超滤膜组件结构与性能研究

、、、。UF1.5～2m。、[1]。[2-3]。、。、TMP、、。11.1PVDF1。1.21。、。PLCa3a3、a4。a312111.3003872.310012、。、。、。。30%。300mg/LNaClO+NaOHpH11.499%。TQ028.8A1000-3770(2014)09-[e-mail]@263.net/m2/μm/mm/mmPVDF-1808PVDF660.030.71.3/(m3·h-1)/MPa/MPa/℃pHpH2.0～8.00.30.155～453～102～121Tab.1TheUFmembranemodulesperformanceparameters40920149TECHNOLOGYOFWATERTREATMENTVol.40No.9Sep.,20141012Tab.2InletandoutletwaterqualityofUFmembranesystem/NTUpHCOD/(mg·L-1)ρ/(g·L-1)ρ/(mg·L-1)TDSCl-Ca2+SO42-FeSS15～240.06～0.117.3～7.87.4～7.80.35～0.650.32～0.5434.2～39.334.1～39.017.3～18.217.2～18.00.42～0.470.42～0.462.10～2.492.02～2.420.53～0.660.12～0.2210～400～31Fig.1TheprocessoftheUFmembranesystema6a3a6a4a5。a4。1.330min→60s→60s→60s→30min……6m3/h3m3/h20%5m3/h0.10m3/h100%。1.42。22.1、2172h。213m3/h26m3/h32TMPTMP。212TMPTMP23kPa26kPa7%。TMP28kPa32kPa13%TMPTMP。22TMP57kPa53kPaTMP85kPa59kPa48%9%。、、TMP。。。2TMP。TMPTMP。TMPTMPTMPTMP。。。2TMPFig.2Transmembranepressureandthegrowthratepressure-timecurveunderdifferenteffluentways030609012015018003060900102030405060
t/hTMP/kPa/%4091022.232TMP。3TMP80%73%TMP。。[4]。TMP[5]。。2。TMP[6]。、TMP。、、。2.3[8-9]。。23。31c2a。。、。。1b2c2NaClO+NaOH、。、。3Tab.3TheChemicalcleaningandtheeffectoftheUFmembranesystem/%/(m3·m-2·h-1·MPa-1)12a)0.4%pH2.530minb)30mg/LNaClO+NaOH30min、30min、30minc)3min、5、0.1m3/h60s3m3/h60s3m3/h10min4a)5min、5、0.1m3/h60s3m3/h60s3m3/h10min4b)0.4%pH2.230min、25minc)300mg/LNaClO+NaOHpH11.430min、30min、30min1.961.961.961.961.961.961.051.291.621.561.681.741.291.621.671.681.741.95263653015533Fig.3Inletwaterpressure-timeandTransmembranepressure-timecurveunderdifferenteffluentways0306090120150180405060708090100110
p/kPat/h103THERESEARCHOFULTRAFILTRATIONMEMBRANEMODULESTRUCTUREANDPERFORMANCEZuoYing1,ShenJuli2,LvXiaolong1,ZhuYuanyuan1(1.StateKeyLaboratoryofHollowFiberMembraneMaterialsandMembraneProcess,InstituteofBiologicalandChemicalEngineering,TianjinPolytechnicUniversity,Tianjin300387,China;2.HangzhouWaterTreatmentTechnologyDevelopmentCenter,Hangzhou310012,China)Abstract:Theauthorusedmembranemoduletocontrolthewatervalveforinvestigationoftherunningconditionofmembranemodule,whichhassingle-endedanddouble-endedeffluentstructuralstyle.Inaddition,thechemicalcleaningtestingwasalsostudiedinthisresearch.Theresultsshowthatthetransmembranepressure,membranefoulingandcleaningeffectarequitedifferentduetothedifferenteffluentwaysofultrafiltrationmembranes.Comparedtothesingle-endeffluentway,thegrowthratesoftransmembranepressureandmembranefoulingofthedouble-endseffluentwayareslowerundertwokindsofmembranefluxconditions.Whileinthehighfluxcondition,theadvantageofdouble-endsstructureismoreobvious.Ineveryoperationterm,thedouble-endstransmembranepressureisalwayslessthansingle-endstructure,andthetransmembranepressurerecoveryperformanceofdouble-endseffluentwillbebetterafterthebackwashing.Beforethechemicalcleaning,aphysicalcleaningcouldremovemostsedimentonmembranesurfaceandthepermeabilityrecoverycouldachieve30%.Thebestcleaningapproachisadding300mg/L(pH11.4)ofNaClO+NaOHafteracidcleaning.Inthatcase,thepermeabilityrecoverywillachieve99%,thereforemostofthemembranefoulingcomponentsarebacteriaandorganicpollutant.Keywords:ultrafiltration;moduledesign;effluentstyle;chemicalcleaning、、、[7-8]。[9]。1a2bpH2～3。Ning、PVDF、[10-11]。NaClO+NaOHHCl。。+NaClO+NaOH。85%299%。3TMP。TMP。TMPTMP。30%。300mg/LNaClO+NaOHpH11.499%。[1]YoonSH,LeeS,YeomIK-Tae.Eexperimentalverificationofpressuredropmodelsinhollowfibermembrane[J].JMembrSci.,2008,3(10):7-12.[2],,.[J].,2007,27(5):82-88.[3],,.[J].,2008,28(1):31-34.[4],,.[J].,2012,31(5):42-45.[5].[J].,2003,23(4):255-260.[6]Seong-HoonY,Hyung-SooK,Ik-TaeY.Optimizationmodelofsubmergedhollowfibermembranemodules[J].JMembrSci.,2004,234:147-156[7],./[J].,2009,3(6):13-16.[8],.[J].,2005,25(5):402-405.[9],,.[J].,2009,25(23):41-44.[10]NingRY.ReverseosmosisprocesschemistryrelevanttotheGulf[J].Desalination,1999,123(23):157-164.[11],,.[J].,2008,31(7):11-13.409104