AO工艺处理焦化废水研究陈劲松

　　　200927A/O＊陈劲松　文一波　王　凯　李天增(,　101102)　:研究A/O工艺处理焦化废水的运行过程与COD、氨氮的降解规律,结果表明,系统的启动期约为30d,工艺系统在提升负荷阶段COD与NH3-N去除率基本保持不变;满COD负荷运行阶段,COD与NH3-N的去除率分别为82.8%、97.3%;进出水总氰浓度分别13.57和0.78mg/L;工艺系统运行温度为28～30℃,总水力停留时间为142.5h,污泥回流比为100%,混合液回流比为400%。:焦化废水;A/O工艺;氨氮;总氰RESEARCHONCOKE-PLANTWASTEWATERTREATMENTBYA/OPROCESSChenJinsong　WenYibo　WangKai　LiTianzeng(BeijingSoundEnvironmentalProtectionGroup,Beijing101102,China)Abstract:TheoperationprocessofA/OprocessandthepropertyofCOD,NH3-Nremovalwasinvestigated.Theresultsshowedthatthestart-uptimeofthebioreactorsystemwasabout30d.Therewasahardlyvaria-tionoftheremovalratesofCODandammonianitrogenatatthephaseofincreasingCODload.AtthefullCODloadoperationphase,theremovalratesofCODandammonianitrogenconcentrationwere82.8%and97.3%respectively.Thetotalcyanideconcentrationoftheinfluentandeffluentwas13.57and0.78mg/L,respec-tively;Thetemperatureandhydraulicdetentiontimeoftheactivatedsludgesystemwasbetween28℃and30℃and142.5h,respectively;Thesludgerecycleratiowas100andthemixedliquorrecycleratiowas400.Keywords:coke-plantwastewater;A/Oprocess;ammonianitrogen;totalcyanide＊(20071D0900500324)。0　,,、、,、、、,[1-2]。0.002～0.015mg/L,,。0.1～0.2mg/L[3]。COD80%[4];,HCN50mg,KCN150～300mg,CN-0.3～0.5mg/L,[5]。18～20mg/L[6]。NH3-N521mg/L[7]。。,。A/O,COD、NH3-N。1　1.1　试验装置、,1。1-;2-;3-;4-;5-;6-;7-;8-;9-;10-;11-;12-;13-;14-;15-;16-。1　A/OA/O,251,50133DOI:10.13205/j.hjgc.2009.s1.114　　　200927m3。,,。1.2　操作方式,,,,。,,,,,,,4∶1。,100%。。1.3　进水水质,,,1。1　　　mg/L(pH)ρ(COD)ρ(NH3-N)ρ(PO43--P)ρ(S2-)ρ()pH2300～3500200～3101.0～8.090.0～120.0520.0～740.08.0～9.02　2.1　工艺系统启动试验结果,,。07111,115,1129。1121,3,1121-292.5。DO0.42.0mg/L,CODNH3-N23。2　COD23,3　,COD1100mg/L,NH3-N72mg/L,CODNH3-N,2474.34mg/L,;COD1300mg/L,NH3-N80mg/L,CODNH3-N,370,7.25mg/L,,MLVSS/MLSS0.51。,COD1460mg/L,NH3-N89.67mg/L,CODNH3-N,336,3.16mg/L,,MLVSS/MLSS0.60,。2.2　工艺系统提升COD负荷试验结果071130。1130-1251:1,126-91:0.6,1210-201:0.4,1221-291:0.2,142.5h,100%,400%。DO0.42.0mg/L。CODNH3-N45。4　CODCOD4、5,1:1,COD1702mg/L,NH3-N106mg/L,CODNH3-N34　　　2009275　COD,220,3.2mg/L,CODNH3-N87.1%、97.0%,;1:0.6,COD1959mg/L,NH3-N135mg/L,CODNH3-N,300,3.6mg/L,CODNH3-N84.7%、97.3%,;1:0.4,COD2284mg/L,NH3-N156mg/L,COD,NH3-N,430,4.6mg/L,CODNH3-N81.2%,97.1%,,,;1∶0.2,COD2570mg/L,NH3-N217mg/L,COD,NH3-N,400,6.1mg/L,CODNH3-N84.4%、97.2%,,,,COD。2.3　工艺系统满COD负荷时试验结果COD,071130-08123。28～30℃,142.5h,100%,400%。DO0.42.0mg/L。CODNH3-N67。6、7COD,COD3234.6mg/L,NH3-N327.8mg/L,CODNH3-N,557.4,8.7mg/L,CODNH3-N6　CODCOD7　COD82.8%、97.3%,,,,COD,,CODNH3-N,,,。734.2mg/L,0.38mg/L;13.57mg/L,0.78mg/L;94.5～121.4mg/L,8.02～10.0mg/L。3　1),,A/O,1,MLVSS/MLSS。2)A/O,142.5h,100%,400%,1:0.61:0.2,CODNH3-N,84.4%、97.2%,,,,COD。3)COD,A/O28～30℃,142.5h,100%,400%。COD(61)35　　　200927。100mg/L,。6　SV3　SBR30minTP,,100mg/L(),TP65.52%69.95%,;;;。[1],.[J].(),2007,12(4):46-49.[2],,.[M].:,1999:308-315.[3],.[J].,2007,27(1):951-261.[4],.[J].,2006,28(4):48-49.[5]ClarkT,StephensonT,PearcePA.Phosphorusremovalbychem-icalprecipitationinabiologicalaeratedfilter[J].WatRes,1997,31(10):2557-2563.[6],,.[J].,2006,26(3):409-415.[7]YuqiuWang,TianweiHan,ZeXu,etal.Optimizationofphos-phorusremovalfromsecondaryeffluentusingsimplexmethodinTianjin,China[J].JournalofHazardousMaterialsB,2005,121:183-186.[8],.[J].,2002,24(2):81-84.[9],,,etal.[J].,2007,1(5):20-24.　　361005　　(0592)2188132E-mail　[e-mail]2008-01-22(35)3234.6mg/L,NH3-N327.8mg/L,CODNH3-N,557.4,8.7mg/L,CODNH3-N82.8%、97.3%。COD,,COD,,CODNH3-N,,,。COD、,。[1].[D].:,1995:3-28.[2]ZhangMin,TayJH,QianYi,etal.Comparisonbetweenanaerobic-anoxic-oxicandanoxic-oxicsystemsforcokeplantwastewatertreatment[J].JournalofEnvironmentalEngineering,1997,9:879-880.[3],,,.[M].:,1983:17-18.[4]ZhangMin,TayJH,QianYi,etal.Cokeplantwastewatertreat-mentbyfixedbiofilmsystemforCODandNH3-Nremoval[J].Wat.Res,1998,32(2):519-527.[5],,,.[M].:2002:202-203.[6],,,.[J].,2002,52(5):22-24.[7]XuJinQiu,JiaJinPing,WangJingWei.Decompositionoforganiccompoundsincokeplantwastewaterbyultrasonicirradiationanditscombinedprocess[J].Chem.Res.Chineseu,2004,20(4):421—428.　　101102　　(010)60594937E-mail　[e-mail]2008-11-1461