Belton American Cinema Study Guide |[EBook]

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The Explanation of Mass transfer is well elaborated by Treybal especially in the 3rd edition. The book is available in the market as well as in the online store in notebook and PDF formats. There are many self-assessments and numerical problem which a student cant solve just by its own and some times teachers also get confused in solving those problems. For the complete comprehensive guide of this operations, there is a solution manual to it which is available on our site by the name of Mass transfer 3rd edition Solution manual and is free. Anyone can download it for free in ebook and pdf formats. Read our DMCA policy. If you find any violation on our page or any copyrighted content, Then please contact us Asap, That content and data shall be removed or takedown within 48 working hours. ( Please read our Disclaimer ) Read our DMCA policy. If you find any violation on our page or any copyrighted content, Then please contact us Asap, That content and data shall be removed or takedown within 48 working hours. ( Please read our Disclaimer ). S i: Ba i: 100 e f he b) The a e age S a a c ce i d) The S e eigh i c) The S ec a i i a de i. ai. f he i e. 1.2a. Concen a ion of a li id ol ion fed o a di illa ion col mn. A a e f i ified a a ga, LNG, f A a a ha he f CH4, 4.6 C2H6, 1.2 C3H8, a d 0.7 CO2. Ca c a e: a) A e age ec a eigh f he LNG i e. S a c ii: 93.5 i b) Weigh f ac i S f CH4 i he i e. i Ba i: 100 e f LNG c) The LNG i hea ed 300 K a d 140 Pa, a d a ga i e de he e c di i. S i g i i e c e e. E i a e he de i f he 1.4b. Concen a ion of a fl e ga. A fl e ga con i of ca bon dio ide, o gen, a e apo, and ni ogen. The mola f ac ion of CO2 and O2 in a ample of he ga a e 12 and 6, e pec i el. The eigh f ac ion of H2O in he ga i 6.17. E ima e he den i of hi ga a 500 K and 110 kPa. I c i fa e i i e fa ia a d ai. The ga e e h gh he b f a ac ed bed ga ab he e i f c ec e a ea f e i id a e ha ab b 90 f a f a ia, a d i a ai.

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The ab be e e i c i d ica i h a i e a dia e e a) Neg ec i g he e a a i f a e, ca c a e he a ia f ac i i he ga ea ab be. S i a be he f 2.5. i g he a e ci (defi ed a a f ae e i e be: 1.6b. Velocities and flu es in a gas mi ture.Solution Molar average velocit, V Mass average velocit, vm Basis: 1 kmole of gas mi ture b) Evaluate the four flu es: jO2, nO2, JO2, NO2. Solution: 1.7b. P ope ie of ai a a ed i h a e apo. Ai, ed i a 30- 3 c ai e a 340 K a d 101.3 Pa i f i g e ie f he ga i e: a) M e f ac i f ae a.S a a ed i h a e a. De e i e he i a) A i ee ai f F ae a: a a a ed i e b) c) d) 1.8c. Wa e balance a o nd an ind ial cooling o e. The ef e, a a a f he ci c a i g a e be de ibe a e di ca ded (b d ). Wi dage e f he e ae e i a ed a 0.2 f he eci c a i a e. E i a e he a e - a e e i e e. Solution c) Calculate the water-vapor partial pressure and relative humidit in the air leaving the dr er. Solution Calc la e a e a A i ee ai e f e a 350 K ae a: 1.10b. Acti ated carbon adsorption; material balances. A a e ga c ai 0.3 e e i ai, a d cc ie a e f 2,500 3 a 298 K a d 101.3 Pa. I a eff ed ce he e ec e f hi ga, i i e ed 100 g f ac i a ed ca b, i i ia f ee f e e. The e i a ed each e i ib i a c a e ea e a d e e. A i g ha he ai d e ad b he ca b, ca c a e he e i ib i c ce a i f e e i he ga e ha e, a d he a f e e ad bed b he ca b.Sol ion E pe imen al al e 1.14d. Diffusivit of polar gases If one or both components of a binary gas mixture are polar, a modified Lennard-Jones relation is often used. Brokaw (Ind. Eng. Chem. Process Design De elop., 8:240, 1969) has suggested an alternative method for this case. Calculate the effective diffusivit of nitrogen through a stagnant gas mi ture at 373 K and 1.5 bar. The mi ture composition is: O2 15 mole CO 30 CO2 35 N2 20 Sol;ution Calculate mole fractions on a nitrogen (1)-free basis: o gen (2); carbon mono ide (3); carbon dio ide (4) Calculate binar MS diffusivities from Wilke-Lee equation 1.18a,d.

Mercur removal from flue gases b sorbent injection. Mercur is considered for possible regulation in the electric power industr under Title III of the 1990 Clean Air Act Amendments. One promising approach for removing mercur from fossil-fired flue gas involves the direct injection of activated carbon into the gas. An important parameter of the model is the effective diffusivit of mercuric chloride vapor traces in the flue gas. If the flue gas is at 1.013 bar and 408 K, and its composition (on a mercuric chloride-free basis) is 6 O2, 12 CO2, 7 H2O, and 75 N2, estimate the effective diffusivit of mercuric chloride in the flue gas. Assume that onl the HgCl2 is adsorbed b the activated carbon. Whe a a di cia e i i,i a he ha ec e diff e. I he ab e ce f a e ec ic e ia, he diff i fa i ge a a be ea ed a ec a diff i.Estimate the diffusion coefficient of oxygen in liquid water at 298 K. Use the Hayduk and Minhas correlation for solutes in aqueous solutions. Estimate the diffusivity of carbon tetrachloride in a dilute solution in n-hexane at 298 K using the Hayduk and Minhas correlation for nonaqueous solutions. Compare it to the result obtained using the data on Table 1.2. The viscosity of water at 288 K is 1.15 cP. Solution Iniitial estimates From Table 2.1 1.24b, d. Concentration dependence of binar liquid diffusivities.S ed b Ha e (1953) i 0.42 10-5 diff e ii a e a 298 K ii f a e i e ha da dS i E i a e he i fi i e di i f Ha d -Mi ha f a F A e di A, he i fi i e di a 298 K i i diff f e ha i i b) E i a e he diff i i f ace e i a e a 298 K he he f ac i f ace e i i i 35. F hi e a 298 K, he ac i i c efficie f ace e i gi e b Wi e ai (S i h, J. M., e a., Introduction to Chemical Engineering Thermod namics, 5 h ed, McG a -Hi C., I c., Ne Y, NY, 1996): S i E i a e he he d a ic fac F A e di A E i a e he i fi i e di i f Ha d -Mi ha f a diff e ii f ace i ei a e a 298 K 1.25b, d. Stead -state, one-dimensional, gas-phase flu calculation.

A flat plate of solid carbon is being burned in the presence of pure o gen according to the reaction Molecular diffusion of gaseous reactant and products takes place through a gas film adjacent to the carbon surface; the thickness of this film is 1.0 mm. On the outside of the film, the gas concentration is 40 CO, 20 O2, and 40 CO2. The reaction at the surface ma be assumed to be instantaneous, therefore, ne t to the carbon surface, there is virtuall no o gen.The temperature of the gas film is 600 K, and the pressure is 1 bar. Orthogonal collocation matrices The p e The Ma e and empe a ell-S efan diff e in he apo ion coefficicien pha e a e ae The length of the diffusion path is The densit of the gas phase follows from the ideal gas law Initial estimates of the flu es Initial estimates of the concentrations Stoichiometric relations (No o gen) 1.26b. Stead -state, one-dimensional, liquid-phase flu calculation. Ammonia, NH3, is being selectively removed from an air-NH3 mixture by absorption into water. In this steady-state process, ammonia is transferred by molecular diffusion through a stagnant gas layer 5 mm thick and then through a stagnant water layer 0.1 mm thick. The concentration of ammonia at the outer boundary of the gas layer is 3.42 mol percent and the concentration at the lower boundary of the water layer is esentially zero.The temperature of the system is 288 K and the total pressure is 1 atm. Assume that the gas and liquid are in equilibrium at the interface. Sol ion: Ini ial e ima e: 1.28c. Stead -state molecular diffusion in gases. A i e f e ha a d ae a i bei g ec ified i a adiaba ic di i a i c. The a c h i a i ed a d a fe ed f he i id he a ha e. Wa e a c de e (e gh he a e hea f a i a i eeded b he a c h bei g e a a ed) a d i a fe ed f he a he i id ha e. B h c e diff e h gh a ga fi 0.1 hic. The e e a e i 368 K a d he e e i 1 a. The e f ac i f e ha i 0.8 e ide f he fi a d 0.2 he he ide f he fi.

Based on the Lewis relation, estimate the diffusivit of water vapor in air at 300 K and 1 atm. Compare our result with the value predicted b the WilkeLee equation. Wa e e a a i g f a d a 300 K d e b ec a diff i ac a ai hic. If he e a i e h idi f he ai a he e edge f he fi i 20, a d he ba, e i a e he d i he a e e e e da, a i g ha c di i i he fi c a. The a e e f ae a af ci f e e a e ca be acc a e he Wag e e a i (Reid, e a., 1987) S fi 1.5 a e ei 1 e ai e i a ed f i F A e di A 1.31b, d. Stead -state molecular diffusion in a ternar gas s stem. Ca c a e he f e a d c ce a i fi e f he e a e h d ge (1), i ge (2), a d ca b di ide (3) de he f i g c di i. The e e a e i 308 K a d he e ei 1 atm. The diffusion path length is 86 mm. At one end of the diffusion path the concentration is 20 mole H2, 40 N2, 40 CO2; at the other end, the concentration is 50 H2, 20 N2, 30 CO2. Orthogonal collocation matrices The p e The Ma e and empe a ell-S efan diff The leng h of he diff The den i e in he apo ion coefficicien pha e a e ae ion pa h i of he ga pha e follo f om he ideal ga la Initial estimates of the flu es Initial estimates of the concentrations 2.1a. Ma - an fe coefficien in a ga ab o be. A ga ab be i ed e e be e e (C6H6) a f ai b c bbi g he ga i e iha a i e i a 300 K a d 1 a.The de i f id a h ha e e i 1.145 i a e e a 347 K i 670 Pa (Pe a d Chi, 1973).I a ab a e e i e, ai a 300 K a d 1 a i b a high eed a a e he ec a g a ha a ha c ai i id ace e (C3H6O), hich e a a e a ia. 1 g a d 50 c ide. I i c ec ed a e e i c ai i g i id ace e hich a a ica e ace he ace e e a a ed, ai ai i g a c a i id e e i he a e ei e a, i a b e ed ha 2.0 L f ace e e a a ed i 5 i. E i a e a fe c efficie. S ai i face f a The a i a.D i g he a e i 27 2.4b. Mass-transfer coefficients from etted- all e perimental data. A e ed- a e e i e a e - c i fa ga i e, 50 i dia e e a d 1.0 g. Wa e a 308 K f d he i e a. I ea e he e ed ec i a 308 K a d i h a e a i e h idi f 34.

Wi h he he f e a i (2-52), e i a e he a e age a - a fe c efficie, i h he d i i g f ce i e f a f ac i. S i 2.7c. a) I he i ba a e i e e hi Ma an fe in an ann la pace. S i b) M ad a d Pe (T an. AIChE, 38, 593, 1942) hea - a fe c efficie i a a a ace: he e d a d di a e he dia e e defi ed a Wied c efficie S i f he a a g he c di i ide a d i e ide dia e e e i f f a a). C a e e ed he f f he a a fe a d e i aeb h e. The a e e f a c h a 300 K i 2.7 Pa. S i P e ie f di e i e f ac h i ca b di ide a 300 K a d 1 a c) Za a a (Ad. Heat Transfer,, 93, 1972) ed he f a fe c efficie i a agge ed be ba a a ge e i ia Che e: U e he a - a fe e c efficie f a b). C S i e i a a g a e he e. Solution Laminar flo At the bulk of the solution, point 2: At the interface, point 1: 2.11b. Ma an fe f om a fla li id face. E i a e he a - a fe c efficie edic ed b e a i (2-28) (2-29) a d c aei he a e ea ed e e i e a. N ice ha, d e he high a i i f ace e, he a e age ace e c ce a i i he ga fi i e a i e high. The ef e, e ie ch a de i a d i c i h d be e i a ed ca ef. Repeat E ample 2.9 for a drop of ater hich is originall 2 mm in diameter. Solution 2.13b. Dissolution of a solid sphere into a flo ing liquid stream. Estimate the mass-transfer coefficient for the dissolution of sodium chloride from a cast sphere, 1.5 cm in diameter, if placed in a flowing water stream. Solution From Prob. 2.10: 2.14b. Sublimation of a solid sphere into a gas stream. Solution For air at 347 K and 1 atm: Estimate DAB from the Wilke-Lee equation Lennard-Jones parameters for naphthalene 2.15b. Dissolution of a solid sphere into a flo ing liquid stream. The cr stal of Problem 1.26 is a sphere 2-cm in diameter.Solution b) Estimate the rate at which the cr stal dissolves and compare it to the answer obtained in Problem 1.26. Solution From Prob.1.26 From Prob.1.26: 2.16c. Mass transfer inside a circular pipe. Water flows through a thin tube, the walls of which are lightly coated with benzoic acid (C7H6O2).

Under these conditions, equation (2-63) applies.Water flows down the inside wall of a 25-mm ID wetted-wall tower of the design of Figure 2.2, while air flows upward through the core. Compute the average partial pressure of water in the air leaving if the tower is 1 g. S i F a e a 294 K 2.18c. Ma an fe in an ann la pace. I d i g he b i a i f a h ha e e i a ai ea, a i e iga c c ed a 3- - g a a d c. E i a e he a ia e e f a h ha e e i he ai ea e i i g f he be. Sol ion In hi i a ion, he e ill be a mola fl f om he inne all, NA1, i h pecific in e facial a ea, a1, and a fl f om he o e all, NA2, i h a ea a2. A ma e ial balance on a diffe en ial ol me elemen ield: Define: Then: Fo he in e io all: For the outer all: 2.19c. Ben ene evaporation on the outside surface of a single c linder. Wilke and Hougan (T an. AIChE, 41, 445, 1945) reported the mass transfer in beds of granular solids. Air was blown through a bed of porous celite pellets wetted with water, and by evaporating this water under adiabatic conditions, they reported gas-film coefficients for packed beds. Solution From the Wilke-Lee equation 2.21b. Ma an fe and p e e d op in a packed bed. The porosit of the bed is 40.Solution From the Wilke-Lee equation: b) E ima e he p e Sol ion e d op h o gh he bed. 2.22b. Volumetric mass-transfer coefficients in industrial to ers. The interfacial surface area per unit volume, a, in many types of packing materials used in industrial towers is virtually impossible to measure. Both a and the mass-transfer coefficient depend on the physical geometry of the equipment and on the flow rates of the two contacting, inmiscible streams. Accordingly, they are normally correlated together as the volumetric masstransfer coefficient, k c a. Empirical equations for the volumetric coefficients must be obtained experimentally for each type of mass-transfer operation. Sherwood and Holloway (Trans.
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AIChE, 36, 21, 39, 1940) obtained the following correlation for the liquid-film mass-transfer coefficient in packed absorption towers The values of a and n to be used in equation (2-71) for various industrial packings are listed in the following table, when SI units are used exclusively.Compare the results. Solution 2.23b. Mass transfer in fluidi ed beds. They studied different arrangements of packed columns, including fluidized beds. The fluidized bed experiments were performed in a 5-cm-ID circular column, 75-cm high. Solution b) Ca a o a e al.U ing hi co ela ion, e ima e he ma coefficien, L, if he po o i of he bed i 60. Compa e o e l o ha of pa a). - an fe Sol ion 2.24b. Mass transfer in a hollo -fiber boiler feed ater deaerator. Con ide he hollo -fibe BFW deae a o de c ibed in E ample 2-13.A ming ha onl o gen diff e ac o he memb ane, calc la e he ga ol me flo a e and compo i ion a he l men o le. Re ea E a e 3.1, b f a i id c ce a i f 0.6 e e a e f 320 K. S e f ac i e ea da i 3.2b. Application of Raoult's law to a binar s stem.N a he a e, -C7H16, a d a c a e, -C8H18, f idea i. A 373 K, a he a e ha a a e e f 106 Pa a d a c a e f 47.1 Pa. a) Wha d be he c ii f a he a e- c a e i ha b i a 373 K de a 93 Pa e e? S i b) Wha (a)? S d be he c ii f he a i e i ib i i h he i ha i de c ibed i i 3.4a. Henr 's la: saturation of ater ith o gen.Re ea E a e 3.3, b a i g ha he a ia, ai, a d a e a e b gh i c ac i a 3 c ed c ai e. The e i 10 f ga ace e he i id. F a e i hich c e A i a fe i g f e i ib i e a i i gi e b he e A,i i he e i ib i i a f ac i. Sol ion Ini ial g e e 3.9d. Absorption of ammonia b water: use of F-t pe mass-transfer coefficients. Sol ion Ini ial g e e 3.10b. Ma - an fe e i ance d ing ab o p ion of ammonia. For mass transfer across the hollow-fiber membrane contactors described in Example 2.13, the overall mass-transfer coefficient based on the liquid concentrations, KL, is given by (Yang and Cussler, AIC E J., 32, 1910, Nov.

1986) where k L, k M, and k c are the individual mass-transfer coefficients in the liquid, across the membrane, and in the gas, respectively; and H is Henry's law constant, the gas equilibrium concentration divided by that in the liquid.D i g ab i f bi i ga e, a a fe f a high c ce a ed ga i e a e di e i id i fe e a e ace. A,i a) Sh e ai S I ha, de he c i he ga ha e: di i de c ibed ab e, he ga i e facia c ce ai a i fie he I he i F He id ha e: ' La: The: Rea a gi g: b) I a ce ai a a a ed f he ab i f SO2 f ai b ea f ae,a e i i he e i e he ga c ai ed 30 SO2 b e a d a i c ac i h a i id c ai i g 0.2 SO2 b e. The e e a e a 303 K a d he a e e 1 a. E i a e he i e facia c ce a i a d he ca SO2 a f. The e Hg ( ) i ib i SO2 bi i da a a Ini ial g e: 3.13d. Distillation of a mi ture of methanol and ater in a packed to er: use of F-t pe mass-transfer coefficients. At a different point in the packed distillation column of Example 3.6, the methanol content of the bulk of the gas phase is 76.2 mole ; that of the bulk of the liquid phase is 60 mole . The e e i g ac i a ed ca b c ai 15 c 3 be e e a (a STP) ad bed e g a f he ca b. The e e a e a d a e e a e ai ai ed a 306 K a d 1 a.Solution d) F S he c di i f a (c), ca c a e he be f idea age e i ed.The ac i a ed ca b ea i g he ad be f P b e 3.14 i ege e a ed b c e c e c ac i h ea a 380 K a d 1 a. The ege e a ed ca b i e ed he ad be, hi e he i e f ea a d de bed be e e a i c de ed. The c de a e e a a e i a ga ic a d a a e ha e a d he ha e a e e a a ed b deca a i. From Problem 3.14 From the XY diagram: b) For a steam flow rate of twice the minimum, calculate the ben ene concentration in the gas mixture leaving the desorber, and the number of ideal stages required. Solution 3.16b. Material balances: adsorption of ben ene vapor on activated carbon; cocurrent operation. If the adsorption process described in Problem 3.14 took place cocurrentl, calculate the minimum flow rate of activated carbon required. Solution Fom Problem 3.

14: From the XY diagram: 3.17b. Material balances in batch processes: dr ing of soap with air. I i de i ed d 10 g f a f 20 i eb eigh e ha 6 i eb 3 c ac i h h ai. The e a i aced i a e e c ai i g 8.06 f ai a 350 K, 1 a, a da ae-a a ia e e f 1.6 Pa. The e i a ed each e i ib i, a d he he ai i he e e i e i e e aced b f e h ai f he igi a i ec e a d e e a e. H a i e he ce be e ea ed i de each he ecified a i ec e f e ha 6. Nicotine in a ater solution containing 2 nicotine is to be e tracted ith kerosene at 293 K. Water and kerosene are essentiall insoluble. Determine the percentage e traction of nicotine if 100 kg of the feed solution is e tracted in a sequence of four batch ideal e tractions using 49.0 kg of fresh, pure kerosene each. The d i g a d i id- i id e ac i eai de c ibed i P b e 3.17 a d 3.18, e ec i e, a e e a e faf c fig a i ca ed a c -f ca cade. Fig e 3.27 i a che a ic diag a fac -f ca cade f idea age. Each age i e e e ed b a ci c e, a d i hi each age a a fe cc a if i c c e f. The L ha e f f e age he e, bei g c ac ed i each age b a f e h V ha e. If he e i ib i -di ib i c e f he c -f ca cade i e e he e aigh a d f e, i ca be h ha (T e ba, 1980) he e S i age. I i ia e i a e 3.20a. Cross-flo cascade of ideal stages: nicotine e traction. C ide he ic i e e ac i fP be 3.18 a d 3.19. Ca c a e he e i ed achie e a ea 95 e ac i efficie c. S be f idea age i U e 8 idea age 3.21b. Kremser equations: absorption of h drogen sulfide. The i i ia c ii f he feed ga i 2.5 e e ce H2S. A fi a ga ea c ai i g 0.1 e e ce H2S i de i ed. The ab bi g a e i e e he e f ee f H2S.Solution at SC b) Determine the composition of the e iting liquid. Solution c) Calculate the number of ideal stages required. Solution 3.22b. Absorption ith chemical reaction: H2S scrubbing ith MEA. A h i P b e 3-21, c bbi g f h d ge fide f a a ga i g ae i ac ica i ce i e i e a ge a f ae d e he bi i f H2S i a e.

If a 2N i f e ha a i e (MEA) i ae i ed a he ab be, h e e, he e i ed i id f a e i ed ced d a a ica beca e he MEA eac i h he ab bed H2S i he i id ha e, effec i e i c ea i g i bi i. F hi i e g h a d a e e a e f 298 K, he bi i f H2S ca be a i a ed b (de Ne e, N., Air Poll ion Con rol Engineering, 2 d ed., McG a -Hi, B, MA, 2000): Re ea he ca c a i ab be. S i fP be 3.21, b i g a 2N e ha a i e i a 3.23b. Kremser equations: absorption of sulfur dio ide.Solution b) Calculate the number of ideal stages required for the specified flow rates and percentage SO2 removal. Solution 3.24b. Kremser equations: absorption of sulfur dio ide. An ab o be i a ailable o ea he fl e ga of P oblem 3.23 hich i e i alen o 8.5 e ilib i m age. a) Calc la e he a e flo a e o be ed in hi ab o be if 90 of he SO2 i o be emo ed. Calc la e al o he SO2 concen a ion in he a e lea ing he ab o be. Sol ion Ini ial e ima e b) Wha i he e ce age e a f SO2 ha ca be achie ed i h hi ab a e ed i he a e ha a ca c a ed i P b e 3.23 (a)? S be if he a e f i I i ia e i a e 3.25b. Kremser equations: liquid e traction. I i de i ed ed ce he c ce a i f hi i 0.037 (b eigh ) ace ic acid b e ac i i h 3-he a a 298 K. The i e 3-he a c ai 0.02 (b eigh ) ace ic acid. A e ac i c i a ai ab e hich i e i a e ac e c e ca cade f 15 e i ib i age. Wha e f a e i e i ed. Ca c a e he c ii f he e ha e ea i g he c. A 1-butanol acid solution is to be e tracted ith pure ater. Operation is at 298 K and 1 atm. For practical purposes, 1-butanol and ater are inmiscible.Solution b) If he a e i i e a a ha i he e 1-b a c ce S g he a e be f age, b a i ( ee P b e 3.19)? i ac -f ca cade, i 3.27c. Glucose sorption on an ion e change resin.Fi d he be f e i ib i age e i ed. S i b) If 5 equilibrium stages are added to the cascade of part a), calculate the resin flo required to maintain the same degree of glucose sorption. Solution 4.1a. Void fraction near the alls of packed beds. C ide a c i d ica e e i h a dia e e f 305 f 50.

Beca e f he ci a a e f he id-f ac i adia a ia i f ac ed bed, he e a e a be f ca i c e he a he e he ca id f ac i i e ac e a he a ic a e f he bed. F he bed de c ibed i E a e 4.1, ca c a e he di a ce f he a he fi fi e ch ca i. Annular packed beds (APBs) involving the flow of fluids are used in many technical and engineering applications, such as in chemical reactors, heat exchangers, and fusion reactor blankets. It is well known that the wall in a packed bed affects the radial void fraction distribution. Since APBs have two walls that can simultaneously affect the radial void fraction distribution, it is essential to include this variation in transport models. The correlation is Consider an APB with outside diameter of 140 mm, inside diameter of 40 mm, packed with identical 10-mm diameter spheres. (a) Estimate the void fraction at a distance from the outer wall of 25 mm. Repea P oblem 4.5, b ing ce amic in ead of pla ic In alo addle. Repeat E ample 4.3, but using 15-mm ceramic Raschig rings as packing material. Solution Packed Col mn Design Program This program calculates the diameter of a packed column to satisf a given pressure drop criterium, and estimates the volumetric mass-transfer coefficients. A packed to er is to be designed for the countercurrent contact of a ben ene-nitrogen gas mi ture ith kerosene to ash out the ben ene from the gas. The b e be ed a he ga i e i ha e a ea echa ica efficie c f 60. The air flow rate to be used is 5 times the minimum. Estimate the corresponding mass-transfer coefficients. Repeat E ample 4.5, but using an air flo rate that is t ice the minimum required. Solution Initial estimate of the column height, Z Ini ial e ima e of ga hold p Calculate po er required 4.16b. Stripping chloroform from water b sparging with air. Repeat Example 4.5, but using the same air flow rate used in Problem 4.15, and specifying a chloroform removal efficiency of 99.

I he ea e f a e a e, de i ab e ga e a e f e e i ed de bed f he ae,a d ge i ad bed i he a e he b bb e f ai a e di e ed ea he b f ae a i a d. A he b bb e i e, e ca be a fe ed f he ga he i id f he i id he ga de e di g he c ce a i d i i g f ce. S i Ini ial e ima e of ga hold p Initial estimate of transfer efficienc (b) Calculate power required 4.19c,d. Batch aste ater aeration using spargers; effect of liquid depth. C ide he i a i de c ibed i P b e 4.18. Acc di g Ec e fe de (2000), f f b bb e-diff i ae a i e he e ic a - a fe c efficie i a ih i de h Z acc di g he e a i hi he e he e 4.18, ca c a e f eg e i e ai c a cha ge. E i a e he c e di g a e f L a a i f he e. Hi: Re e be ha he a e f he d, he ef e he c - ec i a a ea f he d cha ge a he a e de h i U i g he ga de e ed i P b 4.18, he f i g ec f e i ge e a ed 4.20c. Flooding conditions in a packed cooling to er. The a e i c ac ed i h ai, a 300 K a d 101.3 Pa e e ia d, da adc ec e he a e f. A sieve-tray tower is to be designed for stripping an aniline (C6H7N)-water solution with steam. Use a weir height of 40 mm. Design for a 75 approach to the flood velocity. Report details respecting tower diameter, tray spacing, weir length, gas-pressure drop, and entrainment in the gas. Check for excessive weeping. Repeat Problem 4.22, but for a 45 approach to flooding. A dilute aqueous solution of methanol is to be stripped with steam in a sieve-tray tower. Use a weir height of 50 mm. Design for 80 approach to the flood velocity. A gas containing methane, propane, and n-butane is to be scrubbed countercurrently in a sieve-tray tower with a hydrocarbon oil to absorb principally the butane. A process for making small amounts of hydrogen by cracking ammonia is being considered, and residual uncracked ammonia is to be removed from the resulting gas. The gas will consist of H2 and N2 in the molar ratio 3:1, containing 3 NH3 by volume.

The ammonia will be removed by scrubbing the gas countercurrently with pure liquid water in a sieve-tray tower. Design for an 80 approach to the flood velocity. A sieve-tray tower is to be designed for distillation of a mixture of toluene and methylcyclohexane. Design for a 60 approach to the flood velocity. Check for excessive weeping. (b) Estimate the tray efficiency corrected for entrainment for the design reported in part (a). A a e idi g i e i ib i age i ed f i i ga ia f a a e ae ea b ea fc e c e ai a 1 a a d 300 K. Ca c a e he c ce a i f a ia i he e i a e if he i e i id c ce a i i 0.1 ea ia, he i e ai i f ee f a ia, a d 1.873 a da d c bic e e f ai a e fed he e e i ga f a e a e. S i Initial estimate 5.4a. Ammonia stripping from a wastewater in a tra tower. The Murphree plate efficienc for the ammonia stripper of Problem 5.3 is constant at 0.581. Estimate the number of real tra s required. Solution Use 9 tra s 5.5b. Ammonia stripping from a wastewater in a tra tower. A hea - i ea a 320 K i ed i a ab be e e di e a a ai ea. The hea i i he ec c ed bac he ce he e ce i bei g a i a ba i, a d i f ai f ca e- i ab be i a 16- a e ie e- a c.The de i ed. The c e c, a d he M a. h ee 5.7b. Absorption of ammonia in a laborator -scale tra tower. An absorption column for laboratory use has been carefully constructed so that it has exactly 4 equilibrium stages, and is being used to measure equilibrium data. Water is used as the solvent to absorb ammonia from air. The system operates isothermally at 300 K and 1 atm. The inlet water is pure distilled water. Assuming that Henry s law applies, calculate the slope of the equilibrium line. Solution Initial estimate 5.8c,d. Absorption of ammonia in a seive-tra tower. A process for making small amounts of hydrogen by cracking ammonia is being considered and residual, uncracked ammonia is to be removed from the resulting gas.

The gas will consist of H2 and N2 in the molar ratio 3:1, containing 3 NH3 by volume, at a pressure of 2 bars and a temperature of 303 K. There is available a sieve-tray tower, 0.75 m diameter, containing 6 cross-flow trays at 0.5 m tray spacing. The perforations are 4.75 mm in diameter, arranged in triangular pitch on 12.5 mm centers, punched in sheet metal 2 mm thick. The weir height is 40 mm. The gas flow rate should not exceed 80 of the flooding value.A a a fac i g d ice i b c e i ai d ce a f e ga hich, he c ea ed a d c ed, i c ai 15 CO2, 6 O2, a d 79 N2. A i id- -ga a i f 1.2 i e he i i i ecified. A e i he a eai.A 298 K a d 1.2 a, he e i ib i e f ac i f ca b di ide e a e i f e ha a i e (30 ) i gi e b he e A,i i he e f ac i a) Ca c a e he i g a S f CO2 i f i he i id i e e i g he e.Estimate the overall tra efficienc for the absorber, and the number of real tra s required. Estimate thhe average value of m at liquid concentrations along the operating line and use theaverage in the correlation given. Solution 5.11c,d. Absorption of carbon disulfide in a sieve-tra tower. Carbon disulfide, CS2, used as a solvent in a chemical plant, is evaporated from the product in a dryer into an inert gas (essentially N2) in order to avoid an explosion hazard. The CS2-N2 mixture is to be scrubbed with an absorbent hydrocarbon oil. The partial pressure of CS2 in the original gas is 50 mm Hg, and the CS2 concentration in the outlet gas is not to exceed 0.5. The oil enters the absorber essentially pure at a rate 1.5 times the minimum, and solutions of oil and CS2 follow Raoult s law. Design a sieve-tray tower for this process. Design for a gas velocity which is 70 of the flooding velocity. Determine the number of equilibrium tra s for the absorber of Problem 5.11, assuming adiabatic operation. A straw oil used to absorb benzene from coke-oven gas is to be steam-stripped in a sieve-plate column at atmospheric pressure to recover the disolved benzene, C6H6.