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、、、、。。、、、[1]。[2-3]、。、、、、。EGSBUASB。EGSBUASBHRT。EGSB。EGSB、SO42-EGSB。11.11。EGSB。EGSB13.4L2.0m1.6m。EGSB11211.0500512.071000EGSB35℃±1℃11d75%COD6000mg·L-112kgCOD·m-3·d-12m·h-1CODSO42-80%2000mg·L-1COD/SO42-3CODSO42-、、。EGSBX703.1A1000-3700(2009)02-092-052008-07-1407276708D1954-、13811854754E-mailxuan7524@yahoo.com.cn。35220092TECHNOLOGYOFWATERTREATMENTVol.35No.2Feb.,200992DOI:10.16796/j.cnki.1000-3770.2009.02.0251EGSBTable1ProcessparametersofEGSBreactor/d/m·h-1/kgCOD·m-3·d-1pHCOD/mg·L-1/mg·L-1/%1～1112～5960～1410～4:14:1～9:19:10.2～1.01.0～2.02.04.04.0～12.012.06.4～7.36.8～7.46.7～7.520002000～6000600021～8050～270500～100096～9895～9881～8935±1℃。1.2。。mCODmNmP=20051。1.3UASB。0.948g·mL-194.0%VSS/TSS89.7%。1.4pH231pHCODHACH-45600CODTOC-Apollo9000TOCBOD5TSSVFADX-600SO42-、NO3-、Cl-DX-600ZD-3A。2141dEGSB1～11d、12～59d60～141d。1。2.111d。4kgCOD·m-3·d-10.2m·h-1。。2、3。4dCOD95%114:15kgCOD·m-3·d-11m·h-1COD98%。。、 1EGSBFig.1SchematicdiagramoftheexperimentalEGSBreactor12345678910110250500750100012501500175020002250 /dCOD/mg L 90919293949596979899100COD/%2EGSBFig.2TheresultofEGSBreactorstartupprocess3a×703b×4k3SEMFig.3TheSEMgraphofthegranularsludgeinstartupprocessEGSB93。。2.248d。EGSB。4、5。30L·d-1。COD。12d59d4kgCOD·m-3·d-112kgCOD·m-3·d-141911m·h-12m·h-1EGSB。EGSBCOD95%。。2.382d。EGSB、EGSB。6、7。6000mg·L-1。60d16.67%COD8dCOD89%。COD。28dCOD80%～89%。20%66.67%COD82%SO42-。。128d75%2376.8mg·L-12dCOD65%306mg·L-1、。2.4。[4-6]。COD/SO42-EGSB5a×455b×4k5SEMFig.5TheSEMgraphofthegranularsludgeinsludgecultureprocess1216202428323640444852566001000200030004000500060007000/dCOD/mg L 90919293949596979899100COD/%4Fig.4Theresultofsludgecultureprocess607080901001101201301401020304050607080 /d/%5060708090100COD /%6Fig.6Theresultofprocesstest7a×607b×4k7SEMFig.7TheSEMgraphofthegranularsludgeinprocesstest35294。8。61d124d225mg·L-11665mg·L-1EGSBCOD90%80%。125d1893mg·L-170%COD80%。2000mg·L-1。9COD/SO42-。COD/SO42-CODSO42-。COD/SO42-25CODSO42-89%COD/SO42-5～10COD81%～86%SO42-2000mg·L-1COD/SO42-3CODSO42-。COD6000mg·L-1、12kgCOD·m-3·d-12m·h-1SO42-2000mg·L-1COD/SO42-3CODSO42-80%。EGSB。3EGSB35±1℃4kgCOD·m-3·d-1COD2m·h-1。75%EGSBCOD6000mg·L-112kgCOD·m-3·d-12m·h-1CODSO42-80%。COD6000mg·L-1、12kgCOD·m-3·d-12m·h-1SO42-2000mg·L-1COD/SO42-3。[1],,.[J].,2006,24(1):30-32.[2],.[J].,2002,28(1):50-52.[3],,.(MBR)[J]..2005,23(4):12-14.[4],,,.[J].,2001,27(1):37-39.[5],,.[J].,2003,29(3):46-50.[6],,.[J].,2005,31(3):20-24.6070809010011012013014005001000150020002500020406080100120SO /% SO /mg L /d 8Fig.8Relationshipbetweensulfateconcentrationandremovalrate23.45.49.418.675.433.373.1750556065707580859095100 /%COD/SO 9COD、SO42-COD/SO42-Fig.9RelationshipbetweenCODremovalrateandCOD/SO42-EGSB95TREATMENTOFPHARMACEUTICALINTERMEDIATESECONDARYEFFLUENTUSINGPVDFTUBULARMEMBRANEWULi1,XUZhen-liang1，ZHANGJuan2,FENGFei1,CHENGLiang1(1.MembraneScienceandEngineeringR&DLab,ChemicalEngineeringResearchCenter，EastChinaUniversityofScienceandTechnology，Shanghai200237,China;2.StateKeyLaboratoryofPollutionControlandResourcesReuse,NanjingUniversity,Nanjing210093,China)Abstract:PVDFtubularultrafiltrationmembraneswithcutoffmolecularweightof100000Dalton(MembraneA)and50000Dalton(MembraneB)wereusedforthepre-treatmentofthepharmaceuticalintermediatebiochemistrydrainage.Theeffectoftrans-membranepressure,feedflowvelocity,temper-ature,pHandmembranefoulingontheUFprocesseswasanalyzed.TheresultsshowedthatMembraneBwasbetterthanMembraneA.Theconstantfluxwas50L·m-2·h-1atatrans-membranepressureof0.12MPa,feedflowvelocityof3.4m·s-1,atemperatureof14℃andpHvalueof6～8.Theperi-odofchemicalcleaningwas72hours.TheaveragerejectionratioofCODwas25.5%.Theaveragerejectionratioofanilinewas40.5%.Theturbidityofpermeatewaslowerthan0.5NUTwhileSDIwaslowerthan1.5.TheseresultsmettherequirementofROfeedflowquality.Besides,therecoveryeffi-ciencyofpurewaterforMembraneBwasmorethan80%aftermembranecleaningbyNaOHsolutionwhichpHwas12.Ithadagoodrepeatability.Keywords:tubularUF;bio-chemicaleffluent;PVDF;wastewaterreuse;pretreatmentDYEINGWASTEWATERTREATMENTBYPOROUSCERAMICMEMBRANEINMICROFILTRATIONLIWei,LIFang,CHENJi-hua（CollegeofEnvironmentalScienceandEngineering,DongHuaUniversity,Shanghai201620,China）Abstract:Thefiltrationprocessdealingwithdyeingwastewaterbyporousceramicmicrofiltrationmembranewasstudied.Theeffectofoperationparame-ters,suchasoperationpressure,crossflowvelocity,onpermeatesfluxofthemembraneandoperationtimewasdiscussed.TheresultsshowedtheremovalefficiencyofCODwasaround30%andtheremovalefficiencyofNH3-Nwasaround20%withtheoperationpressurewas0.275MPa,thecrossflowvelocitywas2.5m·s-1andtheoperationtimewas20min.Whenthedosageofkaolinwas0.3g·L-1inthewastewatertheaverageremovalefficiencyofCODwas50%.Keywords：porousceramicmembrane;dyeingwastewater;microfiltration;wastewatertreatment,2003,24(1):91-97.[7]BarkerDJ,StuckyDC.Areviewofsolublemicrobialproducts(SMP)inwastewatertreatmentsystems[J].WatRes.,1999,33(14):3063-3082.[8],,,.[J]..2006,26(3):37