AO和A2O工艺对膜生物反应器处理焦化废水影响的研究宋志伟

3　12环境工程学报Vol.3,No.12200912ChineseJournalofEnvironmentalEngineeringDec.2009A/OA2/O宋志伟　张芙蓉　曲　直(,150027)　　,A/OA2/O,、,。:A2/O、NH3-N、COD99%、90%95%;A/O、NH3-NCOD97%、75%93%。A2/ONH3-NA/O,50%～70%。,A2/O59%,A/O56%。,A2/OA/O。　　　A2/O　A/O　X703　　　A　　　1673-9108(2009)12-2198-05InfluenceofA/OandA2/OprocessoncokingwastewatertreatmentinmembranebioreactorSongZhiwei　ZhangFurong　QuZhi(CollegeofResourceandEnvironmentalEngineering,HeilongjiangInstituteofScienceandTechnology,Harbin150027,China)Abstract　Inordertoinvestigateoptimumprocess,anoxic-anaerobic-oxic(A2/O)andanoxic-oxic(A/O)processwereappliedtotreatcokingwastewaterinmembranebioreactor(MBR),pollutantremovalratewasana-lyzed,andmembranefoulingwasstudied.Theresultsshowedthattheremovalrateofphenol,NH3-N,CODwas99%,90%and95%respectivelyusingA2/Oprocess.Bycontrast,itwas97%,75%,93%respectivelywithA/Oprocess.TheNH3-Nremovalrateofformerwasobviouslysuperiortothatoflater,thedenitrificationrateofA2/Owasmaintainedintherangeof50%～70%,whichwasbetterthanthatofA/O.Analysisofmembranefoulingindicatesthatinfluenceofoperatingmodeonthemembranefoulingwasnotobvious,thepermeatefluxdeclinewithA2/Oreached59%,whileitwas56%underA/O.ItcouldbeseenthatA2/Oprocesshadanad-vantageoverA/Oprocess.Keywords　membranebioreactor;cokingwastewater;anoxic-anaerobic-oxic;anoxic-oxic:(YJSCX2009-015HKJ):2009-07-29;:2009-08-21:(1968～),,,,。E-mail:[e-mail]　　、,、、、,[1],、,,。,,16。,。(membranebioreactor,MBR),,,。,,NH3-N12:A/OA2/O[2,3],[4～6],。,,,,,[7]。,,,CODNH3-N2[8]。,A/O(-),,,A/O。A2/O(--)A/O,,,[9～11]。,A/O[12～16],。A2/O。A/OA2/O,、,。1　1.1　(1),2,25L,,。(0.1～0.2μm,0.2m2),。,,,,,。1.2　:,1000mg/L,100mg/L,150mg/L,MgSO4·7H2O15mg/L,375mg/L,KH2PSO415mg/L,K2HPSO435mg/L,Fe-1　Fig.1　SchematicdiagramofmembranebioreactorSO4·7H2O20mg/L,CaCl2100mg/L,NH4Cl2100mg/L,100mg/L。:,6100mg/L,SV25%。1.3　[17]:,COD,NH3-N,,NO3-N,NO2-NN-(1-)-。1.4　15d,20～25℃。A/O4h,0.5～1mg/L,16h,2.5～3.5mg/L[13,14];A2/O4h,0.5～1mg/L,3h,0.5mg/L,16h。,pH6.5～7.5。,8min,7min;,3000～4000mg/L[14]。2　2.1　A/OA2/O22。2,370mg/L,A2/O5mg/L,99%;A/O10mg/L,97%,A2/OA/O5mg/L。2219932　A2/OA/OFig.2　ComparisonofremovalrateofphenoliccompoundsbetweenA2/OandA/Oprocess95%,,A/OA2/O2,。A2/OA/O,,A2/O,。2.2　A/OA2/O3。3　A2/OA/ONH3-NFig.3　ComparisonofremovalrateofNH3-NbetweenA2/OandA/Oprocess3,A/O100mg/L,20mg/L,,75%。A2/O,,,,,7d,100mg/L,10mg/L,A/O10mg/L,90%。NH3-N,NH3-N,NH3-N。,,,,,,,24。4　A2/OA/OFig.4　ComparisonofdenitrificationratebetweenA2/OandA/O4,A2/O50%～70%,A/O30%～50%,A2/OA/O,,,,,,,A2/OA/O,2。2.3　CODA/OA2/O2COD,5。5　A2/OA/OCODFig.5　ComparisonofCODremovalratebetweenA2/OandA/Oprocess220012:A/OA2/O5,2COD2400mg/L,2,A2/O100mg/L,COD95%,,。A/OCOD150mg/L,93%,A2/OA/OCOD50mg/L,A2/O,,,。2,COD,,COD,A2/O。2.4　2.4.1　膜通量的变化A/O、A2/O6。6　Fig.6　Changeofmembraneflux　　6,,,A/O,56%,A2/O,59%。A/OA2/O2。2.4.2　膜表观结构的变化,,6。7　Fig.7　SEMphotosofmembranemicrostructure　　7(a),,(b)A2/O,(c)A/O,,,。7(b)7(c),A/O,,,A2/O。3　　(1)A2/OA/O2,A2/O5mg/L,99%;A/O10mg/L,97%,A2/OA/O5mg/L。(2)A2/ONH3-NA/O,A2/ONH3-N90%,50%～70%,A/ONH3-N75%,30%～50%。(3)A2/OCOD100mg/L,COD95%;A/OCOD150mg/L,2201393%。(4),。[1],..,2006,(2):58～59[2]YamamotoK.Householdmembranebioreactorindomes-ticwastewatertreatment.Wat.Sci.Tech.,1993,27(1):171～178[3]MasudaS.,WatanableY.,IshiguroM.Bio-filmproper-tiesandsimultaneousnitrificationanddenitrificationinaerobicrotatingbiologicalcontactors.Wat.Sci.Tech.,1991,23(12):1355～1363[4]Halling-SorensenB.,HjulerH.Simultaneousnitrificationanddenitrificationwithandupflowfixedbedreactorap-plyingclinoptiloliteasmedia.Wat.Treat.,1992,7:77～88[5]MoriyamaK.,SatoK.,HaradaY.,etal.Simultaneousbiological-removalofnitrogenandphosphorususingox-ic-anaerobic-oxicprocess.Wat.Sci.Tech.,1990,22(7～8):61～66[6]MunchE.V.,LantP.,KellerJ.Simultaneousnitrifica-tionanddenitrificationinbench-scalesequencingbatchreactors.Wat.Res.,1996,30(2):277～284[7],..,1999,25(2):63～69[8]..,2007,38(1):62～63[9],,.-.,2007,4(1):33～36[10],,,.-.,1995,8(1):1～4[11],,.COD.,2007,38(2):108～111[12],.-.,2008,28(4):40～43[13],,..,2008,2(11):1475～1478[14],,..,2006,16(4):209～212[15],,,..,2009,28(2):1～5[16],,..,2006,17(6):88～90[17]《》.(4).:,2002.256～258,2742202