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1.1a. Concentration of a gas mi[ture. A Pi[WXUe Rf QRbOe gaVeV [heOiXP (1), aUgRQ (2), NU\SWRQ (3), aQd [eQRQ (4)] iV aW a WRWaO SUeVVXUe Rf 200 NPa aQd a WePSeUaWXUe Rf 400 K. If Whe Pi[WXUe haV eTXaO PROe fUacWiRQV Rf each Rf Whe gaVeV, deWeUPiQe: a) The cRPSRViWiRQ Rf Whe Pi[WXUe iQ WeUPV Rf PaVV fUacWiRQV. SROXWiRQ: BaViV: 100 NPROe Rf Whe Pi[WXUe b) The aYeUage PROecXOaU ZeighW Rf Whe Pi[WXUe. SROXWiRQ c) The WRWaO PROaU cRQceQWUaWiRQ. SROXWiRQ d) The PaVV deQViW\. SROXWiRQ 1.2a. ConcenWUaWion of a liTXid VolXWion fed Wo a diVWillaWion colXmn. A VolXWion of caUbon WeWUachloUide (1) and caUbon diVXlfide (2) conWaining 50% b\ ZeighW each iV Wo be conWinXoXVl\ diVWilled aW Whe UaWe of 4,000 kg/h DeWeUmine: a) The concenWUaWion of Whe mi[WXUe in WeUmV of mole fUacWionV. SolXWion BaViV: 100 kg mi[WXUe b) The aYeUage molecXlaU ZeighW of Whe mi[WXUe. SolXWion c) CalcXlaWe Whe feed UaWe in kmol/h. SolXWion 1.3a. ConcenWUaWion of liTXified naWXUal gaV. A VaPSOe Rf OiTXified QaWXUaO gaV, LNG, fURP AOaVNa haV Whe fROORZiQg PROaU cRPSRViWiRQ: 93.5% CH4, 4.6% C2H6, 1.2% C3H8, aQd 0.7% CO2. CaOcXOaWe: a) AYeUage PROecXOaU ZeighW Rf Whe LNG Pi[WXUe. SROXWiRQ b) WeighW fUacWiRQ Rf CH4 iQ Whe Pi[WXUe. SROXWiRQ BaViV: 100 NPROeV Rf LNG c) The LNG iV heaWed WR 300 K aQd 140 NPa, aQd YaSRUi]eV cRPSOeWeO\. EVWiPaWe Whe deQViW\ Rf Whe gaV Pi[WXUe XQdeU WheVe cRQdiWiRQV. SROXWiRQ 1.4b. ConcenWUaWion of a flXe gaV. A flXe gaV conViVWV of caUbon dio[ide, o[\gen, ZaWeU YapoU, and niWUogen. The molaU fUacWionV of CO2 and O2 in a Vample of Whe gaV aUe 12% and 6%, UeVpecWiYel\. The ZeighW fUacWion of H2O in Whe gaV iV 6.17%. EVWimaWe Whe denViW\ of WhiV gaV aW 500 K and 110 kPa. SolXWion BaViV: 100 kmole of gaV mi[WXUe LeW [ = molaU fUacWion of ZaWeU in Whe mi[WXUe (aV a peUcenW) IniWial eVWimaWe FUom Whe giYen ZaWeU ZeighW fUacWion (0.0617): 1.5b. Material balances around an ammonia gas absorber. A gaV VWUeaP fORZV aW Whe UaWe Rf 10.0 P3/V aW 300 K aQd 102 NPa. IW cRQViVWV Rf aQ eTXiPROaU Pi[WXUe Rf aPPRQia aQd aiU. The gaV eQWeUV WhURXgh Whe bRWWRP Rf a SacNed bed gaV abVRUbeU ZheUe iW fORZV cRXQWeUcRXUUeQW WR a VWUeaP Rf SXUe OiTXid ZaWeU WhaW abVRUbV 90% Rf aOO Rf Whe aPPRQia, aQd YiUWXaOO\ QR aiU. The abVRUbeU YeVVeO iV c\OiQdUicaO ZiWh aQ iQWeUQaO diaPeWeU Rf 2.5 P. a) NegOecWiQg Whe eYaSRUaWiRQ Rf ZaWeU, caOcXOaWe Whe aPPRQia PRO fUacWiRQ iQ Whe gaV OeaYiQg Whe abVRUbeU. SROXWiRQ: BaViV: 1 VecRQd A = aPPRQia B = aiU b) CaOcXOaWe Whe RXWOeW gaV PaVV YeORciW\ (defiQed aV PaVV fORZ UaWe SeU XQiW ePSW\ WXbe cURVV-VecWiRQaO aUea). SROXWiRQ: 1.6b. Velocities and flu[es in a gas mi[ture. A gaV Pi[WXUe aW a WRWaO SUeVVXUe Rf 150 NPa aQd 295 K cRQWaiQV 20% H2, 40% O2, aQd 40% H2O b\ YROXPe. The abVROXWe YeORciWieV Rf each VSecieV aUe -10 P/V, -2 P/V, aQd 12 P/V, UeVSecWiYeO\, aOO in the direction of the ]-a[is. a) Determine the mass average velocit\, v, and the molar average velocit\, V, for the 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. PUopeUWieV of aiU VaWXUaWed ZiWh ZaWeU YapoU. AiU, VWRUed iQ a 30-P3 cRQWaiQeU aW 340 K aQd 101.3 NPa iV VaWXUaWedZiWh ZaWeU YaSRU. DeWeUPiQe Whe fROORZiQg SURSeUWieV Rf Whe gaV Pi[WXUe: a) MROe fUacWiRQ Rf ZaWeU YaSRU. b) AYeUage PROecXOaU ZeighW Rf Whe Pi[WXUe. c) TRWaO PaVV cRQWaiQed iQ Whe WaQN. d) MaVV Rf ZaWeU YaSRU iQ Whe WaQN. SROXWiRQ a) AQWRiQe eTXaWiRQ fRU ZaWeU YaSRU: FRU a VaWXUaWed Pi[WXUe b) c) d) 1.8c. WaWeU balance aUoXnd an indXVWUial cooling WoZeU. The cRROiQg ZaWeU fORZ UaWe WR Whe cRQdeQVeUV Rf a big cRaO-fiUed SRZeU SOaQW iV 8,970 Ng/V. The ZaWeU eQWeUV Whe cRQdeQVeUV aW 29 qC aQd OeaYeV aW 45 qC. FURP Whe cRQdeQVeUV, Whe ZaWeU fORZV WR a cRROiQg WRZeU ZheUe iW iV cRROed dRZQ bacN WR 29 qC b\ cRXQWeUcRXUUeQW cRQWacW ZiWh aiU (Vee FigXUe 1.11). The aiU eQWeUV Whe cRROiQg WRZeU aW Whe UaWe Rf 6,500 Ng/V Rf dU\ aiU, aW a dU\-bXOb WePSeUaWXUe Rf 30 qC aQd a hXPidiW\ Rf 0.016 Ng Rf ZaWeU/Ng Rf dU\ aiU. IW OeaYeV Whe cRROiQg WRZeU VaWXUaWed ZiWh ZaWeU YaSRU aW 38 qC. a) CaOcXOaWe Whe ZaWeU ORVVeV b\ eYaSRUaWiRQ iQ Whe cRROiQg WRZeU. SROXWiRQ CRQVideU Whe aiU OeaYiQg Whe WRZeU VaWXUaWed aW 38 qC. AQWRiQe eTXaWiRQ fRU ZaWeU YaSRU: E = ZaWeU ORVW b\ eYaSRUaWiRQ iQ Whe aiU b) TR accRXQW fRU ZaWeU ORVVeV iQ Whe cRROiQg WRZeU, SaUW Rf Whe effOXeQW fURP a QeaUb\ PXQiciSaO ZaVWeZaWeU WUeaWPeQW SOaQW ZiOO be XVed aV PaNeXS ZaWeU. ThiV PaNeXS ZaWeU cRQWaiQV 500 Pg/L Rf diVVROYed VROidV. TR aYRid fRXOiQg Rf Whe cRQdeQVeU heaW-WUaQVfeU VXUfaceV, Whe ciUcXOaWiQg ZaWeU iV WR cRQWaiQ QR PRUe WhaQ 2,000 Pg/L Rf diVVROYed VROidV. TheUefRUe, a VPaOO aPRXQW Rf Whe ciUcXOaWiQg ZaWeU PXVW be deOibeUaWeO\ diVcaUded (bORZdRZQ). WiQdage ORVVeV fURP Whe WRZeU aUe eVWiPaWed aW 0.2% Rf Whe UeciUcXOaWiRQ UaWe. EVWiPaWe Whe PaNeXS-ZaWeU UeTXiUePeQW. SROXWiRQ W = ZiQdage ORVVeV [P = 500 SSP [c = 2000 SSP M = PaNeXS ZaWeU UaWe B = bORZdRZQ UaWe IQiWiaO eVWiPaWeV WaWeU baOaQce SROidV baOaQce: 1.9b. Water balance around a soap dr\er. It is desired to dr\ 10 kg/min of soap continuousl\ from 17% moisture b\ weight to 4% moisture in a countercourrent stream of hot air. The air enters the dr\er at the rate of 30.0 m3/min at 350 K, 101.3 kPa, and initial water-vapor partial pressure of 1.6 kPa. The dr\er operates at constant temperature and pressure. a) Calculate the moisture content of the entering air, in kg of water/kg of dr\ air. Solution b) Calculate the flow rate of dr\ air, in kg/min. Solution c) Calculate the water-vapor partial pressure and relative humidit\ in the air leaving the dr\er. Solution CalcXlaWe ZaWeU YaSRU SUeVVXUe aW 350 K AQWRiQe eTXaWiRQ fRU ZaWeU YaSRU: 1.10b. ActiYated carbon adsorption; material balances. A ZaVWe gaV cRQWaiQV 0.3% WROXeQe iQ aiU, aQd RccXSieV a YROXPe Rf 2,500 P3 aW 298 K aQd 101.3 NPa. IQ aQ effRUW WR UedXce Whe WROXeQe cRQWeQW Rf WhiV gaV, iW iV e[SRVed WR 100 Ng Rf acWiYaWed caUbRQ, iQiWiaOO\ fUee Rf WROXeQe. The V\VWeP iV aOORZed WR Ueach eTXiOibUiXP aW cRQVWaQW WePSeUaWXUe aQd SUeVVXUe. AVVXPiQg WhaW Whe aiU dReV QRW adVRUb RQ Whe caUbRQ, caOcXOaWe Whe eTXiOibUiXP cRQceQWUaWiRQ Rf WROXeQe iQ Whe gaVeRXV ShaVe, aQd Whe aPRXQW Rf WROXeQe adVRUbed b\ Whe caUbRQ. The adVRUSWiRQ eTXiOibUiXP fRU WhiV V\VWeP iV giYeQ b\ Whe FUeXQdOich iVRWheUP(EAB CRQWURO CRVW MaQXaO, 3Ud. ed., U. S. E. P. A., ReVeaUch TUiaQgOe PaUN, NC, 1987.): ZheUe W iV Whe caUbRQ eTXiOibUiXP adVRUSWiYiW\, iQ Ng Rf WROXeQe/Ng Rf caUbRQ, aQd S* iV Whe eTXiOibUiXP WROXeQe SaUWiaO SUeVVXUe, iQ Pa, aQd PXVW be beWZeeQ 0.7 aQd 345 Pa. SROXWiRQ M = PaVV Rf caUbRQ [ = PROeV Rf WROXeQe adVRUbed IQiWiaO eVWiPaWeV 1.11b. ActiYated carbon adsorption; material balances. It is desired to adsorb 99.5% of the toluene originall\ present in the waste gas of Problem 1.10. Estimate how much activated carbon should be used if the s\stem is allowed to reach equilibrium at constant temperature and pressure. Solution 1.12a, d. Estimation of gas diffusivit\ b\ the Wilke-Lee equation. E. M. LaUVRQ (MS WheViV, OUegRQ SWaWe UQiYeUViW\, 1964) PeaVXUed Whe diffXViYiW\ Rf chORURfRUP iQ aiU aW 298 K aQd 1 aWP aQd UeSRUWed iWV YaOXe aV 0.093 cP2/V. EVWiPaWe Whe diffXViRQ cRefficieQW b\ Whe WiONe-Lee eTXaWiRQ aQd cRPSaUe iW ZiWh Whe e[SeUiPeQWaO YaOXe. SROXWiRQ FURP ASSeQdi[ B 1.13a, d. Estimation of gas diffusivit\ b\ the Wilke-Lee equation. a) EVWimaWe Whe diffXViYiW\ of naphWhalene (C10H8) in aiU aW 303 K and 1 baU. CompaUe iW ZiWh Whe e[peUimenWal YalXe of 0.087 cm2/V UepoUWed in Appendi[ A. The noUmal boiling poinW of naphWhalene iV 491.1 K, and iWV cUiWical YolXme iV 413 cm3/mol. SolXWion E[peUimenWal YalXe b) EVWimaWe WhediffXViYiW\ of p\Uidine (C5H5N) in h\dUogen aW 318 K and 1 aWm. CompaUe iW ZiWh Whe e[peUimenWal YalXe of 0.437 cm2/V UepoUWed in Appendi[ A. The noUmal boiling poinW of p\Uidine iV 388.4 K, and iWV cUiWical YolXme iV 254 cm3/mol. SolXWion E[peUimenWal YalXe c) EVWimaWe Whe diffXViYiW\ of aniline (C6H7N) in aiU aW 273 K and 1 aWm. CompaUe iW ZiWh Whe e[peUimenWal YalXe of 0.061 cm2/V (GXilliland, E. R., IQd. EQg. CheP., 2�:681, 1934). The noUmal boiling poinW of aniline iV 457.6 K, and iWV cUiWical YolXme iV 274 cm3/mol. SolXWion E[peUimenWal YalXe 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 DeYelop., 8:240, 1969) has suggested an alternative method for this case. Equation (1-49) is still used, but the collision integral is now given by mp = dipole moment, debyes [1 debye = 3.162 u 10 -25 (J- m3)1/2] a) Modify the Mathcad routine of Figure 1.3 to implement Brokaw's method. Use the function name DABp(T, P, MA, MB, mA, mB, VA, VB, TbA, TbB) Solution b) EVWiPaWe Whe diffXViRQ cRefficieQW fRU a Pi[WXUe Rf PeWh\O chORUide aQd VXOfXU diR[ide aW 1 baU aQd 323 K, aQd cRPSaUe iW WR Whe e[SeUiPeQWaO YaOXe Rf 0.078 cP2/V. The daWa UeTXiUed WR XVe BURNaZ'V UeOaWiRQ aUe VhRZQ beORZ (Reid, eW aO., 1987): PaUaPeWeU MeWh\O chORUide SXOfXU diR[ide Tb , K 249.1 263.2 Vb , cP 3/PRO 50.6 43.8 PS, deb\eV 1.9 1.6 M 50.5 64.06 SROXWiRQ 1.15d. Diffusivit\ of polar gases EYaOXaWe Whe diffXViRQ cRefficieQW Rf h\dURgeQ chORUide iQ ZaWeU aW 373 K aQd 1 baU. The daWa UeTXiUed WR XVe BURNaZ'V UeOaWiRQ (Vee PURbOeP 1.14) aUe VhRZQ beORZ (Reid, eW aO., 1987): PaUaPeWeU H\dURgeQ chORUide WaWeU Tb , K 188.1 373.2 Vb , cP3/PRO 30.6 18.9 PS, deb\eV 1.1 1.8 M 36.5 18 SROXWiRQ 1.16d. Diffusivit\ of polar gases EYaOXaWe Whe diffXViRQ cRefficieQW Rf h\dURgeQ VXOfide iQ VXOfXU diR[ide aW 298 K aQd 1.5 baU. The daWa UeTXiUed WR XVe BURNaZ'V UeOaWiRQ (VeePURbOeP 1.14) aUe VhRZQ beORZ (Reid, eW aO., 1987): PaUaPeWeU H\dURgeQ VXOfide SXOfXU diR[ide Tb , K 189.6 263.2 Vb , cP3/PRO 35.03 43.8 PS, deb\eV 0.9 1.6 M 34.08 64.06 SROXWiRQ 1.17a,d. Effective diffusivit\ in a multicomponent stagnant gas mi[ture. 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. Meserole, et al. (J. AiU & WaVWe Manage. AVVoc., 49:694-704, 1999) describe a theoretical model for estimating mercur\ removal b\ the sorbent injection process. 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. Meserole et al. reported an effective diffusivit\ value of 0.22 cm2/s. Solution HgCl2 (1) O2 (2) CO2 (3) H2O (4) N2 (5) 1.19a. Wilke-Chang method for liquid diffusivit\. EVWiPaWe Whe OiTXid diffXViYiW\ Rf caUbRQ WeWUachORUide iQ diOXWe VROXWiRQ iQWR eWhaQRO aW 298 K. CRPSaUe WR Whe e[SeUiPeQWaO YaOXe UeSRUWed b\ Reid, eW aO. (1987) aV 1.5 u 10-5 cP2/V. The cUiWicaO YROXPe Rf caUbRQ WeWUachORUide iV 275.9 cP3/PRO. The YiVcRViW\ Rf OiTXid eWhaQRO aW 298 K iV 1.08 cP. SROXWiRQ 1.20b. Diffusion in electrol\te solutions. WheQ a VaOW diVVRciaWeV iQ VROXWiRQ, iRQV UaWheU WhaQ PROecXOeV diffXVe. IQ Whe abVeQce Rf aQ eOecWUic SRWeQWiaO, Whe diffXViRQ Rf a ViQgOe VaOW Pa\ be WUeaWed aV PROecXOaU diffXViRQ. FRU diOXWe VROXWiRQV Rf a ViQgOe VaOW, Whe diffXViRQ cRefficieQW iV giYeQ b\ Whe NeUQVW-HaVNeOO eTXaWiRQ (HaUQed, H. S., aQd B. B. OZeQ, "The Ph\VicaO ChePiVWU\ Rf EOecWURO\Wic SROXWiRQV," ACS MRQRgU. 95, 1950): a) EVWiPaWe Whe diffXViRQ cRefficieQW aW 298 K fRU a YeU\ diOXWe VROXWiRQ Rf HCO iQ ZaWeU. SROXWiRQ b) EVWiPaWe Whe diffXViRQ cRefficieQW aW 273 K fRU a YeU\ diOXWe VROXWiRQ Rf CXSO4 iQ ZaWeU. The YiVcRViW\ Rf OiTXid ZaWeU aW 273 K iV 1.79 cP. 1.21a. O[\gen diffusion in Zater: Ha\duk and Minhas correlation. Estimate the diffusion coefficient of oxygen in liquid water at 298 K. Use the Hayduk and Minhas correlation for solutes in aqueous solutions. At this temperature, the viscosity of water is 0.9 cP. The critical volume of oxygen is 73.4 cm3/mol. The experimental value of this diffusivity was reported as 2.1 u 10ç5 cm2/s (Cussler E. L., DiffXsion, 2nd ed, Cambridge University Press, Cambridge, UK, 1997). Solution 1.22a, d. Liquid diffusivit\: Ha\duk and Minhas correlation. 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 the estimate to the reported value of 3.7 u 10ç5 cm2/s. The following data are available (Reid, et al., 1987): Solution 1.23b. EVWimaWing molaU YolXmeV fUom liTXid diffXVion daWa. The diffusivity of allyl alcohol (C3H6O) in dilute aqueous solution at 288 K is 0.9 u 10 ç5 cm2/s (Reid, et al., 1987). Based on this result, and the Hayduk and Minhas correlation for aqueous solutions, estimate the molar volume of allyl alcohol at its normal boiling point. 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. a) EVWiPaWe Whe diffXViYiW\ Rf eWhaQRO iQ ZaWeU aW 298 K ZheQ Whe PRO fUacWiRQ Rf eWhaQRO iQ VROXWiRQ iV 40%. UQdeU WheVe cRQdiWiRQV (HaPPRQd, B. R., aQd R. H. SWRNeV, Trans. Farada\ Soc., 49, 890, 1953): The e[SeUiPeQWaO YaOXe UeSRUWed b\ HaPPRQd aQd SWRNeV (1953) iV 0.42 u 10-5 cP2/V. SROXWiRQ EVWiPaWe Whe iQfiQiWe diOXWiRQ diffXViYiW\ Rf eWhaQRO iQ ZaWeU aW 298 K fURP Ha\dXN-MiQhaV fRU aTXeRXV VROXWiRQV FURP ASSeQdi[ A, Whe iQfiQiWe diOXWiRQ diffXViYiW\ Rf ZaWeU iQ eWhaQRO aW 298 K iV b) EVWiPaWe Whe diffXViYiW\ Rf aceWRQe iQ ZaWeU aW 298 K ZheQ Whe PRO fUacWiRQ Rf aceWRQe iQ VROXWiRQ iV 35%. FRU WhiV V\VWeP aW 298 K, Whe acWiYiW\ cRefficieQW fRU aceWRQe iV giYeQ b\ WiOVRQ eTXaWiRQ (SPiWh, J. M., eW aO., Introduction to Chemical Engineering Thermod\namics, 5Wh ed, McGUaZ-HiOO CR., IQc., NeZ YRUN, NY, 1996): SROXWiRQ EVWiPaWe Whe WheUPRd\QaPic facWRU FURP ASSeQdi[ A EVWiPaWe Whe iQfiQiWe diOXWiRQ diffXViYiW\ Rf aceWRQe iQ ZaWeU aW 298 K fURP Ha\dXN-MiQhaV fRU aTXeRXV VROXWiRQV 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. Estimate the rate of combustion of the carbon, in kg/m2-min. Solution CO (1), CO2 (2),O2 (3) Calculate binar\ MS diffusivities from Wilke-Lee Appendi[ C-2: Solution of the Ma[Zell-Stefan equations for a multicomponent mi[ture of ideal gases b\ orthogonal collocation (1C = 3). Orthogonal collocation matrices The pUeVVXUe and WempeUaWXUe in Whe YapoXU phaVe aUe The Ma[Zell-SWefan diffXVion coefficicienWV aUe 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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alculate diffusivity 1.27c, d. MolecXlaU diffXVion WhUoXgh a gaV-liTXid inWeUface. 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. The diffusivity of ammonia in air under these conditions is 0.215 cm2/s and in liquid water is 1.77 u 10ç5 cm2/s. Neglecting water evaporation, determine the rate of diffusion of ammonia, in kg/m2-hr. Assume that the gas and liquid are in equilibrium at the interface. SolXWion: IniWial eVWimaWeV: 1.28c. Stead\-state molecular diffusion in gases. A Pi[WXUe Rf eWhaQRO aQd ZaWeU YaSRU iV beiQg UecWified iQ aQ adiabaWic diVWiOOaWiRQ cROXPQ. The aOcRhRO iV YaSRUi]ed aQd WUaQVfeUUed fURP Whe OiTXid WR Whe YaSRU ShaVe. WaWeU YaSRU cRQdeQVeV (eQRXgh WR VXSO\ Whe OaWeQW heaW Rf YaSRUi]aWiRQ Qeeded b\ Whe aOcRhRO beiQg eYaSRUaWed) aQd iV WUaQVfeUUed fURP Whe YaSRU WR Whe OiTXid ShaVe. BRWh cRPSRQeQWV diffXVe WhURXgh a gaV fiOP 0.1 PP WhicN. The WePSeUaWXUe iV 368 K aQd Whe SUeVVXUe iV 1 aWP. The PROe fUacWiRQ Rf eWhaQRO iV 0.8 RQ RQe Vide Rf Whe fiOP aQd 0.2 RQ Whe RWheU Vide Rf Whe fiOP. CaOcXOaWe Whe UaWe Rf diffXViRQ Rf eWhaQRO aQd Rf ZaWeU, iQ Ng/P2-V. The OaWeQW heaW Rf YaSRUi]aWiRQ Rf Whe aOcRhRO aQd ZaWeU aW 368 K caQ be eVWiPaWed b\ Whe PiW]eU aceQWUic facWRU cRUUeOaWiRQ (Reid, eW aO., 1987) ZheUe Z iV Whe aceQWUic facWRU. SROXWiRQ A = eWhaQRO B = ZaWeU CaOcXOaWe eWhaQRO heaW Rf YaSRUi]aWiRQ CaOcXOaWe ZaWeU heaW Rf YaSRUi]aWiRQ EVWiPaWe diffXViYiW\ fURP WiONe-Lee 1.29a, d. Analog\ among molecular heat and mass transfer. It has been observed that for the s\stem air-water vapor at near ambient conditions, Le = 1.0 (Tre\bal, 1980). This observation, called the Lewis relation, has profound implications in humidification operations, as will be seen later. 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 Wilke- Lee equation. For air at 300 K and 1 atm:Cp = 1.01 kJ/kg-K, k = 0.0262 W/m-K, m = 1.846 u 10 -5 kg/m-s, and r = 1.18 kg/m3. Solution Estimate diffusivit\ from the Wilke-Lee equation 1.30b, d. Stead\-state molecular diffusion in gases. WaWeU eYaSRUaWiQg fURP a SRQd aW 300 K dReV VR b\ PROecXOaU diffXViRQ acURVV aQ aiU fiOP 1.5 PP WhicN. If Whe UeOaWiYe hXPidiW\ Rf Whe aiU aW Whe RXWeU edge Rf Whe fiOP iV 20%, aQd Whe WRWaO SUeVVXUe iV 1 baU, eVWiPaWe Whe dURS iQ Whe ZaWeU OeYeO SeU da\, aVVXPiQg WhaW cRQdiWiRQV iQ Whe fiOP UePaiQ cRQVWaQW. The YaSRU SUeVVXUe Rf ZaWeU aV a fXQcWiRQ Rf WePSeUaWXUe caQ be accXUaWeO\ eVWiPaWed fURP Whe WagQeU eTXaWiRQ (Reid, eW aO., 1987) SROXWiRQ FURP ASSeQdi[ A 1.31b, d. Stead\-state molecular diffusion in a ternar\ gas s\stem. CaOcXOaWe Whe fOX[eV aQd cRQceQWUaWiRQ SURfiOeV fRU Whe WeUQaU\ V\VWeP h\dURgeQ (1), QiWURgeQ (2), aQd caUbRQ diR[ide (3) XQdeU Whe fROORZiQg cRQdiWiRQV. The WePSeUaWXUe iV 308 K aQd Whe SUeVVXUe iV 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. The total molar flu[ is ]ero, 1 = 0. The MS diffusion coefficients are D12 = 83.8 mm 2/s, D13 = 68.0 mm2/s, D23 = 16.8 mm 2/s. Solution Appendi[ C-1: Solution of the Ma[Zell-Stefan equations for a multicomponent mi[ture of ideal gases b\ orthogonal collocation (1C = 3). Orthogonal collocation matrices The pUeVVXUe and WempeUaWXUe in Whe YapoXU phaVe aUe The Ma[Zell-SWefan diffXVion coefficicienWV aUe The lengWh of Whe diffXVion paWh iV The denViW\ of Whe gaV phaVe folloZV fUom Whe ideal gaV laZ Initial estimates of the flu[es Initial estimates of the concentrations 2.1a. MaVV-WUanVfeU coefficienWV in a gaV abVoUbeU. A gaV abVRUbeU iV XVed WR UePRYe beQ]eQe (C6H6) YaSRUV fURP aiU b\ VcUXbbiQg Whe gaV Pi[WXUe ZiWh a QRQYROaWiOe RiO aW 300 K aQd 1 aWP. AW a ceUWaiQ SRiQW iQ Whe abVRUbeU, Whe beQ]eQe PROe fUacWiRQ iQ Whe bXON Rf Whe gaV ShaVe iV 0.02, ZhiOe Whe cRUUeVSRQdiQg iQWeUfaciaO beQ]eQe gaV- ShaVe cRQceQWUaWiRQ iV 0.0158. The beQ]eQe fOX[ aW WhaW SRiQW iV PeaVXUed aV 0.62 g/P2-V. a) CaOcXOaWe Whe PaVV-WUaQVfeU cRefficieQW iQ Whe gaV ShaVe aW WhaW SRiQW iQ Whe eTXiSPeQW, e[SUeVViQg Whe dUiYiQg fRUce iQ WeUPV Rf PROe fUacWiRQV . SROXWiRQ b) CaOcXOaWe Whe PaVV-WUaQVfeU cRefficieQW iQ Whe gaV ShaVe aW WhaW SRiQW iQ Whe eTXiSPeQW, e[SUeVViQg Whe dUiYiQg fRUce iQ WeUPV Rf PROaU cRQceQWUaWiRQV, NPRO/P3. SROXWiRQ c) AW Whe VaPe SOace iQ Whe eTXiSPeQW, Whe beQ]eQe PROe fUacWiRQ iQ Whe bXON Rf Whe OiTXid ShaVe iV 0.125, ZhiOe Whe cRUUeVSRQdiQg iQWeUfaciaO beQ]eQe OiTXid-ShaVe cRQceQWUaWiRQ iV 0.158. CaOcXOaWe Whe PaVV-WUaQVfeU cRefficieQW iQ Whe OiTXid ShaVe, e[SUeVViQg Whe dUiYiQg fRUce iQ WeUPV Rf PROe fUacWiRQV. SROXWiRQ 2.2a. MaVV-WUanVfeU coefficienWV fUom naphWhalene VXblimaWion daWa. IQ a OabRUaWRU\ e[SeUiPeQW, aiU aW 347 K aQd 1 aWP iV bORZQ aW high VSeed aURXQd a ViQgOe QaShWhaOeQe (C10H8) VSheUe, Zhich VXbOiPaWeV SaUWiaOO\. WheQ Whe e[SeUiPeQW begiQV, Whe diaPeWeU Rf Whe VSheUe iV 2.0 cP. AW Whe eQd Rf Whe e[SeUiPeQW, 14.32 PiQ OaWeU, Whe diaPeWeU Rf Whe VSheUe iV 1.85 cP. a) EVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW, baVed RQ Whe aYeUage VXUface aUea Rf Whe SaUWicOe, e[SUeVViQg Whe dUiYiQg fRUce iQ WeUPV Rf SaUWiaO SUeVVXUeV. The deQViW\ Rf VROid QaShWhaOeQe iV 1.145 g/cP3, iWV YaSRU SUeVVXUe aW 347 K iV 670 Pa (PeUU\ aQd ChiOWRQ, 1973). SROXWiRQ b) CaOcXOaWe Whe PaVV-WUaQVfeU cRefficieQW, fRU Whe dUiYiQg fRUce iQ WeUPV Rf PROaU cRQceQWUaWiRQV. SROXWiRQ 2.3a. Mass-transfer coefficients from acetone eYaporation data. IQ a OabRUaWRU\ e[SeUiPeQW, aiU aW 300 K aQd 1 aWP iV bORZQ aW high VSeed SaUaOOeO WR Whe VXUface Rf a UecWaQgXOaU VhaOORZ SaQ WhaW cRQWaiQV OiTXid aceWRQe(C3H6O), Zhich eYaSRUaWeV SaUWiaOO\. The SaQ iV 1 P ORQg aQd 50 cPV Zide. IW iV cRQQecWed WR a UeVeUYRiU cRQWaiQiQg OiTXid aceWRQe Zhich aXWRPaWicaOO\ UeSOaceV Whe aceWRQe eYaSRUaWed, PaiQWaiQiQg a cRQVWaQW OiTXid OeYeO iQ Whe SaQ. DXUiQg aQ e[SeUiPeQWaO UXQ, iW ZaV RbVeUYed WhaW 2.0 L Rf aceWRQe eYaSRUaWed iQ 5 PiQ. EVWiPaWe Whe PaVV- WUaQVfeU cRefficieQW. The deQViW\ Rf OiTXid aceWRQe aW 300 K iV 0.79 g/cP3; iWV YaSRU SUeVVXUe iV 27 NPa (PeUU\ aQd ChiOWRQ, 1973). SROXWiRQ 2.4b. Mass-transfer coefficients from Zetted-Zall e[perimental data. A ZeWWed-ZaOO e[SeUiPeQWaO VeW-XS cRQViVWV Rf a gOaVV SiSe, 50 PP iQ diaPeWeU aQd 1.0 P ORQg. WaWeU aW 308 K fORZV dRZQ Whe iQQeU ZaOO. DU\ aiU eQWeUV Whe bRWWRP Rf Whe SiSe aW Whe UaWe Rf 1.04 P3/PiQ, PeaVXUed aW 308 K aQd 1 aWP. IW OeaYeV Whe ZeWWed VecWiRQ aW 308 K aQd ZiWh a UeOaWiYe hXPidiW\ Rf 34%. WiWh Whe heOS Rf eTXaWiRQ (2-52), eVWiPaWe Whe aYeUage PaVV-WUaQVfeU cRefficieQW, ZiWh Whe dUiYiQg fRUce iQ WeUPV Rf PROaU fUacWiRQV. SROXWiRQ 2.7c. MaVV WUanVfeU in an annXlaU Vpace. a) IQ VWXd\iQg UaWeV Rf diffXViRQ Rf QaShWhaOeQe iQWR aiU, aQ iQYeVWigaWRU UeSOaced a 30.5-cP VecWiRQ Rf Whe iQQeU SiSe Rf aQ aQQXOXV ZiWh a QaShWhaOeQe URd. The aQQXOXV ZaV cRPSRVed Rf a 51-PP-OD bUaVV iQQeU SiSe VXUURXQded b\ a 76-PP-ID bUaVV SiSe. WhiOe RSeUaWiQg aW a PaVV YeORciW\ ZiWhiQ Whe aQQXOXV Rf 12.2 Ng Rf aiU/P2-V aW 273 K aQd 1 aWP, Whe iQYeVWigaWRU deWeUPiQed WhaW Whe SaUWiaO SUeVVXUe Rf QaShWhaOeQe iQ Whe e[iWiQg gaV VWUeaP ZaV 0.041 Pa. UQdeU Whe cRQdiWiRQV Rf Whe iQYeVWigaWiRQ, Whe SchPidW QXPbeU Rf Whe gaV ZaV 2.57, Whe YiVcRViW\ ZaV 175 PP, aQd Whe YaSRU SUeVVXUe Rf QaShWhaOeQe ZaV 1.03 Pa. EVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW fURP Whe iQQeU ZaOO fRU WhiV VeW Rf cRQdiWiRQV. AVVXPe WhaW eTXaWiRQ (2-52) aSSOieV. SROXWiRQ b) MRQUad aQd PeOWRQ (TUanV. AIChE, 38, 593, 1942) SUeVeQWed Whe fROORZiQg cRUUeOaWiRQ fRU heaW-WUaQVfeU cRefficieQW iQ aQ aQQXOaU VSace: ZheUe dR aQd di aUe Whe RXWVide aQd iQVide diaPeWeUV Rf Whe aQQXOXV, de iV Whe eTXiYaOeQW diaPeWeU defiQed aV WUiWe dRZQ Whe aQaORgRXV e[SUeVViRQ fRU PaVV WUaQVfeU aQd XVe iW WR eVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW fRU Whe cRQdiWiRQV Rf SaUW a). CRPSaUe bRWh UeVXOWV. SROXWiRQ 2.8c. The Chilton-Colburn analog\: flow across tube banks. WLQGLQJ DQG CKHQH\ (IQd. EQg. Che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b) EVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW WR be e[SecWed fRU eYaSRUaWiRQ Rf Q-SURS\O aOcRhRO iQWR caUbRQ diR[ide fRU Whe VaPe geRPeWUicaO aUUaQgePeQW ZheQ Whe caUbRQ diR[ide fORZV aW a Pa[iPXP YeORciW\ Rf 10 P/V aW 300 K aQd 1 aWP. The YaSRU SUeVVXUe Rf Q-SURS\O aOcRhRO aW 300 K iV 2.7 NPa. SROXWiRQ PURSeUWieV Rf diOXWe Pi[WXUeV Rf SURS\O aOcRhRO iQ caUbRQ diR[ide aW 300 K aQd 1 aWP: c) ZaNaXVNaV (AdY. Heat Transfer, �, 93, 1972) SURSRVed Whe fROORZiQg cRUUeOaWiRQ fRU Whe heaW- WUaQVfeU cRefficieQW iQ a VWaggeUed WXbe baQN aUUaQgePeQW ViPiOaU WR WhaW VWXdied b\ WiQdiQg aQd CheQe\: UVe Whe PaVV-WUaQVfeU e[SUeVViRQ aQaORgRXV WR eTXaWiRQ (2-69) WR eVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW Rf SaUW b). CRPSaUe Whe UeVXOWV. SROXWiRQ 2.9b. MaVV WUanVfeU fUom a flaW plaWe. A 1-m square thin plate of solid naphthalene is oriented parallel to a stream of air flowing at 20 m/s. The air is at 310 K and 101.3 kPa. The naphthalene remains at 290 K; at this temperature the vapor pressure of naphthalene is 26 Pa. Estimate the moles of naphthalene lost from the plate per hour, if the end effects can be ignored. Solution 2.10b. MaVV WUanVfeU fUom a flaW plaWe. A thin plate of solid salt, NaCl, measuring 15 by 15 cm, is to be dragged through seawater at a velocity of 0.6 m/s. The 291 K seawater has a salt concentration of 0.0309 g/cm3. Estimate the rate at which the salt goes into solution if the edge effects can be ignored. Assume that the kinematic viscosity at the average liquid film conditions is 1.02 u 10ç6 m2/s, and the diffusivity is 1.25 u 10ç9 m2/s. The solubility of NaCl in water at 291 K is 0.35 g/cm3, and the density of the saturated solution is 1.22 g/cm3 (Perry and Chilton, 1973) . Solution Laminar floZ At the bulk of the solution, point 2: At the interface, point 1: 2.11b. MaVV WUanVfeU fUom a flaW liTXid VXUface. DXUiQg Whe e[SeUiPeQW deVcUibed iQ PURbOeP 2.3, Whe aiU YeORciW\ ZaV PeaVXUed aW 6 P/V, SaUaOOeO WR Whe ORQgeVW Vide Rf Whe SaQ. EVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW SUedicWed b\ eTXaWiRQ (2-28) RU (2-29) aQd cRPSaUe iW WR Whe YaOXe PeaVXUed e[SeUiPeQWaOO\. NRWice WhaW, dXe WR Whe high YROaWiOiW\ Rf aceWRQe, Whe aYeUage aceWRQe cRQceQWUaWiRQ iQ Whe gaV fiOP iV UeOaWiYeO\ high. TheUefRUe, SURSeUWieV VXch aV deQViW\ aQd YiVcRViW\ VhRXOd be eVWiPaWed caUefXOO\. The fROORZiQg daWa fRU aceWRQe PighW be Qeeded: Tc = 508.1 K, Pc = 47.0 baU, M = 58, Vc = 209 cP 3/PRO, Zc = 0.232 (Reid, eW aO., 1987). SROXWiRQ AYeUage fiOP SURSeUWieV: EVWiPaWe Whe YiVcRViW\ Rf Whe Pi[WXUe fURP LXcaV MeWhRd EVWiPaWe Whe diffXViYiW\ fURP Whe WiONe-Lee eTXaWiRQ 2.12b. EYaporation of a drop of Zater falling in air. Repeat E[ample 2.9 for a drop of Zater Zhich is originall\ 2 mm in diameter. Solution 2.13b. Dissolution of a solid sphere into a floZing 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. The velocity of the 291 K water stream is 1.0 m/s. Assume that the kinematic viscosity at the average liquid film conditions is 1.02 u 10ç6 m2/s, and the mass diffusivity is 1.25 u 10ç9 m2/s. The solubility of NaCl in water at 291 K is 0.35 g/cm3, and the density of the saturated solution is 1.22 g/cm3 (Perry and Chilton, 1973) . Solution From Prob. 2.10: 2.14b. Sublimation of a solid sphere into a gas stream. During the experiment described in Problem 2.2, the air velocity was measured at 10 m/s. Estimate the mass-transfer coefficient predicted by equation (2-36) and compare it to the value measured experimentally. The following data for naphthalene might be needed: Tb = 491.1 K, Vc = 413 cm3/mol. 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 floZing liquid stream. The cr\stal of Problem 1.26 is a sphere 2-cm in diameter. It is falling at terminal velocit\ under the influence of gravit\ into a big tank of water at 288 K. The densit\ of the cr\stal is 1,464 kg/m3 (Perr\ and Chilton, 1973). a) Estimate the cr\stal's terminal velocit\. 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). The water flows slowly, at 298 K and 0.1 cm/s. The pipe is 1-cm in diameter. Under these conditions, equation (2-63) applies. a) Show that a material balance on a length of pipe Lleads to where v is the average fluid velocity, and cA* is the equilibrium solubility concentration. b) What is the average concentration of benzoic acid in the water after 2 m of pipe. The solubility of benzoic acid in water at 298 K is 0.003 g/cm3, and the mass diffusivity is 1.0 u 10ç5 cm2/s (Cussler, 1997). Solution 2.17b. Mass transfer in a Zetted-Zall toZer. 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. Dry air enters at the rate of 7 kg/m2-s. Assume the air is everywhere at its average conditions of 309 K and 1 atm, the water at 294 K, and the mass-transfer coefficient constant. Compute the average partial pressure of water in the air leaving if the tower is 1 P ORQg. SROXWiRQ FRU ZaWeU aW 294 K 2.18c. MaVV WUanVfeU in an annXlaU Vpace. IQ VWXd\iQg Whe VXbOiPaWiRQ Rf QaShWhaOeQe iQWR aQ aiUVWUeaP, aQ iQYeVWigaWRU cRQVWUXcWed a 3-P-ORQg aQQXOaU dXcW. The iQQeU SiSe ZaV Pade fURP a 25-PP-OD, VROid QaShWhaOeQe URd; WhiV ZaV VXUURXQded b\ a 50-PP-ID QaShWhaOeQe SiSe. AiU aW 289 K aQd 1 aWP fORZed WhURXgh Whe aQQXOaU VSace aW aQ aYeUage YeORciW\ Rf 15 P/V. EVWiPaWe Whe SaUWiaO SUeVVXUe Rf QaShWhaOeQe iQ Whe aiUVWUeaP e[iWiQg fURP Whe WXbe. AW 289 K, QaShWhaOeQe haV a YaSRU SUeVVXUe Rf 5.2 Pa, aQd a diffXViYiW\ iQ aiU Rf 0.06 cP2/V. UVe Whe UeVXOWV Rf PURbOeP 2.7 WR eVWiPaWe Whe PaVV-WUaQVfeU cRefficieQW fRU Whe iQQeU VXUface; aQd eTXaWiRQ (2-47), XViQg Whe eTXiYaOeQW diaPeWeU defiQed iQ PURbOeP 2.7, WR eVWiPaWe Whe cRefficieQW fURP Whe RXWeU VXUface. SolXWion In WhiV ViWXaWion, WheUe Zill be a molaU flX[ fUom Whe inneU Zall, NA1, ZiWh Vpecific inWeUfacial aUea, a1, and a flX[ fUom Whe oXWeU Zall, NA2, ZiWh aUea a2. A maWeUial balance on a diffeUenWial YolXme elemenW \ieldV: Define: Then: FoU Whe inWeUioU Zall: For the outer Zall: 2.19c. Ben]ene evaporation on the outside surface of a single c\linder. BeQ]eQe iV eYaSRUaWiQg aW Whe UaWe Rf 20 Ng/hU RYeU Whe VXUface Rf a SRURXV 10-cP-diaPeWeU c\OiQdeU. DU\ aiU aW 325 K aQd 1 aWP fORZV aW UighW aQgOe WR Whe a[iV Rf Whe c\OiQdeU aW a YeORciW\ Rf 2 P/V. The OiTXid iV aW a WePSeUaWXUe Rf 315 K ZheUe iW e[eUWV a YaSRU SUeVVXUe Rf 26.7 NPa. EVWiPaWe Whe OeQgWh Rf Whe c\OiQdeU. FRU beQ]eQe, Tc = 562.2 K, Pc = 48.9 baU, M = 78, Vc = 259 cP 3/PRO, Zc = 0.271 (Reid, eW aO., 1987). SROXWiRQ CaOcXOaWe Whe aYeUage SURSeUWieV Rf Whe fiOP FURP Whe WiONe-Lee eTXaWiRQ FURP Whe LXcaV MeWhRd FURP ET. 2-45: 2.20b. MaVV WUanVfeU in a packed bed. Wilke and Hougan (TUanV. 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. In one run, the following data were reported: effective particle diameter 5.71 mm gas stream mass velocity 0.816 kg/m2-s temperature at the surface 311 K pressure 97.7 kPa kG 4.415 u 10 ç3 kmol/m2-s-atm With the assumption that the properties of the gas mixture are the same as those of air, calculate the gas-film mass-transfer coefficient using equation (2-55) and compare the result with the value reported by Wilke and Hougan. Solution From the Wilke-Lee equation 2.21b. MaVV WUanVfeU and pUeVVXUe dUop in a packed bed. Air at 373 K and 2 atm is passed through a bed 10-cm in diameter composed of iodine spheres 0.7-cm in diameter. The air flows at a rate of 2 m/s, based on the empt\ cross section of the bed. The porosit\ of the bed is 40%. a) How much iodine will evaporate from a bed 0.1 m long? The vapor pressure of iodine at 373 K is 6 kPa. Solution From the Wilke-Lee equation: b) EVWimaWe Whe pUeVVXUe dUop WhUoXgh Whe bed. SolXWion 2.22b. Volumetric mass-transfer coefficients in industrial toZers. 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 mass- transfer coefficient, kca. Empirical equations for the volumetric coefficients must be obtained experimentally for each type of mass-transfer operation. Sherwood and Holloway (Trans. 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. a) Consider the absorption of SO2 with water at 294 K in a tower packed with 25-mm Raschig rings. If the liquid mass velocity is L' = 2.04 kg/m2-s, estimate the liquid-film mass-transfer coefficient. The diffusivity of SO2 in water at 294 K is 1.7 u 10 ç9 m2/s. Solution For dimensional consistency, add the constants: b) Whitney and Vivian (Chem. Eng. Progr., 45, 323, 1949) measured rates of absorption of SO2 in water and found the following expression for 25-mm Raschig rings at 294 K where k[a is in kmole/m 2-s. For the conditions described in part a), estimate the liquid-film mass-transfer coefficient using equation (2-72). Compare the results. Solution 2.23b. Mass transfer in fluidi]ed beds. Cavatorta, et al. (AICKE J., 45, 938, 1999) studied the electrochemical reduction of ferrycianide ions, {Fe(CN)6} ç3, to ferrocyanide, {Fe(CN)6} ç4, in aqueous alkaline solutions. 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. The bed was packed with 0.534-mm spherical glass beads, with a particle density of 2.612 g/cm3. The properties of the aqueous solutions were: density = 1,083 kg/m3, viscosity = 1.30 cP, diffusivity = 5.90 u 10ç10 m2/s. They found that the porosity of the fluidized bed, e, could be correlated with the superficial liquid velocity based on the empty tube, vs, through where vs is in cm/s. a) Using equation (2-56), estimate the mass-transfer coefficient, kL, if the porosity of the bed is 60%. Solution b) CaYaWoUWa eW al. pUopoVed Whe folloZing coUUelaWion Wo eVWimaWe Whe maVV-WUanVfeU coefficienW foU WheiU flXidi]ed bed e[peUimenWal UXnV: ZheUe Re iV baVed on Whe empW\ WXbe YelociW\. UVing WhiV coUUelaWion, eVWimaWe Whe maVV-WUanVfeU coefficienW, NL, if Whe poUoViW\ of Whe bed iV 60%. CompaUe \oXU UeVXlW Wo WhaW of paUW a). SolXWion 2.24b. Mass transfer in a holloZ-fiber boiler feedZater deaerator. ConVideU Whe holloZ-fibeU BFW deaeUaWoU deVcUibed in E[ample 2-13. If Whe ZaWeU floZ UaWe incUeaVeV Wo 60,000 kg/hU Zhile eYeU\Whing elVe UemainV conVWanW, calcXlaWe Whe fUacWion of Whe enWeUing diVVolYed o[\gen WhaW can be UemoYed. SolXWion 2.25b. Mass transfer in a holloZ-fiber boiler feedZater deaerator. a) ConVideU Whe holloZ-fibeU BFW deaeUaWoU deVcUibed in E[ample 2-13. AVVXming WhaW onl\ o[\gen diffXVeV acUoVV Whe membUane, calcXlaWe Whe gaV YolXme floZ UaWe and compoViWion aW Whe lXmen oXWleW. The ZaWeU enWeUV Whe Vhell Vide aW 298 K VaWXUaWed ZiWh aWmoVpheUic o[\gen, Zhich meanV a diVVolYed o[\gen concenWUaWion of 8.38 mg/L. SolXWion b) CaOcXOaWe Whe PaVV-WUaQVfeU cRefficieQW aW Whe aYeUage cRQdiWiRQV iQVide Whe OXPeQ. NegOecW Whe WhicNQeVV Rf Whe fibeU ZaOOV ZheQ eVWiPaWiQg Whe gaV YeORciW\ iQVide Whe OXPeQ. SROXWiRQ CaOcXOaWe Whe aYeUage fORZ cRQdiWiRQV iQVide Whe fibeUV CaOcXOaWe Whe aYeUage R[\geQ PROaU fUacWiRQ iQ Whe gaV FURP LXcaV PeWhRd fRU SXUe N2 FURP Whe WiONe-Lee eTXaWiRQ (From E[ample 2.13) 3.1a. Application of Raoult's law to a binar\ s\stem. ReSeaWE[aPSOe 3.1, bXW fRU a OiTXid cRQceQWUaWiRQ Rf 0.6 PROe fUacWiRQ Rf beQ]eQe aQd a WePSeUaWXUe Rf 320 K. SROXWiRQ 3.2b. Application of Raoult's law to a binar\ s\stem. a) DeWeUPiQe Whe cRPSRViWiRQ Rf Whe OiTXid iQ eTXiOibUiXP ZiWh a YaSRU cRQWaiQiQg 60 PROe SeUceQW beQ]eQe-40 PROe SeUceQW WROXeQe if Whe V\VWeP e[iVWV iQ a YeVVeO XQdeU 1 aWP SUeVVXUe. PUedicW Whe eTXiOibUiXP WePSeUaWXUe. SROXWiRQ IQiWiaO eVWiPaWeV b) DeWeUPiQe Whe cRPSRViWiRQ Rf Whe YaSRU iQ eTXiOibUiXP ZiWh a OiTXid cRQWaiQiQg 60 PROe SeUceQW beQ]eQe-40 PROe SeUceQW WROXeQe if Whe V\VWeP e[iVWV iQ a YeVVeO XQdeU 1 aWP SUeVVXUe. PUedicW Whe eTXiOibUiXP WePSeUaWXUe. SROXWiRQ 3.3a. Application of Raoult's laZ to a binar\ s\stem. NRUPaO heSWaQe, Q-C7H16, aQd QRUPaO RcWaQe, Q-C8H18, fRUP ideaO VROXWiRQV. AW 373 K, QRUPaO heSWaQe haV a YaSRU SUeVVXUe Rf 106 NPa aQd QRUPaO RcWaQe Rf 47.1 NPa. a) WhaW ZRXOd be Whe cRPSRViWiRQ Rf a heSWaQe-RcWaQe VROXWiRQ WhaW bRiOV aW 373 K XQdeU a 93 NPa SUeVVXUe? SROXWiRQ b) WhaW ZRXOd be Whe cRPSRViWiRQ Rf Whe YaSRU iQ eTXiOibUiXP ZiWh Whe VROXWiRQ WhaW iV deVcUibed iQ (a)? SROXWiRQ 3.4a. Henr\'s laZ: saturation of Zater Zith o[\gen. A VROXWiRQ ZiWh R[\geQ diVVROYed iQ ZaWeU cRQWaiQiQg 0.5 Pg O2/100 g Rf H2O iV bURXghW iQ cRQWacW ZiWh a OaUge YROXPe Rf aWPRVSheUic aiU aW 283 K aQd a WRWaO SUeVVXUe Rf 1 aWP. The HeQU\'V OaZ cRQVWaQW fRU Whe R[\geQ-ZaWeU V\VWeP aW 283 K eTXaOV 3.27 u 104 aWP/PROe fUacWiRQ. a) WiOO Whe VROXWiRQ gaiQ RU ORVe R[\geQ? b) WhaW ZiOO be Whe cRQceQWUaWiRQ Rf R[\geQ iQ Whe fiQaO eTXiOibUiXP VROXWiRQ? SROXWiRQ AW eTXiOibUiXP: BaViV: 1 L ZaWeU (1 Ng ZaWeU) ETXiOibUiXP cRQceQWUaWiRQ, ce = 11.42 Pg R[\geQ/L IQiWiaO cRQdiWiRQV: The VROXWiRQ gaiQV R[\geQ. 3.5c. Material balances combined Zith equilibrium relations. ReSeaW E[aPSOe 3.3, bXW aVVXPiQg WhaW Whe aPPRQia, aiU, aQd ZaWeU aUe bURXghW iQWR cRQWacW iQ a cORVed cRQWaiQeU. TheUe iV 10 P3 Rf gaV VSace RYeU Whe OiTXid. AVVXPiQg WhaW Whe gaV-VSace YROXPe aQd Whe WePSeUaWXUe UePaiQ cRQVWaQW XQWiO eTXiOibUiXP iV achieYed, PRdif\ Whe MaWhcad SURgUaP iQ FigXUe 3.2 WR caOcXOaWe: a) Whe WRWaO SUeVVXUe aW eTXiOibUiXP SROXWiRQ IQiWiaO gXeVVeV AQVZHU: P = 1.755 DWP E) WKH HTXLOLEULXP DPPRQLD FRQFHQWUDWLRQ LQ WKH JDV DQG OLTXLG SKDVHV. AQVZHU: \A = 0.145; [A= 0.162 3.6b. MaVV-WUanVfeU UeViVWanceV dXUing abVoUpWion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b) the liquid-film coefficient, kL; Solution Basis: 1 m3 of aqueous solution c) the concentration on the liquid side of the interface, [A,i; Solution Initial estimates of interfacial concentrations: d) the mass flu[ of A. Solution Check this result b\ calculating the gas-phase flu[: 3.7b. Mass-transfer resistances during absorption. FRU a V\VWeP iQ Zhich cRPSRQeQW A iV WUaQVfeUUiQg fURP Whe gaV ShaVe WR Whe OiTXid ShaVe, Whe eTXiOibUiXP UeOaWiRQ iV giYeQ b\ ZheUe SA,i iV Whe eTXiOibUiXP SaUWiaO SUeVVXUe iQ aWP aQd [A,i iV Whe eTXiOibUiXP OiTXid cRQceQWUaWiRQ iQ PROaU fUacWiRQ. AW RQe SRiQW iQ Whe aSSaUaWXV, Whe OiTXid VWUeaP cRQWaiQV 4.5 PROe % aQd Whe gaV VWUeaP cRQWaiQV 9.0 PROe % A. The WRWaO SUeVVXUe iV 1 aWP. The iQdiYidXaO gaV-fiOP cRefficieQW aW WhiV SRiQW iV NG = 3.0 PROe/P 2-V-aWP. FifW\ SeU ceQW Rf Whe RYeUaOO UeViVWaQce WR PaVV WUaQVfeU iV NQRZQ WR be eQcRXQWeUed iQ Whe OiTXid ShaVe. EYaOXaWe a) Whe RYeUaOO PaVV-WUaQVfeU cRefficieQW, K\; SROXWiRQ b) Whe PROaU fOX[ Rf A; SROXWiRQ (\Ae = \A*) c) The OiTXid iQWeUfaciaO cRQceQWUaWiRQ Rf A. SROXWiRQ 3.8d. Absorption of ammonia b\ water: use of F-t\pe mass-transfer coefficients. MRdif\ Whe MaWhcad SURgUaP iQ FigXUe 3.6 WR UeSeaW E[aPSOe 3.5, bXW ZiWh \A,G = 0.70 aQd [A,L = 0.10. EYeU\WhiQg eOVe UePaiQV cRQVWaQW. SolXWion IniWial gXeVVeV 3.9d. Absorption of ammonia b\ water: use of F-t\pe mass-transfer coefficients. Modif\ Whe MaWhcad pUogUam in FigXUe 3.6 Wo UepeaW E[ample 3.5, bXW ZiWh FL = 0.0050 kmol/m 2-V. EYeU\Whing elVe UemainV conVWanW. SolXWion IniWial gXeVVeV 3.10b. MaVV-WUanVfeU UeViVWanceV dXUing abVoUpWion of ammonia. IQ Whe abVRUSWiRQ Rf aPPRQia iQWR ZaWeU fURP aQ aiU-aPPRQia Pi[WXUe a 300 K aQd 1 aWP, Whe iQdiYidXaO fiOP cRefficieQWV ZeUe eVWiPaWed WR be NL = 6.3 cP/hU aQd NG = 1.17 NPRO/P 2-hU-aWP. The eTXiOibUiXP UeOaWiRQVhiS fRU YeU\ diOXWe VROXWiRQV Rf aPPRQia iQ ZaWeU aW 300 K aQd 1 aWP iV DeWeUPiQe Whe fROORZiQg PaVV-WUaQVfeU cRefficieQWV: a) N\ SROXWiRQ b) N[ SROXWiRQ c) Ky Solution d) Fraction of the total resistance to mass transfer that resides in the gas phase. Solution 3.11b. Mass-transfer resistances in holloZ-fiber membrane contactors. 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, AICKE J., 32, 1910, Nov. 1986) where kL, kM, and kc 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. The mass-transfer coefficient across a hydrophobic membrane is from (Prasad and Sirkar, AICKE J., 34, 177, Feb. 1988) where DAB = molecular diffusion coefficient in the gas filling the pores, eM = membrane porosity, tM = membrane tortuosity, d = membrane thickness. For the membrane modules of Example 2.13, eM = 0.4,tM = 2.2, and d = 25 u 10 ç6 m (Prasad and Sirkar, 1988). a) Calculate the corresponding value of kM. Solution For oxygen in nitrogen at 298 K and 1 atm: b) UViQg Whe UeVXOWV Rf SaUW (a), E[aPSOe 2.13, aQd PURbOeP 2.25, caOcXOaWe KL, aQd eVWiPaWe ZhaW fUacWiRQ Rf Whe WRWaO UeViVWaQce WR PaVV WUaQVfeU UeVideV iQ Whe OiTXid fiOP. SROXWiRQ FURP E[aPSOe 2.13: FURP PURb. 2.25: ViUWXaOO\ aOO Rf Whe UeViVWaQce UeVideV iQ Whe OiTXid ShaVe. 3.12c. Combined use of F- and k-t\pe coefficients: absorption of low-solubilit\ gases. DXUiQg abVRUSWiRQ Rf ORZ-VROXbiOiW\ gaVeV, PaVV WUaQVfeU fURP a highO\ cRQceQWUaWed gaV Pi[WXUe WR a YeU\ diOXWe OiTXid VROXWiRQ fUeTXeQWO\ WaNeV SOace. IQ WhaW caVe, aOWhRXgh iW iV aSSURSUiaWe WR XVe a N-W\Se PaVV-WUaQVfeU cRefficieQW iQ Whe OiTXid ShaVe, aQ F-W\Se cRefficieQW PXVW be XVed iQ Whe gaV ShaVe. SiQce diOXWe OiTXid VROXWiRQV XVXaOO\ Rbe\ HeQU\'V OaZ, Whe iQWeUfaciaO cRQceQWUaWiRQV dXUiQg abVRUSWiRQ Rf ORZ-VROXbiOiW\ gaVeV aUe UeOaWed WhURXgh \A,i = P[A,i. a) ShRZ WhaW, XQdeU Whe cRQdiWiRQV deVcUibed abRYe, Whe gaV iQWeUfaciaO cRQceQWUaWiRQ VaWiVfieV Whe eTXaWiRQ SROXWiRQ IQ Whe gaV ShaVe: IQ Whe OiTXid ShaVe: FRU HeQU\'V LaZ: TheQ: ReaUUaQgiQg: b) IQ a ceUWaiQ aSSaUaWXV XVed fRU Whe abVRUSWiRQ Rf SO2 fURP aiU b\ PeaQV Rf ZaWeU, aW RQe SRiQW iQ Whe eTXiSPeQW Whe gaV cRQWaiQed 30% SO2 b\ YROXPe aQd ZaV iQ cRQWacW ZiWh a OiTXid cRQWaiQiQg 0.2% SO2 b\ PROe. The WePSeUaWXUe ZaV 303 K aQd Whe WRWaO SUeVVXUe 1 aWP. EVWiPaWe Whe iQWeUfaciaO cRQceQWUaWiRQV aQd Whe ORcaO SO2 PROaU fOX[. The PaVV-WUaQVfeU cRefficieQWV ZeUe caOcXOaWed aV FG = 0.002 NPRO/P 2-V, N[ = 0.160 NPRO/P 2-V. The eTXiOibUiXP SO2 VROXbiOiW\ daWa aW 303 K aUe (PeUU\ aQd ChiOWRQ, 1973): Ng SO2/100 Ng ZaWeU PaUWiaO SUeVVXUe Rf SO2, PP Hg (WRUU) 0.0 0 0.5 42 1.0 85 1.5 129 2.0176 2.5 224 SROXWiRQ DefiQe: Z = Ng SO2/100 Ng ZaWeU S = PaUWiaO SUeVVXUe Rf SO2, PP Hg (WRUU) IniWial gXeVV: 3.13d. Distillation of a mi[ture of methanol and Zater in a packed toZer: 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 temperature at that point in the tower is around 343 K. The packing characteristics and flow rates at that point are such that FG = 1.542 u 10 ç3 kmol/m2-s, and FL = 8.650 u 10 ç3 kmol/m2-s. Calculate the interfacial compositions and the local methanol flux. To calculate the latent heats of vaporization at the new temperature, modify the values given in Example 3.6 using Watson's method (Smith, et al., 1996): For water, Tc = 647.1 K; for methanol, Tc = 512.6 K Solution For methanol (A) For water (B) PaUameWeUV IniWial eVWimaWeV 3.14b. Material balances: adsorption of ben]ene vapor on activated carbon. AcWiYaWed caUbRQ iV XVed WR UecRYeU beQ]eQe fURP a QiWURgeQ-beQ]eQe YaSRU Pi[WXUe. A QiWURgeQ- beQ]eQe Pi[WXUe aW 306 K aQd 1 aWP cRQWaiQiQg 1% beQ]eQe b\ YROXPe iV WR be SaVVed cRXQWeUcXUUeQWO\ aW Whe UaWe Rf 1.0 P3/V WR a PRYiQg VWUeaP Rf acWiYaWed caUbRQ VR aV WR UePRYe 85% Rf Whe beQ]eQe fURP Whe gaV iQ a cRQWiQXRXV SURceVV. The eQWeUiQg acWiYaWed caUbRQ cRQWaiQV 15 cP3 beQ]eQe YaSRU (aW STP) adVRUbed SeU gUaP Rf Whe caUbRQ. The WePSeUaWXUe aQd WRWaO SUeVVXUe aUe PaiQWaiQed aW 306 K aQd 1 aWP. NiWURgeQ iV QRW adVRUbed. The eTXiOibUiXP adVRUSWiRQ Rf beQ]eQe RQ WhiV acWiYaWed caUbRQ aW 306 K iV UeSRUWed aV fROORZV: BeQ]eQe YaSRU adVRUbed PaUWiaO SUeVVXUe beQ]eQe, PP Hg cP3 (STP)/g caUbRQ 15 0.55 25 0.95 40 1.63 50 2.18 65 3.26 80 4.88 90 6.22 100 7.83 a) PORW Whe eTXiOibUiXP daWa aV X' = Ng beQ]eQe/Ng dU\ caUbRQ, Y' = Ng beQ]eQe/Ng QiWURgeQ fRU a WRWaO SUeVVXUe Rf 1 aWP. SROXWiRQ b) CaOcXOaWe Whe PiQiPXP fORZ UaWe UeTXiUed Rf Whe eQWeUiQg acWiYaWed caUbRQ (UePePbeU WhaW Whe eQWeUiQg caUbRQ cRQWaiQV VRPe adVRUbed beQ]eQe). SROXWiRQ OQ Whe XY diagUaP, ORcaWe Whe SRiQW (X2,Y2). SiQce Whe RSeUaWiQg OiQe iV abRYe Whe eTXiOibUiXP cXUYe aQd Whe eTXiOibUiXP cXUYe iV cRQcaYe XSZaUdV, Whe PiQiPXP RSeUaWiQg OiQe iV RbWaiQed b\ ORcaWiQg, aW Whe iQWeUVecWiRQ Rf Y = Y1 ZiWh Whe eTXiOibUiXP cXUYe, X1Pa[. c) If the carbon flow rate is 20% above the minimum, what will be the concentration of ben]ene adsorbed on the carbon leaving? Solution d) FRU Whe cRQdiWiRQV Rf SaUW (c), caOcXOaWe Whe QXPbeU Rf ideaO VWageV UeTXiUed. SROXWiRQ See VWeSZiVe cRQVWUXcWiRQ RQ Whe XY gUaSh 3.15b. Material balances: desorption of ben]ene vapor from activated carbon. The acWiYaWed caUbRQ OeaYiQg Whe adVRUbeU Rf PURbOeP 3.14 iV UegeQeUaWed b\ cRXQWeUcXUUeQW cRQWacW ZiWh VWeaP aW 380 K aQd 1 aWP. The UegeQeUaWed caUbRQ iV UeWXUQed WR Whe adVRUbeU, ZhiOe Whe Pi[WXUe Rf VWeaP aQd deVRUbed beQ]eQe YaSRUV iV cRQdeQVed. The cRQdeQVaWe VeSaUaWeV iQWR aQ RUgaQic aQd aQ aTXeRXV ShaVe aQd Whe WZR ShaVeV aUe VeSaUaWed b\ decaQWaWiRQ. DXe WR Whe ORZ VROXbiOiW\ Rf beQ]eQe iQ ZaWeU, PRVW Rf Whe beQ]eQe ZiOO be cRQceQWUaWed iQ Whe RUgaQic ShaVe, ZhiOe Whe aTXeRXV ShaVe ZiOO cRQWaiQ RQO\ WUaceV Rf beQ]eQe. The eTXiOibUiXP adVRUSWiRQ daWa aW 380 K aUe aV fROORZV: BeQ]eQe YaSRU adVRUbed PaUWiaO SUeVVXUe beQ]eQe, NPa Ng beQ]eQe/100 Ng caUbRQ 2.9 1.0 5.5 2.0 12.0 5.0 17.1 8.0 20.0 10.0 25.7 15.0 30.0 20.0 a) CaOcXOaWe Whe PiQiPXP VWeaP fORZ UaWe UeTXiUed. SROXWiRQ ETXiOibUiXP cXUYe 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. IW iV deViUed WR dU\ 10 Ng Rf VRaS fURP 20% PRiVWXUe b\ ZeighW WR QR PRUe WhaQ 6% PRiVWXUe b\ cRQWacW ZiWh hRW aiU. The ZeW VRaS iV SOaced iQ a YeVVeO cRQWaiQiQg 8.06 P3 Rf aiU aW 350 K, 1 aWP, aQd a ZaWeU-YaSRU SaUWiaO SUeVVXUe Rf 1.6 NPa. The V\VWeP iV aOORZed WR Ueach eTXiOibUiXP, aQd WheQ Whe aiU iQ Whe YeVVeO iV eQWiUeO\ UeSOaced b\ fUeVh aiU Rf Whe RUigiQaO PRiVWXUe cRQWeQW aQd WePSeUaWXUe. HRZ PaQ\ WiPeV PXVW Whe SURceVV be UeSeaWed iQ RUdeU WR Ueach Whe VSecified VRaS PRiVWXUe cRQWeQW Rf QR PRUe WhaQ 6%? WheQ WhiV VRaS iV e[SRVed WR aiU aW 350 K aQd 1 aWP, Whe eTXiOibUiXP diVWUibXWiRQ Rf PRiVWXUe beWZeeQ Whe aiU aQd Whe VRaS iV aV fROORZV: WW % PRiVWXUe iQ VRaS PaUWiaO SUeVVXUe Rf ZaWeU, NPa 2.40 1.29 3.76 2.56 4.76 3.79 6.10 4.96 7.83 6.19 9.90 7.33 12.63 8.42 15.40 9.58 19.02 10.60 SROXWiRQ GeQeUaWe Whe XY diagUaP From the XY diagram, at the e[it of the fifth equilibrium stage, X = 0.06 and 3.18b. Material balances in batch processes: e[traction of an aqueous nicotine solution Zith kerosene. Nicotine in a Zater solution containing 2% nicotine is to be e[tracted Zith 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 equilibrium data are as folloZs (Claffe\ et al., IQd. EQg. CheP., 42, 166, 1950): X', u 103 kg nicotine/kg Zater Y', u 103 kg nicotine/kg kerosene 1.01 0.81 2.46 1.96 5.02 4.56 7.51 6.86 9.98 9.13 20.4 18.70 Solution From the XY diagram, after 4 e[tractions, X = 0.00422 3.19b. Cross-floZ cascade of ideal stages. The dU\iQg aQd OiTXid-OiTXid e[WUacWiRQ RSeUaWiRQV deVcUibed iQ PURbOePV 3.17 aQd 3.18, UeVSecWiYeO\, aUe e[aPSOeV Rf a fORZ cRQfigXUaWiRQ caOOed a cURVV-fORZ caVcade. FigXUe 3.27 iV a VchePaWic diagUaP Rf a cURVV-fORZ caVcade Rf ideaO VWageV. Each VWage iV UeSUeVeQWed b\ a ciUcOe, aQd ZiWhiQ each VWage PaVV WUaQVfeU RccXUV aV if iQ cRcXUUeQW fORZ. The L ShaVe fORZV fURP RQe VWage WR Whe Qe[W, beiQg cRQWacWed iQ each VWage b\ a fUeVh V ShaVe. If Whe eTXiOibUiXP-diVWUibXWiRQ cXUYe Rf Whe cURVV-fORZ caVcade iV eYeU\ZheUe VWUaighW aQd Rf VORSe P, iW caQ be VhRZQ WhaW (TUe\baO, 1980) ZheUe S iV Whe VWUiSSiQg facWRU, PVS/LS, cRQVWaQW fRU aOO VWageV, aQd N iV Whe WRWaO QXPbeU Rf VWageV. SROYe PURbOeP 3.18 XViQg eTXaWiRQ (3-60), aQd cRPSaUe Whe UeVXOWV RbWaiQed b\ Whe WZR PeWhRdV. SROXWiRQ IQiWiaO eVWiPaWe 3.20a. Cross-floZ cascade of ideal stages: nicotine e[traction. CRQVideU Whe QicRWiQe e[WUacWiRQ Rf PURbOePV 3.18 aQd 3.19. CaOcXOaWe Whe QXPbeU Rf ideaO VWageV UeTXiUed WR achieYe aW OeaVW 95% e[WUacWiRQ efficieQc\. SROXWiRQ UVe 8 ideaO VWageV 3.21b. Kremser equations: absorption of h\drogen sulfide. A VchePe fRU Whe UePRYaO Rf H2S fURP a fORZ Rf 1.0 VWd P 3/V Rf QaWXUaO gaV b\ VcUXbbiQg ZiWh ZaWeU aW 298 K aQd 10 aWP iV beiQg cRQVideUed. The iQiWiaO cRPSRViWiRQ Rf Whe feed gaV iV 2.5 PROe SeUceQW H2S. A fiQaO gaV VWUeaP cRQWaiQiQg RQO\ 0.1 PROe SeUceQW H2S iV deViUed. The abVRUbiQg ZaWeU ZiOO eQWeU Whe V\VWeP fUee Rf H2S. AW Whe giYeQ WePSeUaWXUe aQd SUeVVXUe, Whe V\VWeP ZiOO fROORZ HeQU\'V OaZ, accRUdiQg WR Yi = 48.3Xi, ZheUe Xi = PROeV H2S/PROe Rf ZaWeU; Yi = PROeV H2S/PROe Rf aiU. a) FRU a cRXQWeUcXUUeQW abVRUbeU, deWeUPiQe Whe fORZ UaWe Rf ZaWeU WhaW iV UeTXiUed if 1.5 WiPeV Whe minimum floZ rate is used. 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 Zith chemical reaction: H2S scrubbing ZithMEA. AV VhRZQ iQ PURbOeP 3-21, VcUXbbiQg Rf h\dURgeQ VXOfide fURP QaWXUaO gaV XViQg ZaWeU iV QRW SUacWicaO ViQce iW UeTXiUeV OaUge aPRXQWV Rf ZaWeU dXe WR Whe ORZ VROXbiOiW\ Rf H2S iQ ZaWeU. If a 2N VROXWiRQ Rf PRQReWhaQROaPiQe (MEA) iQ ZaWeU iV XVed aV Whe abVRUbeQW, hRZeYeU, Whe UeTXiUed OiTXid fORZ UaWe iV UedXced dUaPaWicaOO\ becaXVe Whe MEA UeacWV ZiWh Whe abVRUbed H2S iQ Whe OiTXid ShaVe, effecWiYeO\ iQcUeaViQg iWV VROXbiOiW\. FRU WhiV VROXWiRQ VWUeQgWh aQd a WePSeUaWXUe Rf 298 K, Whe VROXbiOiW\ Rf H2S caQ be aSSUR[iPaWed b\ (de NeYeUV, N., Air PollXWion ConWrol Engineering, 2Qd ed., McGUaZ-HiOO, BRVWRQ, MA, 2000): ReSeaW Whe caOcXOaWiRQV Rf PURbOeP 3.21, bXW XViQg a 2N PRQReWhaQROaPiQe VROXWiRQ aV abVRUbeQW. SROXWiRQ 3.23b. Kremser equations: absorption of sulfur dio[ide. A flue gas flows at the rate of 10 kmol/s at 298 K and 1 atm with a SO2 content of 0.15 mole %. Ninety percent of the sulfur dioxide is to be removed by absorption with pure water at 298 K. The design water flow rate will be 50% higher than the minimum. Under these conditions, the equilibrium line is (Ben¶tez, J., PUoceVV EngineeUing and DeVign foU AiU PollXWion ConWUol, Prentice Hall, Englewood Cliffs, NJ, 1993): where Xi = moles SO2/mole of water; Yi = moles SO2/mole of air. a) Calculate the water flow rate and the SO2 concentration in the water leaving the absorber. 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 abVoUbeU iV aYailable Wo WUeaW Whe flXe gaV of PUoblem 3.23 Zhich iV eTXiYalenW Wo 8.5 eTXilibUiXm VWageV. a) CalcXlaWe Whe ZaWeU floZ UaWe Wo be XVed in WhiV abVoUbeU if 90% of Whe SO2 iV Wo be UemoYed. CalcXlaWe alVo Whe SO2 concenWUaWion in Whe ZaWeU leaYing Whe abVoUbeU. SolXWion IniWial eVWimaWe b) WhaW iV Whe SeUceQWage UePRYaO Rf SO2 WhaW caQ be achieYed ZiWh WhiV abVRUbeU if Whe ZaWeU fORZ UaWe XVed iV Whe VaPe WhaW ZaV caOcXOaWed iQ PURbOeP 3.23 (a)? SROXWiRQ IQiWiaO eVWiPaWe 3.25b. Kremser equations: liquid e[traction. AQ aTXeRXV aceWic acid VROXWiRQ fORZV aW Whe UaWe Rf 1,000 Ng/hU. The VROXWiRQ iV 1.1% (b\ ZeighW) aceWic acid. IW iV deViUed WR UedXce Whe cRQceQWUaWiRQ Rf WhiV VROXWiRQ WR 0.037% (b\ ZeighW) aceWic acid b\ e[WUacWiRQ ZiWh 3-heSWaQRO aW 298 K. The iQOeW 3-heSWaQRO cRQWaiQV 0.02% (b\ ZeighW) aceWic acid. AQ e[WUacWiRQ cROXPQ iV aYaiOabOe Zhich iV eTXiYaOeQW WR a cRXQWeUcXUUeQW caVcade Rf 15 eTXiOibUiXP VWageV. WhaW VROYeQW fORZ UaWe iV UeTXiUed? CaOcXOaWe Whe cRPSRViWiRQ Rf Whe VROYeQW ShaVe OeaYiQg Whe cROXPQ. FRU WhiV V\VWeP, eTXiOibUiXP iV giYeQ b\ WW UaWiR aceWic acid iQ VROYeQW = 0.828 u WW UaWiR aceWic acid iQ ZaWeU SROXWiRQ LeW Whe aTXeRXV ShaVe be Whe V-ShaVe; Whe VROYeQW ShaVe iV Whe L-ShaVe. Initial estimate: 3.26c. CoXnWeUcXUUenW YeUVXV cUoVV-floZ e[WUacWion. A 1-butanol acid solution is to be e[tracted Zith pure Zater. The butanol solution contains 4.5% (b\ Zeight) of acetic acid and floZs at the rate of 400 kg/hr. A total Zater floZ rate of 1005 kg/hr is used. Operation is at 298 K and 1 atm. For practical purposes, 1-butanol and Zater are inmiscible. At 298 K, the equilibrium data can be represented b\ YAi = 0.62 XAi, Zhere YAi is the Zeight ratio of acid in the aqueous phase and XAi is the Zeight ratio of acid in the organic phase. a) If the outlet butanol stream is to contain 0.10% (b\ Zeight) acid, hoZ man\ equilibrium stages are required for a countercurrent cascade? Solution b) If Whe ZaWeU iV VSOiW XS eTXaOO\ aPRQg Whe VaPe QXPbeU Rf VWageV, bXW iQ a cURVV-fORZ caVcade, ZhaW iV Whe RXWOeW 1-bXWaQRO cRQceQWUaWiRQ (Vee PURbOeP 3.19)? SROXWiRQ 3.27c. Glucose sorption on an ion e[change resin. ChiQg aQd RXWhYeQ (AIChE S\mp. Ser., 81,S. 242, 1985) fRXQd WhaW Whe eTXiOibUiXP Rf gOXcRVe RQ aQ iRQ e[chaQge UeViQ iQ Whe caOciXP fRUP ZaV OiQeaU fRU cRQceQWUaWiRQV beORZ 50 g/L. TheiU eTXiOibUiXP e[SUeVViRQ aW 303 K iV YAi = 1.961 XAi, ZheUe XAi iV Whe gOXcRVe cRQceQWUaWiRQ iQ Whe UeViQ.(g Rf gOXcRVe SeU OiWeU Rf UeViQ) aQd YAi iV Whe gOXcRVe cRQceQWUaWiRQ iQ VROXWiRQ.(g Rf gOXcRVe SeU OiWeU Rf VROXWiRQ). a) We ZiVh WR VRUb gOXcRVe RQWR WhiV iRQ e[chaQge UeViQ aW 303 K iQ a cRXQWeUcXUUeQW caVcade Rf ideaO VWageV. The cRQceQWUaWiRQ Rf Whe feed VROXWiRQ iV 15 g/L. We ZaQW aQ RXWOeW cRQceQWUaWiRQ Rf 1.0 g/L. The iQOeW UeViQ cRQWaiQV 0.25 g Rf gOXcRVe/L. The feed VROXWiRQ fORZV aW Whe UaWe Rf 100 L/PiQ, ZhiOe Whe UeViQ fORZV aW Whe UaWe Rf 250 L/PiQ. FiQd Whe QXPbeU Rf eTXiOibUiXP VWageV UeTXiUed. SROXWiRQ b) If 5 equilibrium stages are added to the cascade of part a), calculate the resin floZ required to maintain the same degree of glucose sorption. Solution 4.1a. Void fraction near the Zalls of packed beds. CRQVideU a c\OiQdUicaO YeVVeO ZiWh a diaPeWeU Rf 305 PP SacNed ZiWh VROid VSheUeV ZiWh a diaPeWeU Rf 50 PP. a) FURP eTXaWiRQ (4-1), caOcXOaWe Whe aV\PSWRWic SRURViW\ Rf Whe bed. SROXWiRQ AQVZeU b) EVWiPaWe Whe YRid fUacWiRQ aW a diVWaQce Rf 100 PP fURP Whe ZaOO. AQVZeU 4.2b. Void fraction near the Zalls of packed beds. BecaXVe Rf Whe RVciOOaWRU\ QaWXUe Rf Whe YRid-fUacWiRQ UadiaO YaUiaWiRQ Rf SacNed bedV, WheUe aUe a QXPbeU Rf ORcaWiRQV cORVe WR Whe ZaOO ZheUe Whe ORcaO YRid fUacWiRQ iV e[acWO\ eTXaO WR Whe aV\PSWRWic YaOXe fRU Whe bed. FRU Whe bed deVcUibed iQ E[aPSOe 4.1, caOcXOaWe Whe diVWaQce fURP Whe ZaOO WR Whe fiUVW fiYe VXch ORcaWiRQV. SROXWiRQ The ORcaO SRURViW\ QeaU Whe ZaOO eTXaOV Whe aV\PSWRWic SRURViW\ ZheQ J0(DUd) = 0. FURP E[aPSOe 4.1, IQiWiaO eVWiPaWeV Rf Whe URRWV caQ be RbWaiQed fURP Fig. 4.4 IQiWiaO eVWiPaWe IQiWiaO eVWiPaWe IQiWiaO eVWiPaWe IQiWiaO eVWiPaWe IQiWiaO eVWiPaWe 4.3c. Void fraction near the Zalls of packed beds. (a) ShRZ WhaW Whe UadiaO ORcaWiRQ Rf Whe Pa[iPa aQd PiQiPa Rf Whe fXQcWiRQ deVcUibed b\ ETXaWiRQ (4-1) aUe Whe URRWV Rf Whe eTXaWiRQ SROXWiRQ b) FRU Whe SacNed bed Rf E[aPSOe 4.1, caOcXOaWe Whe UadiaO ORcaWiRQ Rf Whe fiUVW fiYe Pa[iPa, aQd Rf Whe fiUVW fiYe PiQiPa; caOcXOaWe Whe aPSOiWXde Rf Whe YRid fUacWiRQ RVciOaWiRQV aW WhRVe SRiQWV. SROXWiRQ IniWial eVWimaWeV of Whe UooWV can be obWained fUom Fig. 4.4 IniWial eVWimaWe IniWial eVWimaWe RepeaWing WhiV pUocedXUe, Whe folloZing UeVXlWV aUe obWained: Ma[ima: Minima U, mm (U*) AmpliWXde, % U,mm (U*) AmpliWXde, % 20.8 (1.04) 37.2 11.3 (0.57) -56.7 39.6 (1.98) 21.1 30.2 (1.51) -27.3 58.3 (2.92) 13.5 49.0 (2.45) -16.7 77.1 (3.85) 9.2 67.7 (3.39) -11.1 95.8 (4.79) 6.4 86.4 (4.32) -7.6 c) CalcXlaWe Whe diVWance fUom Whe Zall aW Zhich Whe abVolXWe YalXe of Whe poUoViW\ flXcWXaWionV haV been dampened Wo leVV Whan 10% of Whe aV\mpWoWic bed poUoViW\. SolXWion FUom Whe UeVXlWV of paUW (b), WhiV mXVW happen aW U* beWZeen 3.39 and 3.85 (d) What fraction of the cross-sectional area of the packed bed is characterized by porosity fluctuations which are within 10% of the asymptotic bed porosity? Solution From part (c) (f) For the packed bed of Example 4.1, estimate the average void fraction by numerical integration of equation (4-65) and estimate the ratio HaY/Hb. Solution 4.4c. Void fraction near the Zalls of annular packed beds. 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. A correlation for this purpose was recently formulated (Mueller, G. E., AIChE J., 45, 2458-60, Nov. 1999). The correlation is restricted to randomly packed beds in annular cylindrical containers of outside diameterDo, inside diameter Di, equivalent diameter De = Do ç Di, consisting of equal-sized spheres of diameter dp, with diameter aspect ratios of 4 ð De/dp ð 20. 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. Solution (b) Plot the void fraction, as predicted by Eq. (4-66), for r* from 0 to R*. (c) ShoZ WhaW Whe aYeUage poUoViW\ foU an APB iV giYen b\ (d) EVWimaWe Whe aYeUage poUoViW\ foU Whe APB deVcUibed aboYe. SolXWion 4.5a. Minimum liquid mass velocit\ for proper wetting of packing. A 1.0-m diameWeU bed XVed foU abVoUpWion of ammonia ZiWh pXUe ZaWeU aW 298 K iV packed ZiWh 25-mm plaVWic InWalo[ VaddleV. CalcXlaWe Whe minimXm ZaWeU floZ UaWe, in kg/V, neded Wo enVXUe pUopeU ZeWWing of Whe packing VXUface. SolXWion FoU plaVWic packing, YL,min = 1.2 mm/V. FUom SWeam TableV 4.6a. Minimum liquid mass velocit\ for proper wetting of packing. RepeaW PUoblem 4.5, bXW XVing ceUamic inVWead of plaVWic InWalo[ VaddleV. SolXWion FoU ceUamic packing, YL,min = 0.15 mm/V. From Steam Tables 4.7b. SSecific OiTXid hROdXS aQd YRid fUacWiRQ iQ fiUVW-geQeUaWiRQ UaQdRP SacNiQg. Repeat Example 4.2, but using 25-mm ceramic Berl saddles as packing material. Solution From Table 4.1: From Example 4.2: 4.8b. SSecific OiTXid hROdXS aQd YRid fUacWiRQ iQ VWUXcWXUed SacNiQg. Repeat Example 4.2, but using Montz metal B1-200 structured packing (very similar to the one shown in Figure 4.3). For this packing, a = 200 mç1, H = 0.979, Ch = 0.547 (Seader and Henley, 1998). Solution From Example 4.2: 4.9b. SSecific OiTXid hROdXS aQd YRid fUacWiRQ iQ fiUVW-geQeUaWiRQ UaQdRP SacNiQg. A WRZeU SacNed ZiWh 25-PP ceUaPic RaVchig UiQgV iV WR be XVed fRU abVRUbiQg beQ]eQe YaSRU fURP a diOXWe Pi[WXUe ZiWh aQ iQeUW gaV XViQg a ZaVh RiO aW 300 K. The YiVcRViW\ Rf Whe RiO iV 2.0 cP aQd iWV deQViW\ iV 840 Ng/P3. The OiTXid PaVV YeORciW\ iV L' = 2.71 Ng/P2-V. EVWiPaWe Whe OiTXid hROdXS, Whe YRid fUacWiRQ, aQd Whe h\dUaXOic VSecific aUea Rf Whe SacNiQg. SROXWiRQ FURP TabOe 4.1: 4.10b. Pressure drop in beds packed Zith first-generation random packings. Repeat E[ample 4.3, but using 15-mm ceramic Raschig rings as packing material. Assume that, for this packing, CS = 1.783. Solution Packed ColXmn 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. Enter data related to the gas and liquid streams Enter liquid flow rate, mL, in kg/s Enter gas flow rate, mG, in kg/s Enter liquid densit\, in kg/m3 Enter gas densit\, kg/m3 Enter liquid viscosit\, Pa-s Enter gas viscosit\, Pa-s Enter temperature, T, in K Enter total pressure, P, in Pa Enter data related to the packing Enter packing factor, Fp, in ft2/ft3 Enter specific area, a, m2/m3 Introduce a units conversion factor in Fp Enter porosit\, fraction Enter loading constant, Ch Enter pressure drop constant, Cp Enter allowed pressure drop, in Pa/m Calculate flow parameter, X Calculate Y at flooding conditions Calculate gas velocit\ at flooding, vGf As a first estimate of the column diameter, D, design for 70% of flooding Calculate gas volume flow rate, QG, in m3/s Calculate liquid volume flow rate, QL, in m3/s Calculate effective particle si]e, dp, in m IWeUaWe Wo find Whe WoZeU diameWeU foU Whe giYen pUeVVXUe dUop ColXmn diameWeU, in meWeUV FUacWional appUoach Wo flooding 4.11b. PUeVVXUe dUop and appUoach Wo flooding in VWUXcWXUed packing. Repeat Example 4.3, but using Montz metal B1-200 structured packing (very similar to the one shown in Figure 4.3). For this packing, Fp = 22 ft 2/ft3, a = 200 mç1, H = 0.979, Ch = 0.547, Cp = 0.355 (Seader and Henley, 1998). Solution Packed ColXmn 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. Enter data related to the gas and liquid streams Enter liquid flow rate, mL, in kg/s Enter gas flow rate, mG, in kg/s Enter liquid densit\, in kg/m3 Enter gas densit\, kg/m3 Enter liquid viscosit\, Pa-s Enter gas viscosit\, Pa-s Enter temperature, T, in K Enter total pressure, P, in Pa Enter data related to the packing Enter packing factor, Fp, in ft2/ft3 Enter specific area, a, m2/m3 Introduce a units conversion factor in Fp Enter porosit\, fraction Enter loading constant, Ch Enter pressure drop constant, Cp Enter allowed pressure drop, in Pa/m Calculate flow parameter, X Calculate Y at flooding conditions Calculate gas velocit\ at flooding, vGf As a first estimate of the column diameter, D, design for 70% of flooding Calculate gas volume flow rate, QG, in m3/s Calculate liquid volume flow rate, QL, in m3/s Calculate effective particle si]e, dp, in m IWeUaWe Wo find Whe WoZeU diameWeU foU Whe giYen pUeVVXUe dUop ColXmn diameWeU, in meWeUV FUacWional appUoach Wo flooding 4.12b, d. Pressure drop in beds packed Zith second-generation random packings. A packed toZer is to be designed for the countercurrent contact of a ben]ene-nitrogen gas mi[ture Zith kerosene to Zash out the ben]ene from the gas. The gas enters the toZer at the rate of 1.5 m3/s, measured at 110 kPa and 298 K, containing 5 mole % ben]ene. Esentiall\, all the ben]ene is abVRUbed b\ Whe NeURVeQe. The OiTXid eQWeUV Whe WRZeU aW Whe UaWe Rf 4.0 Ng/V; Whe OiTXid deQViW\ iV 800 Ng/P3, YiVcRViW\ iV 2.3 cP. The SacNiQg ZiOO be 50-PP PeWaO PaOO UiQgV, aQd Whe WRZeU diaPeWeU ZiOO be chRVeQ WR SURdXce a gaV-SUeVVXUe dURS Rf 400 Pa/P Rf iUUigaWed SacNiQg. (a) CaOcXOaWe Whe WRZeU diaPeWeU WR be XVed, aQd Whe UeVXOWiQg fUacWiRQaO aSSURach WR fORRdiQg. (b) AVVXPe WhaW, fRU Whe diaPeWeU chRVeQ, Whe iUUigaWed SacNed heighW ZiOO be 5 P aQd WhaW 1 P Rf XQiUUigaWed SacNiQg ZiOO be SOaced RYeU Whe OiTXid iQOeW WR acW aV eQWUaiQPeQW VeSaUaWRU. The bORZeU- PRWRU cRPbiQaWiRQ WR be XVed aW Whe gaV iQOeW ZiOO haYe aQ RYeUaOO PechaQicaO efficieQc\ Rf 60%. CaOcXOaWe Whe SRZeU UeTXiUed WR bORZ Whe gaV WhURXgh Whe SacNiQg. SROXWiRQ (a) DeVigQ fRU cRQdiWiRQV aW Whe bRWWRP Rf Whe WRZeU ZheUe Whe Pa[iPXP fORZ Rf gaV aQd OiTXid RccXU BeQ]eQe eQWeUiQg ZiWh Whe gaV: AVVXPiQg WhaW aOO Rf Whe beQ]eQe iV abVRUbed: FURP Whe LXcaV PeWhRd fRU Pi[WXUeV Rf gaVeV: UViQg Whe PacNed CROXPQ DeVigQ PURgUaP: D = 0.913 P f = 0.825 (b) CaOcXOaWe Whe SUeVVXUe dURS WhURXgh Whe dU\ SacNiQg RQ WRS From the Lucas method for mixtures of gases: From equation (4-11): (c) Estimate the volumetric mass-transfer coefficients for the gas and liquid phases. Assume that DL = 5.0 u 10ç10 m2/s. From the wilke-Lee equation, DG = 0.0885 cm 2/s From Table 4.2, CL = 1.192, CV = 0.410Using the Packed Column Design Program: kLah = 0.00675 s ç1; kyah = 0.26 kmol/m 3-s 4.13b, d. Pressure drop in beds packed Zith structured packings. Redesign the packed bed of Problem 4.12, but using Montz metal B1-200 structured packing (very similar to the one shown in Figure 4.3). For this packing, Fp = 22 ft 2/ft3, a = 200 mç1, e = 0.979, Ch = 0.547, Cp = 0.355, CL = 0.971, CV = 0.390 (Seader and Henley, 1998). Solution Using the Packed Column Design Program: D = 0.85 m f = 0.859 kLah = 0.00861 s ç1; kyah = 0.376 kmol/m 3-s 4.14c, d. Air stripping of ZasteZater in a packed column. A wastewater stream of 0.038 m3/s, containing 10 ppm (by weight) of benzene, is to be stripped with air in a packed column operating at 298 K and 2 atm to reduce the benzene concentration to 0.005 ppm. The packing specified is 50-mm plastic Pall rings. The air flow rate to be used is 5 times the minimum. Henry's lawconstant for benzene in water at this temperature is 0.6 kPa-m3/mole (Davis and Cornwell, 1998). Calculate the tower diameter if the gas-pressure drop is not to exceed 500 Pa/m of packed height. Estimate the corresponding mass-transfer coefficients. The diffusivity of benzene vapor in air at 298 K and 1 atm is 0.096 cm2/s; the diffusivity of liquid benzene in water at infinite dilution at 298 K is 1.02 u 10ç5 cm2/s (Cussler, 1997). Solution Calculate m, the slope of the equilibrium curve: For water at 298 K, Calculate the minimum air flow rate: Convert liquid concentrations from ppm to mole fractions At these low concentrations the equilibrium and operating lines are straight, and y2 (max) = y2* = mx2 Using the Packed Column Design Program: D = 1.145 m f = 0.766 kLah = 0.032 s ç1; kyah = 0.335 kmol/m 3-s 4.15b. Stripping chloroform from water b\ sparging with air. Repeat E[ample 4.5, but using an air floZ rate that is tZice the minimum required. Solution Initial estimate of the column height, Z IniWial eVWimaWe of gaV holdXp Calculate poZer 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%. Solution For 99% removal efficiency, xin/xout = 100 Z = 1.30 m WT(Z) = 5.0 kW 4.17b. Stripping chlorine from water b\ sparging with air. A vessel 2.0 m in diameter and 2.0 m deep (measured from the gas sparger at the bottom to liquid overflow at the top) is to be used for stripping chlorine from water by sparging with air. The water will flow continuously downward at the rate of 7.5 kg/s with an initial chlorine concentration of 5 mg/L. Airflow will be 0.22 kg/s at 298 K. The sparger is in the form of a ring, 25 cm in diameter, containing 200 orifices, each 3.0 mm in diameter. Henry's law constant for chlorine in water at this temperature is 0.11 kPa-m3/mole (Perry and Chilton, 1973). The diffusivity of chlorine at infinite dilution in water at 298 K is 1.25 u 10ç5 cm2/s (Cussler, 1997). (a) Assuming that all the resistance to mass transfer resides in the liquid phase, estimate the chlorine removal efficiency achieved. Solution IniWial eVWimaWe of gaV holdXp IWeUaWiQg XQWiO Z = 2.0 P: (b) CaOcXOaWe SRZeU UeTXiUed 4.18c,d. Batch ZasteZater aeration using spargers. IQ Whe WUeaWPeQW Rf ZaVWeZaWeU, XQdeViUabOe gaVeV aUe fUeTXeQWO\ VWUiSSed RU deVRUbed fURP Whe ZaWeU, aQd R[\geQ iV adVRUbed iQWR Whe ZaWeU ZheQ bXbbOeV Rf aiU aUe diVSeUVed QeaU Whe bRWWRP Rf aeUaWiRQ WaQNV RU SRQdV. AV Whe bXbbOeV UiVe, VROXWe caQ be WUaQVfeUUed fURP Whe gaV WR Whe OiTXid RU fURP Whe OiTXid WR Whe gaV deSeQdiQg XSRQ Whe cRQceQWUaWiRQ dUiYiQg fRUce. FRU baWch aeUaWiRQ iQ a cRQVWaQW YROXPe WaQN, aQ R[\geQ PaVV-baOaQce caQ be ZUiWWeQ aV ZheUe cA* iV Whe R[\geQ VaWXUaWiRQ cRQceQWUaWiRQ. IQWegUaWiQg beWZeeQ Whe WiPe OiPiWV ]eUR aQd W aQd Whe cRUUeVSRQdiQg diVVROYed R[\geQ cRQceQWUaWiRQ OiPiWV cA,0 aQd cA,W; aVVXPiQg WhaW cA* UePaiQV eVVeQWiaOO\ cRQVWaQW, aQd WhaW aOO Whe UeViVWaQce WR PaVV WUaQVfeU UeVideV iQ Whe OiTXid ShaVe: IQ aeUaWiRQ WaQNV, ZheUe aiU iV UeOeaVed aW aQ iQcUeaVed OiTXid deSWh, Whe VROXbiOiW\ Rf R[\geQ iV iQfOXeQced bRWh b\ Whe iQcUeaViQg SUeVVXUe Rf Whe aiU eQWeUiQg Whe aeUaWiRQ WaQN aQd b\ Whe decUeaViQg R[\geQ SaUWiaO SUeVVXUe iQ Whe aiU bXbbOe aV R[\geQ iV abVRUbed. FRU WheVe caVeV, Whe XVe Rf a PeaQ VaWXUaWiRQ YaOXe cRUUeVSRQdiQg WR Whe aeUaWiRQ WaQN PiddeSWh iV VXggeVWed (EcNeQfeOdeU, W. W. JU., IndXVWUial WaWeU PollXWion ConWUol, 3Ud ed., McGUaZ-HiOO, BRVWRQ, Ma, 2000): ZheUe cV = VaWXUaWiRQ diVVROYed R[\geQ cRQceQWUaWiRQ iQ fUeVh ZaWeU e[SRVed WR aWPRVSheUic aiU aW 101.3 NPa cRQWaiQiQg 20.9% R[\geQ, PR = abVROXWe SUeVVXUe aW Whe deSWh Rf aiU UeOeaVe, PV = aWPRVSheUic SUeVVXUe, OW = PROaU R[\geQ SeUceQW iQ Whe aiU OeaYiQg Whe aeUaWiRQ WaQN. The PROaU R[\geQ SeUceQW iQ Whe aiU OeaYiQg Whe aeUaWiRQ WaQN iV UeOaWed WR Whe R[\geQ WUaQVfeU efficieQc\, Oeff, WhURXgh ZheUe CRQVideU a 567 P3 aeUaWiRQ SRQd aeUaWed ZiWh 15 VSaUgeUV, each XViQg cRPSUeVVed aiU aW a UaWe Rf 0.01 Ng/V. Each VSaUgeU iV iQ Whe fRUP Rf a UiQg, 100 cP iQ diaPeWeU, cRQWaiQiQg 20 RUificeV, each 3.0 PP iQ diaPeWeU. The VSaUgeUV ZiOO be ORcaWed 5 P beORZ Whe VXUface Rf Whe SRQd. The ZaWeU WePSeUaWXUe iV 298 K; aWPRVSheUic cRQdiWiRQV aUe 298 K aQd 101.3 NPa. UQdeU WheVe cRQdiWiRQV, cV = 8.38 Pg/L (DaYiV aQd CRUQZeOO, 1998). (a) EVWiPaWe Whe YROXPeWUic PaVV-WUaQVfeU cRefficieQW fRU WheVe cRQdiWiRQV fURP eTXaWiRQV (4-23) aQd (4-25). (b) EVWiPaWe Whe WiPe UeTXiUed WR UaiVe Whe diVVROYed R[\geQ cRQceQWUaWiRQ fURP 0.5 Pg/L WR 6.0 Pg/L, aQd caOcXOaWe Whe UeVXOWiQg R[\geQ WUaQVfeU efficieQc\. (c) EVWiPaWe Whe SRZeU UeTXiUed WR RSeUaWe Whe 15 VSaUgeUV, if Whe PechaQicaO efficieQc\ Rf Whe cRPSUeVVRU iV 60%. SROXWiRQ IniWial eVWimaWe of gaV holdXp Initial estimate of transfer efficienc\ (b) Calculate power required 4.19c,d. Batch ZasteZater aeration using spargers; effect of liquid depth. CRQVideU Whe ViWXaWiRQ deVcUibed iQ PURbOeP 4.18. AccRUdiQg WR EcNeQfeOdeU (2000), fRU PRVW W\SeV Rf bXbbOe-diffXViRQ aeUaWiRQ V\VWePV Whe YROXPeWUic PaVV-WUaQVfeU cRefficieQW ZiOO YaU\ ZiWh OiTXid deSWh Z accRUdiQg WR Whe UeOaWiRQVhiS ZheUe Whe e[SRQeQW Q haV a YaOXe QeaU 0.7 fRU PRVW V\VWePV. FRU Whe aeUaWiRQ SRQd Rf PURbOeP 4.18, caOcXOaWe NLa aW YaOXeV Rf Z = 3P, 4P, 6P, aQd 7 P. EVWiPaWe Whe cRUUeVSRQdiQg YaOXe Rf Q fURP UegUeVViRQ aQaO\ViV Rf Whe UeVXOWV. HiQW: RePePbeU WhaW Whe WRWaO YROXPe Rf Whe SRQd PXVW UePaiQ cRQVWaQW, WheUefRUe Whe cURVV-VecWiRQaO aUea Rf Whe SRQd PXVW chaQge aV Whe ZaWeU deSWh chaQgeV. SROXWiRQ UViQg Whe SURgUaP deYeORSed iQ PURb 4.18, Whe fROORZiQg YecWRU Rf UeVXOWV iV geQeUaWed 4.20c. Flooding conditions in a packed cooling toZer. A cRROiQg WRZeU, 2 P iQ diaPeWeU, SacNed ZiWh 75-PP ceUaPic HifORZ UiQgV, iV fed ZiWh ZaWeU aW 316 K aW a UaWe Rf 25 Ng/P2-V. The ZaWeU iV cRQWacWed ZiWh aiU, aW 300 K aQd 101.3 NPa eVVeQWiaOO\ dU\, dUaZQ XSZaUd cRXQWeUcXUUeQWO\ WR Whe ZaWeU fORZ. NegOecWiQg eYaSRUaWiRQ Rf Whe ZaWeU aQd chaQgeV iQ Whe aiU WePSeUaWXUe, eVWiPaWe Whe YROXPeWUic UaWe Rf aiUfORZ, iQ P3/V, Zhich ZRXOd fORRd Whe WRZeU. SROXWiRQ LMV = OiTXid PaVV YeORciW\ GMV = gaVV PaVV YeORciW\ InWUodXce a XniWV conYeUVion facWoU in Fp IniWial eVWimaWe of GMV 4.21c,d. Design of a sieve-tra\ column for ethanol absorption RepeaW Whe calcXlaWionV of E[ampleV 4.6, 4.7, 4.8, and 4.9 foU a colXmn diameWeU coUUeVponding Wo 50% of flooding. SolXWion FUom Whe SieYe-PlaWe DeVign PUogUam, Whe folloZing UeVXlWV aUe obWained foU I = 0.5 D = 1.176 m W = 0.6 m 'P = 590 Pa/WUa\ FUoXde No. = 1.22 (no e[ceVViYe Zeeping) E = 0.0165 EOG = 0.8123 EMG = 0.8865 EMGE = 0.878 4.22c,d. Design of a sieve-tra\ column for aniline stripping. A sieve-tray tower is to be designed for stripping an aniline (C6H7N)-water solution with steam. The circumstances at the top of the tower, which are to be used to establish the design, are: Temperature = 371.5 K Pressure = 100 kPa Liquid: Rate = 10.0 kg/s Composition = 7.00 mass % aniline Density = 961 kg/m3 Viscosity = 0.3 cP Surface tension = 58 dyne/cm Diffusivity = 4.27 u 10ç5 cm2/s (est.) Foaming factor = 0.90 Vapor: Rate = 5.0 kg/s Composition = 3.6 mole % aniline Density = 0.670 kg/m3 Viscosity = 118 mP (est.) Diffusivity = 0.116 cm2/s (est.) The equilibrium data at this concentration indicates that P = 0.0636 (Treybal, 1980). (a) Design a suitable cross-flow sieve-tray for such a tower. Take do = 5.5 mm on an equilateral- triangular pitch 12 mm between hole centers, punched in stainless steel sheet metal 2 mm thick. 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