分段进水SBR处理低CN值含盐废水的脱氮效果

SBRC/N刘山虎1，潘绵立2，赵伟1，王鸿1，王亚宜1(1．同济大学环境科学与工程学院污染控制与资源化研究国家重点实验室，上海200092;2．上海医药工业研究院药理评价研究中心，上海200040)针对低C/N值含盐废水利用传统生物脱氮工艺处理时存在有机碳源不足、脱氮效率低的问题，提出以优先利用原水中的可生物降解有机物和减少外加碳源为目的的分段进水SBR工艺。对比分析了5种不同进水方式下的脱氮效率、N2O释放量及转化率，结果表明:在外碳源充足的条件下，5种进水方式均可实现较好的脱氮效果，但进水比例为1∶2∶3的三段式进水脱氮过程中N2O的转化率较一段进水方式减少了约46%。在二段进水方式中，进水比例为1∶1的N2O转化率最高，达到了5．1%，而进水比例为1∶2的仅有2．5%。对比最后一次硝化结束时系统内的NO－x－N浓度，一、二、三段式的分别为41．5、23．3、19．7mg/L，因此通过分段进水可节省后续反硝化时间和反硝化外碳源需求量。可见，当处理低C/N值含盐废水时，采用适当的分段进水方式和进水比例，可在实现高效脱氮、降低运行成本的同时防止N2O的大量释放。分段进水SBR;低C/N值;含盐废水;N2OX703A1000－4602201305－0005－0551078283、5117832512QH1402400NitrogenRemovalEfficiencyofStep-feedSBRinTreatmentofLowC/NSalineWastewaterLIUShan-hu1PANMian-li2ZHAOWei1WANGHong1WANGYa-yi11．StateKeyLaboratoryofPollutionControlandResourceReuseSchoolofEnvironmentalScienceandEngineeringTongjiUniversityShanghai200092China2．CenterforPharmacologicalEvaluationShanghaiInstituteofPharmaceuticalIndustryShanghai200040ChinaAbstractLackofcarbonsourceandlownitrogenremovalefficiencyoccurredwhenconventionalbiologicalnitrogenremovalprocesseswereusedtotreatlowcarbontonitrogenratioC/Nsalinewastewater．Astep-feedsequencingbatchreactorSBRwasproposedtomakefulluseoftheinfluentcarbonsourceandreduceexternalcarbonsourceaddition．Fivedifferentstep-feedmodeswerecomparedintermsofnitrogenremovalefficiencyN2Oemissionandconversionrate．Theresultsshowedthathighnitrogenremovalefficiencywasachievedinallfivestep-feedmodeswhensufficientexternalcarbonsourcewasprovided．HowevertheN2Oconversionrateofthethree-stepmodewiththeinfluentflowratioof1∶2∶3reducedby46%comparedtothatoftheone-stepmode．Regardingtothetwo-stepmodethehighestN2Oconversionrateof5．1%wasobservedattheinfluentflowratioof1∶1andthelowestthatof2．5%occurredattheinfluentflowratioof1∶2．AdditionallyNO－x－Nwasaccumulatedattheend·5·第29卷第5期2013年3月中国给水排水CHINAWATER＆WASTEWATERVol．29No．5Mar．2013ofthelastaerobicstageandwasreducedfrom41．5mg/Lone-stepmodeto23．3mg/Ltwo-stepmodeand19．7mg/Lthree-stepmodeindicatingthattheexternalcarbonsourceanddenitrificationtimecouldbesaved．TakentogetherhighnitrogenremovalefficiencylowoperationcostandlowN2Oemissioncouldbeachievedusingstep-feedoperationalmodesinSBRwhentreatinglowC/Nratiosalinewastewater．Keywordsstep-feedSBRlowC/NratiosalinewastewaterN2O1。C、NP23C/N4。C/NN2O。Hiroki5COD/N＜3．5N2O20%～30%67．5g/LN2O2．85。C/NN2O。SBR78。Yang8SBRN2ON2OA/O50%。SBRC/NN2O。1材料和方法1.1。5LSBR10g/L12。10min、3h、2h、0．5h0．5h。90%、NO－2－N85%。MLVSS3800mg/LSRT25d。KH2PO422．0mg/LMgSO4·7H2O103．0mg/LCaCl210．0mg/LNaCl10．0g/LCH2OH0．2g/LCOD=300mg/LNH4Cl319．0mg/L0．3mL/L。C/N0．14g/LCOD=200mg/L。1.22．6L1．2L2．4L25±1℃。51、1∶2、1∶1、2∶11∶2∶3。1Fig．1Differentkindsofstep-feedmodes①N2OPHA。N2O。②1∶2、1∶12∶1N2O。·6·第29卷第5期中国给水排水．watergasheat．com③N2ON2OCODNH+4－N=66mg/LC/N=0、COD=300mg/LNH+4－N=60mg/LC/N=5COD=60mg/LNH+4－N=20mg/LC/N=3N2O。1.3Milli-pore0．45μm4℃。PHBPHV。NH+4－N、NO－3－N、NO－2－N、MLSSMLVSS9DO、pHDO、pHN2O10。PHBPHVOehmen11PHBPHVPHA。2结果与讨论2.1N2ON2O1。1N2OTab．1NitrogenremovalandN2Oreleaseunderdifferentfeedingmodes1∶21∶12∶1a/%2639383844N2O/mg·g－1VSS0．670．740．900．830．20N2O/mg·g－1VSS0．190．03b0．040．060．040．440．24bN2O/%4．12．55．13．22．2/h3332．52．5MLVSS/g·L－11．61．7/1．22．3/2．01．9/1．62．4/1．8/1．4NO－2－N/mg·L－132．920．421．519．717．7NO－3－N/mg·L－18．61．62．93．82N2ONH+4－NMLVSSNO－3－NNO－2－NabN2O。。15NO－x－N41．5mg/L23．3mg/L19．7mg/L。NO－x－NHRT、。1．69N2O46%。N2O①DO8mg/L240～300minDO0．5mg/L2N2ON2O②PHANO－x－N1．43mg/LPHA19mg/gVSS10mg/gVSS20mg/LCODWang10PHAN2O。2DOFig．2DOvariationswiththree-step-feedoperationalmode·7·．watergasheat．com刘山虎，等:分段进水SBR处理低C/N值含盐废水的脱氮效果第29卷第5期2.2CODNO－x－NDO。N2O1∶2N2O。12N2ONO－x－NN2ON2O。NO－2－NN2O。5NO－2－N80%1∶12∶1NO－2－N26．6mg/L24．8mg/L3N2O。3NO－2－NFig．3NO－2－Nvariationswithdifferenttwo-step-feedoperationalmodes2.3C/NN2ONO－2－NCODCOD。CODN2O。C/N=330～90N2ONO－2－N4。N2O。CODCODN2O。4N2OabcFig．4EffectofdifferentinfluentqualitiesonnitrogenremovalandN2Oemission3结论①。②SBRN2ON2O46%。③。1．J．2000161149－50．2AhmedMShayyaWHHoeyDetal．BrinedisposalfromreverseosmosisdesalinationplantsinOmanandtheUnitedArabEmiratesJ．Desalination20011332135－147．3．J．200828111－4．4．C/N·8·第29卷第5期中国给水排水．watergasheat．comJ．2009292225－230．5HirokiIKeisukeH．Nitrousoxideproductioninhigh-loadingbiologicalnitrogenremovalprocessunderlowCOD/NratioconditionJ．WaterRes2001353657－664．6．N2OJ．20093041079－1082．7．DO、ORP、pHSBRJ．2003232252－256．8YangQingLiuXiuhongPengChengyaoetal．N2Oproductionduringnitrogenremovalvianitritefromdo-mesticwastewatermainsourcesandcontrolmethodJ．EnvironSciTechnol200943249400－9406．9．4M．2002．10WangYayiGengJunjunRenZhongjiaetal．Effectofanaerobicreactiontimeondenitrifyingphosphorusre-movalandN2OproductionJ．BioresourTechnol2011102105674－5684．11OehmenAKeller-LehmannBZengRJetal．Optimis-ationofpoly-β-hydroxyalkanoateanalysisusinggaschro-matographyforenhancedbiologicalphosphorusremovalsystemsJ．JChromatogrA200510701/2131－136．12．N2OJ．20103091－9．1987－。[e-mail]櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆櫆2012－09－20(上接第4页)byproductformationfromchlorineandalternativedisin-fectantsJ．WaterRes20074181667－1678．3PlewaMJWagnerEDRichardsonSDetal．Chemicalandbiologicalcharacterizationofnewlydis