
chemical engineering
Questions and Answers of
Chemical Engineering
For multicomponent GP in perfectly mixed systems, use of \(\Sigma \mathrm{y}_{\mathrm{r}, \mathrm{i}}=1.0\) or \(\Sigma \mathrm{y}_{\mathrm{p}, \mathrm{i}}=1.0\) may lead to incorrect solution, but
Physically, in GP, why does the highest value of \(y_{p}\) occur when the operating line is vertical \(\left(-F_{r} / F_{p}=\infty\right.\), which means \(\left.\mathrm{F}_{\mathrm{p}} \approx
In large membrane systems, it is common to have membrane cascades with membranes arranged both in parallel and in series. What are advantages of this arrangement? The arrangements after the first set
Compare the decanter-distillation hybrid system in Figure 8-3A to the pervap-distillation hybrid system in Figure 19-16B. Why is one of the products from the decanter used as column reflux but one of
In Example 19-3, why is it better to guess \(\theta\) instead of \(F_{p}\) ?Example 19-3 A perfectly mixed GP unit is separating a mixture that is 20.0 mol% carbon dioxide, 5.0 mol% oxygen, and 75.0
Someone attached the feed line to the permeate outlet fitting on the hollow fiber RO unit. The permeate product line was attached to the feed fitting. If salty feed water at 50.0 bar is sent to the
Distillation and membrane separators can be combined as hybrid systems in a number of ways. Brainstorm as many methods as you can.
Devise schemes that will increase UF separation of intermediate molecular weight polypeptide from a low molecular weight compound if retention of intermediate molecular weight polypeptide is
UF and MF feed-and-bleed systems are often operated batch instead of continuous. Sketch how you would do this operation.
For an RO system in which osmotic pressure is a linear function of weight fraction of solute, \(\pi=a^{\prime} x\), show that at the same values of \(\mathrm{x}_{\mathrm{p}}\), the relationship
Solve Eq. (19-19a) for \(x_{p}\) as a function of \(x_{r}\). Xp[xp('a'-1)+' (PP)+1] M1+(a'a'-1)x, (19-19a)
Derive Eq. (19-32a) from shell balances. You should obtain a second-order equation. Do a first integration, and apply boundary condition \(\mathrm{R}=1.0\) at \(\mathrm{z}=0\). (J'solv Psolv)x+D dx 0
Derive Eq. (19-11e). Yin,i (19-11e) 1+(KM.i-1)0
The best single source for phase diagrams remains the National Research Council's 1930 International Critical Tables of Numerical Data, Physics, Chemistry and Technology. Why are there fewer
Growth columns are not MSMPR crystallizers. Which MSMPR assumptions are not met by growth columns?
Your manager wants you to purify \(10,000.0 \mathrm{~kg} / \mathrm{h}\) of tin by zone melting at the very fast velocity of \(0.50 \mathrm{~m} / \mathrm{h}\). Each zone melting line will have enough
Delineate the differences between crystallization from solution and melt crystallization.
Visit https://www.sulzer.com/en/products/separation-technology/crystallization and study the presentations on static, falling-film, and suspension crystallization. Write a short report on what
Arctic explorers learned from indigenous natives that year-old ice, which had gone through a partial melting cycle during the Arctic summer, produced drinkable water when melted but fresh ice did
The distribution coefficient of manganese in aluminum is \(\mathrm{k}=1.0\). Dream up possible methods to purify aluminum that contains Mn impurity.
Design a distribution manifold to do the necessary switching of lines for Figure 18-8 if a single falling-film crystallizer is used. Fresh feed Feed tanks Feed after last Recycle Crystallization Feed
Figure 18-13B indicates that the distillate from the distillation column, which is the recycle stream to the crystallizer, is mixed with the fresh feed. Because mixing is the opposite of separation,
Show the steps required to go from Eq. (18-26a) to Eq. (18-26c). dQ= 1 WL (TC-Tmelt) dt tp tc 1 =U(WL) (TC-Tmelt) dt (18-26a, b) + + hHTF Kmetal kc hNC 1 1 1 UhHTF cond. Al tp 1 1 Kcond.C hNC tc
For a static crystallizer, start with Eq. (18-33i) and derive the formula for the general case of determining the thickness \(\mathrm{t}_{\mathrm{C}, 2}\) at time \(\mathrm{t}_{2}\) when the starting
A mixture of \(\beta\)-methylnaphthalene \(+\beta\)-chloronaphthalene \((\beta \mathrm{cn})\) at \(1.0 \mathrm{~atm}\) (Figure 17 \(8 \mathrm{~A})\) has liquid and solid in equilibrium at
We have \(15.0 \mathrm{kmol}\) mixture that is \(60 \mathrm{~mol} \%\) naphthalene and \(40 \mathrm{~mol} \%\) phenol at \(100^{\circ} \mathrm{C}\). Data are in Figure 18-1.a. When it is slowly
\(100 \mathrm{kmol} / \mathrm{h}\) of an \(8 \mathrm{~mol} \%\) naphthalene \(-92 \mathrm{~mol} \%\) phenol mixture at \(40^{\circ} \mathrm{C}\) is fed to a continuous crystallizer. The crystallizer
The activity coefficients \(\gamma_{\mathrm{A}}\) and \(\gamma_{\mathrm{W}}\) for the solid-liquid phase equilibrium of acetic acid and water and the Margules constants A and B are determined in
You have successful laboratory results for suspension melt crystallization with an SSCC followed by a growth vessel and a wash column. For a pilot plant, you want to increase the feed flow rate by a
Determine what happens if we start with \(100.0 \mathrm{kmol}\) of a \(5.0 \mathrm{~mol} \%\) acetic acid, 95.0 \(\mathrm{mol} \%\) water mixture at \(5^{\circ} \mathrm{C}\) and cool it slowly. Data
Determine the thermal \(\delta_{\mathrm{T}}\) and mass \(\delta_{\mathrm{M}}\) boundary layer thicknesses for Example \(18-5\) at \(\mathrm{T}_{\text {avg }}=69.2^{\circ} \mathrm{C}\).Example
Determine the effects of entrainment for Example 18-1, Part C, for the following:Example 18-1a. Melt of eutectic composition replaced with feed,, \(\mathrm{e}_{\mathrm{v}} \approx 0.30\).b. Operating
Woods (1995b) provides different heat capacity and latent heat equations for phenol and naphthalene with different temperature ranges. Note that these are predicted values regardless of the existence
We wish to purify \(99.81 \mathrm{wt} \%\) anthracene to \(99.96 \mathrm{wt} \%\). The only impurity is fluorene. Assume equilibrium operation.a. Will one pass in a zone refiner with \(\mathrm{L} /
a. In Table \(18-8\), the column labeled \(\Delta \mathrm{G} / \Delta \mathrm{t}\), which is a measure of the acceleration of G, was calculated from a larger spreadsheet table with values spaced at
Using the integration results in Example 18-7 as a base, predict the change in crystal thickness if additional feed is added for 300 more seconds to the falling-film system after a layer of crystal
A saturated aqueous solution of \(\mathrm{CuSO}_{4}\) at \(60^{\circ} \mathrm{C}\) is cooled in a cooling crystallizer (no loss of water) to \(0^{\circ} \mathrm{C}\). The product crystals are hydrate
Your technician is doing a steady-state evaporative crystallization of nickel chloride. The inlet water flow rate is \(100 \mathrm{~kg} / \mathrm{h}\). The feed is a saturated liquid at \(100^{\circ}
\(1000 \mathrm{~kg} / \mathrm{h}\) of an aqueous feed that is \(20 \mathrm{wt} \% \mathrm{Na}_{2} \mathrm{CO}_{3}\) at \(80^{\circ} \mathrm{C}\) is fed to a vacuum crystallizer operating at
Nickel chloride solubility data are given in Table \(17-1\). We start with \(100 \mathrm{~kg}\) of water saturated with \(\mathrm{NiCl}_{2}\) at \(100^{\circ} \mathrm{C}\) and cool to \(10^{\circ}
Solve Example 17-15 Part E calculating the solution density by assuming that volumes add. Determine the error in the amount of crystals collected by comparing your answer to the answer determined
In crystallization of potassium chloride with a \(100^{\circ} \mathrm{C}\) feed and the crystallizer operating at \(20^{\circ} \mathrm{C}\), we obtain \(\mathrm{G}=4.0 \times 10^{-7} \mathrm{~m} /
Urea crystallization \(\left(\mathrm{k}_{\mathrm{v}}=1.0, \tau=5.9 \mathrm{~h}, ho_{\mathrm{c}}=1.33 \mathrm{~g}\right)\) ) resulted in the following partial sieve analysis (screen numbers in the
A saturated feed of potassium chloride at \(100^{\circ} \mathrm{C}\) is fed to a cooling crystallizer operating at \(20^{\circ} \mathrm{C}\). We obtain \(\mathrm{G}=4.0 \times 10^{-7} \mathrm{~m} /
a. Discard the data point for the size 14 screen in Example 17-9, and find \(G\) and \(n^{\circ}\).Example 17-9b. Is the error larger for \(\mathrm{G}\) or for \(\mathrm{n}^{0}\) ? Why? Assuming the
\(1000 \mathrm{~kg}\) of a \(3.5 \mathrm{wt} \%\) aqueous solution of \(\mathrm{NaCl}\) is frozen following the method used for eutectic freeze concentration (EFC).a. How much water is removed before
a. Predict the complete screen analysis for Example 17-11. The stack of screens used the following Tyler mesh screens: \(10,12,14,20,24,32,42,60,80\).Example 17-11b. How many grams of undersized
Example 17-14, part B, illustrates a method to increase the size of product crystals by seeding. An alternative procedure that might be feasible in some situations is to keep supersaturation,
A \(3.2-\mathrm{m}^{3}\) cooling crystallizer is seeded with \(10.0 \mathrm{~kg} / \mathrm{h}\) of seeds that have a mean size of \(0.006 \mathrm{~mm}\). We want to increase the size of product
A \(3.0-\mathrm{m}^{3}\) cooling crystallizer is operating over a temperature range that gives \(\mathrm{C}_{\mathrm{in}}=82 \mathrm{~kg}\) solute \(/ 100 \mathrm{~kg}\) water and \(\mathrm{C}_{\text
We want to use controlled cooling of a batch crystallizer that is crystallizing \(\mathrm{KCl}\) from an aqueous solution. The feed is saturated at the initial temperature of \(90^{\circ}
a. At \(18^{\circ} \mathrm{C}\), the concentration solubility product of \(\mathrm{AgBr}\) is \(\mathrm{K}_{\mathrm{SAgBr}}=4.1 \times 10^{-13}(\mathrm{~mol} / \mathrm{L})^{2}\) (Mullin, 2001). What
a. The concentration solubility product of \(\mathrm{Al}(\mathrm{OH})_{3}\) is \(1.1 \times 10^{-15}(\mathrm{~mol} / \mathrm{L})^{4}\) (Mullin, 2001). At saturation, what is the concentration of
A technician is making saturated aqueous solutions of copper chromate \(\mathrm{Cu}\left(\mathrm{CrO}_{4}\right)\), copper hydroxide \(\mathrm{Cu}(\mathrm{OH})_{2}\), and mixtures of these two
\(700 \mathrm{~kg} / \mathrm{h}\) of a \(20 \mathrm{wt} \%\) aqueous solution of sodium carbonate at \(100^{\circ} \mathrm{C}\) is fed to a vacuum crystallizer operating at \(30^{\circ} \mathrm{C}
An aqueous mixture that is \(30 \mathrm{wt} \% \mathrm{Mn}\left(\mathrm{NO}_{3}\right)_{2}\), initially at \(20^{\circ} \mathrm{C}\), is cooled slowly so that it is always at equilibrium. Data are in
A saturated sodium nitrate, \(\mathrm{NaNO}_{3}\), solution at \(100^{\circ} \mathrm{C}\) at a feed rate of \(1000 \mathrm{~kg} / \mathrm{h}\) of water is sent to a steady-state evaporative
We mix \(1100 \mathrm{~kg} / \mathrm{h}\) of water at \(100^{\circ} \mathrm{C}\) with \(750 \mathrm{~kg} / \mathrm{h}\) of copper sulphate hydrate crystals. This mixture is cooled to \(10^{\circ}
A saturated aqueous solution of sodium chloride at \(100^{\circ} \mathrm{C}\) is fed to a steady-state evaporative crystallizer system that operates at \(100^{\circ} \mathrm{C} .
A nickel chloride solution at \(100^{\circ} \mathrm{C}\) containing \(0.80 \mathrm{~kg}\) anhydrous \(\mathrm{NiCl}_{2} / \mathrm{kg}\) water (not saturated) is sent to an evaporative crystallizer
\(1000 \mathrm{~kg} / \mathrm{h}\) of a saturated aqueous solution of citric acid at \(80^{\circ} \mathrm{C}\) is fed to an evaporative/cooling crystallizer. \(\mathrm{V} \mathrm{kg} / \mathrm{h}\)
We wish to precipitate \(\mathrm{Al}^{+3}\) from 2.0 liters of a dilute solution of \(\mathrm{Al}(\mathrm{OH})_{3}\) in water. The concentration is \(7.0 \times 10^{-5} \mathrm{~mol} / \mathrm{L}\)
Develop a batch or semibatch crystallization for a nonvolatile solute dissolved in water and available, but not saturated, at \(65^{\circ} \mathrm{C}\). Solubility in water is moderatejly temperature
If birth and death rates are not negligible, show that Eq. (17-21a) for a steady-state crystallizer becomes\[ \frac{\mathrm{dn}}{\mathrm{dL}}+\frac{\mathrm{n}}{\mathrm{G}
Derivation of MSMPR distributions:a. Derive Eq. (17-24a) and then Eqs. (17-24b) and (17-24c).b. Derive Eq. (17-26a) and then Eqs. (17-26b) and (17-27).c. Derive Eq. (17-29a) and then Eqs. (17-29b)
The text states, "The weight average crystal length \(=3.67 \mathrm{G \tau}\). ." Prove this result is correct.
Equations (17-37) and (17-40a) assume equal growth on all three faces. Derive equations that correspond to Eqs. (17-40a) and (17-40b) if there is equal growth on two faces and very slow growth
We wish to distill \(80.0 \mathrm{~mol} / \mathrm{s}\) of a saturated vapor feed at \(15.0 \mathrm{~atm}\). The feed is \(10.0 \mathrm{~mol} \%\) ethane, \(30.0 \mathrm{~mol} \%\) propane, \(50.0
Determine the overall efficiency for the column designed by the ratebased method in Aspen Plus Lab 13, step 10. If you saved your program, use the saved program as the starting point for the
One of your company's bearded engineers does not always keep his beard as clean as he could. When in the plant, he follows instructions and wears a hair net but does not cover his beard. You expect
Why does an experimental sieve analysis tend to size platelets (Figure 15-7D) based on the second-largest dimension? Assume that holes in the sieve are square.Figure 15-7D D.
a. Based on the data in Table \(17-1\), rank the cations \(\left(\mathrm{NH}_{4}, \mathrm{Ba}, \mathrm{Ca}, \mathrm{Cu}, \mathrm{Mg}, \mathrm{Mn}, \mathrm{Ni}, \mathrm{K}, \mathrm{Na}\right)\) in
Figure 17-7 shows the phase equilibrium for aqueous solutions of five salts. In the discussion about this figure, the Federal Highway Administration (1996) states, "The fact that calcium chloride has
What are the differences between the CSD analysis for a MSMPR crystallizer and a seeded crystallizer?
The text states that for seeded crystallizers, "within limits, supersaturation can be increased to increase growth rate." What are the limits?
In Example 17-14, part \(\mathrm{A}, \Delta \mathrm{L}_{\text {growth }}=0.2971 \mathrm{~mm}\) compared to \(0.2918 \mathrm{~mm}\) in Example 1713. Why does the very sharp seed distribution
Suppose we are operating a laboratory crystallizer with shaft rotation \(\omega_{\mathrm{js}}\) where crystals are suspended just above the floor, Eq. (17-42c). We desire to scale up the crystallizer
Assume trays are plug flow, and repeat Problem 16.D21 parts a and \(b\). In addition, calculate \(\mathrm{E}_{\mathrm{pt}}\) for the three mole fractions \(\mathrm{x}_{\mathrm{W}}=0.48,0.36\), and
Use the Peclet number [Eq. (16-111a)] to determine which model (completely mixed or plug flow) is appropriate for the distillation column calculation at \(\mathrm{x}_{\mathrm{W}}=0.48\) in Problems
The value of \(\mathrm{E}_{\mathrm{MD}}=0.927\) in Example 16-5 is lower than the 0.95 value your supervisor expects. You are tasked to see if the current mixer with the current feed rate can be
For Example 16-1, estimate an average \(\mathrm{H}_{\mathrm{OG}}\) in the stripping section. Then calculate \(\mathrm{n}_{\mathrm{OG}}\) and \(\mathrm{h}_{\mathrm{E}}=\mathrm{H}_{\mathrm{OG}, \text {
If 1.0 -in. metal Pall rings are used instead of 2.0 -in. rings in Example \(16-2\) :a. Recalculate flooding velocity and required diameter.b. Recalculate \(\mathrm{H}_{\mathrm{G}}\) and
In part E of Example 16-2, a HETP value of \(2.15 \mathrm{ft}\) is calculated for the top of the enriching section. Since the average error in individual mass transfer coefficients
A distillation column at \(101.3 \mathrm{kPa}\) is separating a two-phase feed that is \(60.0 \%\) liquid, \(40.0 \mathrm{~mol} \%\) methanol, and \(60.0 \mathrm{~mol} \%\) water. Distillate product
A distillation column with \(6.0 \mathrm{ft}\) of packing can be operated as a stripper with liquid feed, as an enricher with vapor feed, or at total reflux. We are separating methanol from
A distillation column with \(8.01 \mathrm{~m}\) of packing operating at total reflux separates methanol from ethanol at \(101.3 \mathrm{kPa}\). Average relative volatility is 1.69 . Methanol mole
A distillation column operating at total reflux is separating acetone and ethanol at \(1.0 \mathrm{~atm}\). The height of packing is \(2.0 \mathrm{~m}\). The column has a partial reboiler and a total
We wish to strip \(\mathrm{SO}_{2}\) from water using pure air at \(20.0^{\circ} \mathrm{C}\). Outlet water contains \(0.0060 \mathrm{~mol} \% \mathrm{SO}_{2}\), and inlet water contains \(0.112
If 1-in. metal Raschig rings are used instead of 2-in. rings in Example \(16-2\) :Example 16-2Example 4-3Example 16-1a. Recalculate the flooding velocity and the required diameter.b. Recalculate
A packed tower is used to absorb ammonia from air using aqueous sulfuric acid. Gas enters the tower at \(31.0 \mathrm{lbmol} /\left(\mathrm{h}-\mathrm{ft}^{2}\right)\) and is 1.0 \(\mathrm{mol} \%\)
Water originally saturated with carbon tetrachloride \(\left(\mathrm{CCl}_{4}\right)\) at \(25.0^{\circ} \mathrm{C}\) and \(1.0 \mathrm{~atm}\) is stripped with pure air at \(25.0^{\circ}
We are separating methanol and water in a staged distillation column at total reflux to determine Murphree efficiency. Pressure is \(101.3 \mathrm{kPa}\). The column has a 2.0 -in. head of liquid on
The constants obtained by Shende and Sharma (1974) for use in Eq. (16-72) are given in the following table. Assume their experiments with \(\mathrm{NaOH}-\mathrm{SO}_{2}\) were done at \(1.0
We are separating methanol and water in a staged distillation column at total reflux to determine Murphree efficiency. Pressure is \(101.3 \mathrm{kPa}\). The column has a 2.0 -in. head of liquid on
The large-scale column in Example 16-4 is fed a saturated liquid with mole fraction \(\mathrm{z}=0.5\), and separation is essentially complete ( \(\mathrm{x}_{\text {dist }} \sim 1.0\) and
Although the largest errors in calculating the height of a packed column are errors in (1) mass transfer coefficients and (2) VLE data, calculation errors can also be significant because calculation
Errors in mass transfer coefficients obviously affect the value of \(\mathrm{H}_{\mathrm{G}}\) and hence the height of the packed section. These errors also affect calculation of
For extraction of benzoic acid from water into toluene with toluene the dispersed phase, we measure the following mole fractions of benzoic acid: \(\mathrm{x}_{\mathrm{D}, \text { in }}=0,
For extraction of benzoic acid from water into toluene with toluene the dispersed phase, we measure the following concentrations of benzoic acid: \(\mathrm{C}_{\mathrm{D}, \text { in }}=0,
Estimate average particle diameter, mass transfer coefficients, and mixer stage efficiency for extraction of benzoic acid from water into toluene for Example 13-7.Example 13-7 Design a baffled mixing
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