含硫酸钠高氨氮废水膜技术脱除研究王小乐

。、、[1]。15%[2]NH3-N6g/L[2-3]。。、[4]。、、、、。1976WatanabeH、、、[5-16]。。11.1、pH、。1.22准90mm×1000mm0.50～0.60mm、65～75μm0.1～0.3μm。≥12000≤0.3MPa5～40℃13.91m2。1.31。pH12。。312111.1001242.100037。25.1℃5.2℃44.7%pH9.511.581Na2SO416.7g/L150.3g/L14.6%NH3-N4g/L32dNH3-N95%3.7～4.4μm/s。TQ028.8A1000-3770(2016)[e-mail]@bjut.edu.cn42520165Vol.42No.5May,2016DOI:10.16796/j.cnki.1000-3770.2016.05.006233。2。2。1.4K12[17-20]K=Vln(ρ0/ρt)/(At1)1K=qVln(ρ0/ρt)/A。2ρ0、ρt、NH3VAt1qV。、[19-21]。1K=1KL+1KM。3KLKM。QiZKL4[22-23]KLr1/DW=1.88[4ur12/(lDW)]1/3。4r1DWul。KM[21]KM=DGετ1r1HRTln(r2/r1)。5DGετHNH3R8.314×10-3J/(mol·K)Tr2。6J=m/(At2)。6Jt2m。[24]。NH3-N722pHPHS-2CpHpHpHPHG-21D-1pH/ORPPA-C3。22.1NH3-N1136L/hpH11.5pH0NH3-N4g/LNa2SO416.7g/L5.2～25.1℃5%3。3NH3-N。25.1℃5.2℃5.17μm/s2.86μm/s44.7%NH3-N96.2%83.5%。DGDW45KMKL。。1Fig.1Flowchartofsinglemembrane2Fig.2Schematicdiagramofammoniaremovalprinciple42524θ/℃3NH3-NFig.3EffectoftemperatureonNH3-Nremoverateandoverallmasstransfercoefficient05101520253050607080901000123456
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K/(μm·s-1)NH3-N。。2.2pHpHNH3-N。1136L/hpH0NH3-N4g/L16℃Na2SO416.7g/LpH9.56～13.484。4pH。1pH9.5611.490.7μm/s5.6μm/s22.7%86.2%。7pHDGDwNH3NH4+NH3KMKLKNH3-N。lg(NH3/NH4+)=pH-pKa。72pH11.4913.48NH3-N。NH3KMKL。pH11.5。2.3。136L/hpH11.52pH0NH3-N4g/L25℃Na2SO416.7g/L。5。55.3μm/s。400min3.8μm/s50min70.4%。。。2.4Na2SO4Na2SO4。21、50、136L/hpH11.5210%H2SO4NH3-N4g/L20℃Na2SO416.7～150.3g/L。67。4pHNH3-NFig.4EffectofpHonNH3-NremoverateandoverallmasstransfercoefficientK/(μm·s-1)910111213140204060801000123456
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pH5Fig.5DifferentprocessingmodeonoverallmasstransfercoefficientK/(μm·s-1)0501001502002503003504000123456

t/min256Na2SO416.7g/L150.3g/L14.6%Na2SO4。Na2SO4。Na2SO4Na2SO4。7Na2SO4。24h16.7g/LNa2SO417.5mg/(cm2·h)150.3g/LNa2SO4-11.7mg/(cm2·h)。Na2SO4Na2SO4。0。Na2SO4。2.532d。21136L/hpH11.43～11.6910%H2SO419～25℃NH3-N4g/LNa2SO416.7g/L。8。832dNH3-N93.4%～96.1%3.7～4.4μm/sNH3-N200mg/L。5－6。。。3NH3-NNH3-N。pH1。Na2SO4。32d。ρ(Na2SO4)/(g·L-1)6Na2SO4Fig.6Na2SO4concentonoverallmasstransfercoefficientK/(μm·s-1)0204060801001201401600.00.40.81.21.62.07Na2SO4Fig.7Na2SO4concentonwaterpermeateflux0510152025-30-20-1001020J/(mgcmh)t/h16.766.8116.933.483.5133.650.1100.2150.3ρ(Na2SO4)0510152025303550607080901000123456
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t/dK/(μm·s-1)832dNH3-NFig.8NH3-Nremoverateandoverallmasstransfercoefficientin32dstabilityexperiment42526422－2016、、、、、、、。!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!ResearchonRemovalofHighAmmoniaWastewaterContainingSodiumSulfatebyMembraneAbsorptionWangXiaole1,TanKeyan2,GaoYang1,YangHong1(1.BeijingUniversityofTechnology,KeyLaboratoryofBeijingforWaterQualityScienceandWaterEnvironmentRecoveryEngineering,100124;2.NationalResearchCenterforGeoanalysis,ChineseAcademyofGeologicalSciences,100037:Beijing,China)Abstract:Theexperimentswerecarriedouttostudytheeffectofvariousparametersonthetransferperformance,andtheexperimentalfeasibilitywasidentified.Theresultsdemonstratedthatasthetemperaturedecreasedfrom25.1℃to5.2℃,theoveralltransfercoefficientdecreasedby44.7%.Inaddition,increasingpHfrom9.5to11.5resultedin800%enhancementintheoveralltransfercoefficient.Thereactionsolutionthroughthemembraneofacontinuousprocessrun,theoveralltransfercoefficientremainedunchanged.Whencirculatedthereactionsolution,however,theoverallmasstransfercoefficientdecreasedgradually.WiththemassconcentrationofNa2SO4increasedfrom16.7g/Lto150.3g/L,theoveralltransfercoefficientincreasedby14.6%andthepermeatefluxturnedfrompositivetonegative.Inthestabilityexperiment,withmassconcentrationofammoniawas4g/L,thepoly-propylenehollowfibermembranerun32dstably,ammoniaremovalrateremainedabove95%,theoverallmasstransfercoefficientstabilizedbetween3.7~4.4μm/s,andtheleakphenomenonwasnotobserved.Keywords:polypropylenehollowfibermembrane;membraneabsorption;highammoniawastewatercontainingsodiumsulfate[1],,.、[J].,2010,26(10):5-8.[2],,,.[J].,2012,63(4):1108-1115.[3],,,.[J].,2013,31(1):5-8.[4],,,.[J].,2010,26(14):26-29.[5]WatanabeH,MiyauchiT.ThePermeationofiodinethroughadiaphragmtypeliquidmembrane:thediffusioncoefficientofiodineinpoly(dimethylsiloxane)[J].KagakuKogakuRonbunshu,1976,2(3):262-265.[6],./[J].,1996,24(3):233-238.[7]SemmensMJ,FosterDM,CusslerEL.Ammoniaremovalfromwaterusingmicroporoushollowfibers[J].JournalofMembraneScience,1990,51:127-140.[8],,,.[J].,2002,3(7):56-60.[9],,.[C].:,2007.[10].[D].:,2010.[11]MandowaraA,BhattacharyaPK.Membranecontactorasdegasseroperatedundervacuumforammoniaremovalfromwater:Anumericalsimulationofmasstransferunderlaminarflowconditions[J].Computers&ChemicalEngineering,2009,33(6):1123-1131.[12].、、[D].:,2012.[13].、[D].:,2013.[14]./[D].:,2013.[15],,./[J].,2005,31(2):17-20.[16],,./[J].,2004,24(6):29-33.[17],.[J].,1994,13(2):157-162.[18],.NH3-N[J].,1995(4):7-10.[19]QinY,CabralJMS.Lumenmasstransferinhollow-fibermembraneprocesseswithconstantexternalresistances[J].AicheJournal,1997,43(8):1975-1988.[20]AndYQ,CabralJMS.Lumenmasstransferinhollow-fibermembraneprocesseswithnonlinearboundaryconditions[J].AicheJournal,1998,44(4):836-848.[21]WangShichang,Xu