低含量氨氮污水厌氧氨氧化影响因素研究付丽霞

[1]。、、、CANON[2-5]。、,、、[6]。AnaerobicammoniumoxidationANAMMOXDelft。1995DelftMulder、N2[7]。VandeGraafNO2-[8]。NH4+-NNO2--NNH4+-N、NO2--NN2[9]。Kuypers[10]。pH、。11.13L120cm1/31.25L。30～34℃。1。1Fig.1Experimentalapparatusandprocessschemechart11121.3000712.330100165d。TN0.17kg·m-3·d-1NO2--NNH4+-N100%93%。pH、。～18mg·L-1pH=8.0、30℃、TOC40mg·L-1。pHX703.1A1000-3770(2010)[e-mail]36420104TECHNOLOGYOFWATERTREATMENTVol.36No.4Apr.,201050DOI:10.16796/j.cnki.1000-3770.2010.04.0121.2．24hMLSSMLVSS27.7、17.7g·L-1MLSSMLVSS0.6391.000。1.31NH4ClNaNO22[11]。1.4、pHpHSSVSS[12]。22.1、30℃、pH7.5。。113dNO3--NS2-4.8、3mmol·L-1HRT24h。NH4ClS2-、NO3-、NH4+11.60.8。7d11dNH4+-N46dNH4+-N67%NO3--N。SO42-NO3--NNO3--NNH4+-N。52d。TN36h。NH4+-NNO2--N1mmol·L-1NH4+-NNO2--N80%NH4+-NNO3--N42d24hTN0.17kg·m-3·d-110dNO2--NNH4+-N100%93.04%NO3--NNO2--N、NH4+-N。2.2pH、。2.2.1pH30℃2mL1518mLNH4+-NNO2--N56mg·L-1MLSS2064mg·L-1pH6.5、7.0、7.5、8.0、8.5531pH。DO24h。2。2pH6.57.0pHpHpH81Tab.1Compositionofexperimentalwaterρ/mg·L-1KH2PO4CaCl2MgSO4·7H2OKHCO327.21361205001mL·L-11mL·L-12Tab.2Contentoftracedelementsinexperimentalwaterρ/mg·L-1EDTAFeSO4·7H2OEDTAZnSO4·7H2OCoCl2·6H2O2MnCl2·4H2OCuSO4·5H2ONa2MoO4·2H2ONiCl2·6H2ONa2SeO4·10H2OH3BO4500050001500043040990250220190210145169.8%72.9%pH8.552.6%63.9%。pH8。VanDeGraafpHpHFreeammoniaFAFreenitrousacidFNAHNO2[13]。FAFNAFAFNA(1)(2)[14]。ρ(FA)＝Mr(NH3)Ar(N)×ρ(NH4+-N)×10pHKbKw+10pH(1)ρ(FNA)＝Mr(NO2-)Ar(N)×ρ(NO2--NKa×10pH。(2)ρ(NH4+-N)ρ(NO2--N)MrArKbKW30℃Kb/KW=1.24×109Ka=0.505×10-3。pHFAFNA3。FAFNA75.7680.02868mg·L-1[15]。3pH6.57.0FNA2pHFNA。pH。2.2.22mL1818mL56mg·L-1pH8TOC0、40、80、120、140、250mg·L-163。DO。30℃24h。45。4560%TOC250mg·L-1。TOCTOC80mg·L-1。FuxC6.06.57.07.58.08.59.00102030405060020406080100
/mgL
/%
pH
2pHFig.2ChangofAmmonianitrogenunderdifferentpHconcentration3pHFAFNAFig.3EffectofpHonFAandFNAconcentration6.06.57.07.58.08.59.00.02.55.07.510.012.515.00.0000.0250.0500.0750.1000.1250.150
(FNA)/mgL
(FA)/mgLpH
4Fig.4Changofnitrogenunderdifferentglucoseinfluentconcentrations050100150200250020406080100120
(TOC)?/mgL
/mgL


5Fig.5Nitrogenremovalrateunderdifferentglucoseinfluentconcentrations050100150200250020406080100(TOC)/mgL
/%36452[16]。67。67TOC20%。TOC020mg·L-184.7%51.9%TOCTOC80mg·L-1。TOC80mg·L-1。TOC80mg·L-1。2.2.2、、3TOC250mg·L-12mL918mL56mg·L-1pH=7.6～8.23。30℃。24h。4ABCD3。3、。。3。。2.3pH、、3220、30℃pH37.5、8.0、8.530、40、80mg·L-1L6(2×32)。500mL220mL300mL14mg·L-120、30℃1h。MLSS1376mg·L-13v4。Kmf=mfkmf=Kmf/(mf)Rm=mkf。6Fig.6Changofnitrogenunderdifferentsodiuminfluentconcentrations

















(TOC)/mgL
/mgL


7Fig.7Nitrogenremovalrateunderdifferentsodiuminfluentconcentrations0200400600800020406080100(TOC)/mgL
/%3Tab.3Nitrogenremovalrateunderdifferentorganicmatterinfluentconcentrations/%TN91.340.924.122.589.610010030.977.264.268.519.4534NH4+-N3、pH、。。pH。4k1、k2、k330℃pH=8.5TOC40mg·L-1。pH=8.0TOC≤80mg·L-1。pH524h。5BA30℃pH=8.0TOC40mg·L-1。3pH8。TOC80mg·L-1。。。3。、。30℃pH=8.0TOC40mg·L-1。[1],.[J].,2006,32(9):30-33.[2]QiR,YangK,YuZX.TreatmentofcokeplantwastewaterbySNDfixedbiofilmhybridsystem[J].JournalofEnvironmentalSciences-China,2007,19(2):153-159.[3]VolckeEIP,LoccufierM,NoldusEJL,etal.OperationofaSHARONnitritationreactor:practicalimplicationsfromatheoreticalstudy[J].WaterScienceandTechnology,2007,56(6):145-154.[4]JossA,SalzgeberD,EugsterJ,etal.Full-scalenitrogenremovalfromdigesterliquidwithpartialnitritationandanammoxinoneSBR[J].EnvironmentalScienceandTechnology,2009,43(14):5301-5306.[5]Vazquez-PadinJR,PozoMJ,JarpaM,etal.TreatmentofanaerobicsludgedigestereffluentsbytheCANONprocessinanairpulsingSBR[J].JournalofHazardousMaterials,2009,166(1):336-334.[6]VanDongenU,JettenMS,VanLoosdrechtMC.TheSHARON-ANAMMOXprocessfortreatmentofammoniumrichwastewater[J].WaterScienceandTechnology,2001,44(1):153-160.[7]MulderA,VandeGraafAA,RobertsonLA,etal.Anaerobic/℃pHρ()/mg·L-1v/mg·g-1·h-11234562020203030307.58.08.57.58.08.504080408000.1680.1980.3200.4180.2710.396K1K2K3k1k2k3R6.8610.852.293.621.335.864.697.162.932.353.581.235.646.165.912.823.082.960.264Tab.4Orthogonalexperimentaldataofanaerobicammoniumoxidation5Tab.5Programandtheresultsofcomparativeexperiments/℃pHρ(TOC)/mg·L-1ρ/mg·L-1ρ/mg·L-1/%NH4+-NNO2--NNH4+-NNO2--NNH4+-NNO2--NAB30308.58.0404053.551.558.0257.0220.511.56.5885.30561.777.788.689.736454FACTORSAFFECTINGTHEANAMMOXPROCESSUNDERLOWAMMONIACONCENTRATIONFuLixia1,WuLibo1,ZhangYiran1,LongBin2(1.CollegeofEnvironmentalScienceandEngineering,NankaiUniversity,Tianjin300071,China;2.JiangxiJindalaiEnvironmentalProtectionResearchandDevelopmentCenterCompanyLimited,Nanchang330100,ChinaAbstract:Theanaerobicammoniumoxidation(ANAMMOX)reactorwassuccessfullytransitedstartingupinanupflowblanketfilter(UBF)for165days.TheANAMMOXwasfromtheautotrophicdenitrification.Afterthestart-upoftheANAMMOXreactor,thevolumetricloadingratewasupto0.17kg·m-3