分段进水多级AO生物脱氮工艺设计研究高俊发

AO高俊发　王　骊　关　江　李　建(,710054)　介绍分段进水多级AO生物脱氮工艺的基本原理及工艺特性,并结合国外研究现状和工程应用实例,对该工艺运行操作和设计的几个重要影响因素进行了探讨。分段进水多级AO生物脱氮工艺取消了混合液内回流,反应器段数越多,脱氮效率越高,但是工艺设计与运行也会随之变复杂,工程实际应用中多采用2～4段。各级缺氧段与好氧段的比值可采用1∶1.5。污泥回流比为50%的分段进水多级AO三段工艺的脱氮率为78%。　分段进水　多级AO工艺　生物脱氮0　,。,、、,。,AO。1　,1,(SRT)。MLSS,。:AO,,AOE,n[1]:En=100%-(100%-E)n　En———;E———AO;n———。,1。2　2.1　为生物脱氮过程提供足够的碳源,CODCr,。1　,,,,,。2.2　脱氮效率高AO,。ηN:ηEX;、ηDN[2]。:ηN=ηEX+ηDN(1)ηEX=α·XE·QECT-Nin·Q(2)ηDN=(1-ηEX)(∑n-1i=1QiQ+r)(1+r)(3)　CT-Nin———,gm3;a———,gg;XE———,gm3;QE———,m3d;Q———,m3d;r———,%。,(ηEX=0),(1)=(3)ηN=ηDN=1-1n(1+r)11　　　200712256DOI:10.13205/j.hjgc.2007.06.028η=1-1n×11+r×100%(4)　η———,%;n———。()2。2　　2,,。0%～50%,;50%～150%,;150%,。50%()AO378%,,50%300%。,AO。2.3　池容小,基建投资省,,50%,SS,MLSS。MLSS,MLSS,MLSS。(),1[3]。1　AOAOMLSS(mg·L-1)%3000100100MLSS(mg·L-1)%1540018.52385725.93300033.477.8(50%)　　1,MLSS,AO30%,,77.8%,。2.4　节省能耗,减少运行费用AO,,70%。2.5　承受冲击负荷能力强,,。“,”[4]。。2.6　运行方式灵活AO,,。10℃,AOOO;15～30℃,AOAO;30℃,AAOO,,。3　3.1　反应器段数、,,,,。,(4)。2～4[5]。3.2　进水流量分配,。,。,,12,,[6]。3.3　反应器各段容积比,。n[7]:T=nKC0Cn1n-1(5)12　　　200712256　T———,h;K———(、pH,,mg(g·h);C0———,mgL;Cn———,mgL。,,。1,,,,,。。,KDN0.27mg(g·h),KN0.4mg(g·h),1∶1.5,11。3.4　污泥回流比AO,。TNMLSS。,MLSS,,50%。4　3×104m3d,、2,50%,20℃。2　、mgLBOD5CODCrSSTNTP200350200354≤20≤60≤20≤10≤1　　2,35-1035=71.4%,(4)3。3AO,2。610h,。T(A1)∶T(O1)∶T(A2)∶T(O2)∶T(A3)∶T(O3)=1∶1.5∶1.5∶2.3∶2.3∶3.4,V=15000×1024=6250m3。3。　　,3AO78%,BOD590%。　　　3　15000m3d()mmmm3A15.8156522O18.7156783A28.7156783O213.31561197A313.31561197O32015618006282,AO、。5　(1)AO,、、,。(2),,。2～4,50%。(3)AO30%,,,。(4),,1∶1.5,11。(5),。10℃,AOOO;15～30℃,AOAO;30℃,AAOO,,。[1]　.AO.,2003,26(4):8-9.[2]　,,.AO.,2006,37(1):7-9.[3]　ステップ..JS,91217.[4]　,.AO———AO、AO.,2001,12(3):341-342.[5]　,..,2003,19(4):32-36.13　　　200712256[6]　,,..,2006,7(10):83-86.[7]　.D.,.W...,,.:,1984:17-20.　　710054　416#E-mail　[e-mail]2007-05-22物化法处理氟苯生产废水技术＊李国平　邱　阳　夏明芳　张利民　王志良(,210036)　研究酸化+萃取+无机除氟+粒子群电催化氧化等物化技术处理氟苯生产废水的工艺条件。在适宜的工艺条件下,废水中CODCr、苯酚、F、石油类去除率可分别达到99.2%、99.99%、99.9%、99.5%以上,出水CODCr、苯酚、F-、石油类、TOC均低于《污水综合排放标准》(GB8978-1996)中一级排放标准限值;同时可回收废水中苯酚,实现废水资源化。　氟苯　萃取　粒子群电催化　废水　资源化　　　　　　　　＊(2005033)0　、、、[1]。[2]HF(AHF),、CODCr、,,。、[3-4](),。1　1.1　废水水质及工艺流程,CODCr、、()、、pH(NaOH)9000～10000、2500～3000、1800～2000、420～490、3400～7600mgL。1。1　　1.1.1　35%,pH0.5～5,,CODCr,pHCODCr。1.1.2　(1∶1),()1∶0.5～1∶6,()CODCr。1∶4,10～55℃,()。1∶4,10～20℃,()1～10min,()。1.1.3　CaCO3,300～900rmin,30min,pH5～6,CaO,300rmin,5～6min,pH7～8,,。,,。1.1.4　,2.5～3.0V,20～120min14　　　200712256NOVELCIRCULATINGFLUIDIZEDBEDBIOREACTORFORNITROGENREMOVALUNDERDIFFERENTNITRIFIEDLIQUIDRECIRCULATIONRATESCuiYubo　LiuHongbo　BaiChunxue(7)…………………………………………………………………………………………………………………………………………Abstract　Anewbiologicalnitrogenremovalprocess———Thecirculatingfluidizedbedbioreactor(CFBBR)isdevelopedforsimultaneousremovalofnitrogenandorganicmatter.Thissystemiscomposedofanaerobicbed,aerobicbedandconnectingdevice.Influentandnitrifiedliquidfromaerobicbedenteranaerobicbedfromthebottomoftheanaerobicbed,completingtheremovalofnitrogenandorganicmatter.Thesystemperformanceundertheconditionsofdifferentinflowloadingsandnitrifiedliquidrecirculationratesrangingfrom200%to600%wasexamined.Fromtechnicalandeconomicpointofview,theoptimumnitrifiedliquidrecyclerateis400%.Withashortesttotalretentiontimeof2.5h(0.8hintheanaerobicbedand1.7hintheaerobicbed)andanitrifiedliquidrecirculationrateof400%basedontheinfluentflowrate,theaverageremovalefficienciesandeffluentconcentrationsoftotalnitrogenandsolubleCODCrarefoundtobe88%,95%and3.5mgL,16mgL,respectively.TheVSSconcentration,nitrificationrateanddenitrificationrateinthesystemarelessthan1gL,0.026-0.1g(g·d)and0.016～0.074g(g·d)respectively.Keywords　circulatingfluidizedbedbioreactor,nitrification,denitrificationandrecirculationrateRESEARCHONDESIGNOFMULTISTAGEAOSTEPFEEDBIOLOGICALNITROGENREMOVALPROCESSGaoJunfa　WangLi　GuanJiangetal(11)…………………………………………………Abstract　Thispaperreviewstheprincipleandcharacteristicsofstep-feedmultistageAObiologicalnitrogenremovalprocess,meanwhile,consultedwiththecurrentstatusofresearchinabroadandtheprojectapplicationexamples,someimportantfactorsregardingtheoperationanddesignoftheprocessarediscussed.Thestep-feedmultistageAObiologicalnitrogenremovalprocessdoesnotapplyinternalmixedliquidreturn,themorereactors,thehighernitrogenremovalrate,butthedesignandoperationoftheprocesswillbecomplexaswell.Thequantitiesofreactorinprojectapplicationareusually2～4.Thevolumeratiooftheanoxicsectiontotheoxicsectionis1∶1.5.Asforthree-step-feedmultistageAObiologicalnitrogenremovalprocess,whenthenitrogenremovalattherateof78%,sludgereturnonlyattherateof50%.Keywords　step-feed,multistageAOprocessandbiologicalnitrogenremovalTREATMENTOFFLUOBENZENEWASTEWATERBYPHYSICOCHEMICALMETHODSLiGuoping　QiuYang　XiaMingfangetal(14)………………………………………………………………………………………Abstract　Itwasstudiedthattheprocessconditionsoftreatingfluobenzenewastewaterwithacidification,extraction,inorganicfluorideremovalandelectrocatalysis.Atthesuitableconditions,theremovalratesofCODCr,phenol,F-andpetroleumareover99.2%,99.99%,99.9%,99.5%,theeffluentindexessuchasCODCr,phenol,F-,petroleumandTOCwerelowerthanth