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ENVIRONMENTAL BIOTECHNOLOGYOne-stage partial nitritation/anammox at15°Con pretreated sewage:feasibility demonstration at lab-scale Haydée De Clippeleir&Siegfried E.Vlaeminck&Fabian De Wilde&Katrien Daeninck&Mariela Mosquera&Pascal Boeckx&Willy Verstraete&Nico BoonReceived:26November2012/Revised:28January2013/Accepted:30January2013#Springer-Verlag Berlin Heidelberg2013Abstract Energy-positive sewage treatment can beachieved by implementation of oxygen-limited autotrophicnitrification/denitrification(OLAND)in the main water line,as the latter does not require organic carbon and thereforeallows maximum energy recovery through anaerobic diges-tion of organics.To test the feasibility of mainstreamOLAND,the effect of a gradual temperature decrease from29to15°C and a chemical oxygen demand(COD)/Nincrease from0to2was tested in an OLAND rotatingbiological contactor operating at55–60mg NH4+–NL−1 and a hydraulic retention time of1h.Moreover,the effectof the operational conditions and feeding strategies on thereactor cycle balances,including NO and N2O emissionswere studied in detail.This study showed for the first timethat total nitrogen removal rates of0.5g NL−1day−1can bemaintained when decreasing the temperature from29to15°Cand when low nitrogen concentration and moderate CODlevels are treated.Nitrite accumulation together with elevatedNO and N2O emissions(5%of N load)were needed to favoranammox compared with nitratation at low free ammonia(<0.25mg NL−1),low free nitrous acid(<0.9μg NL−1),and higher DO levels(3–4mg O2L−1).Although the total nitrogen removal rates showed potential,the accumulation of nitrite and nitrate resulted in lower nitrogen removal efficiencies (around40%),which should be improved in the future. Moreover,a balance should be found in the future between the increased NO and N2O emissions and a decreased energy consumption to justify OLAND mainstream treatment. Keywords Energyself-sufficient.Nitrospira.Nitricoxide. Nitrous oxide.DeammonificationIntroductionCurrently,around40full-scale one-stage partial nitrita-tion/anammox plants are implemented to treat highly loaded nitrogen streams devoid in carbon(Vlaeminck et al.2012). This process,known under the acronyms oxygen-limited autotrophic nitrification/denitrification(OLAND)(Kuai and Verstraete1998),deammonification(Wett2006),com-pletely autotrophic nitrogen removal over nitrite(Third et al. 2001),etc.,showed highly efficient and stable performance when treating digestates from sewage sludge treatment plants and industrial wastewaters(Wett2006;Abma et al. 2010;Jeanningros et al.2010).For clarity,one-stage partial nitritiation/anammox processes will be referred to as OLAND in this work.From an energy point of view,the implementation of the OLAND process for the treatment of sewage sludge digestate decreased the net energy consump-tion of a municipal wastewater treatment plant(WWTP)by 50%,with a combination of a lower aeration cost in the side stream and the opportunity to recover more organics from the mainstream(Siegrist et al.2008).Moreover,when co-digestion of kitchen waste was applied,an energyneutral Electronic supplementary material The online version of this article(doi:10.1007/s00253-013-4744-x)contains supplementary material,which is available to authorized users.H.De Clippeleir:S.E.Vlaeminck:F.De Wilde:K.Daeninck:M.Mosquera:W.Verstraete:N.Boon(*)Laboratory for Microbial Ecology and Technology(LabMET),Ghent University,Coupure Links653,9000Gent,Belgiume-mail:Nico.Boon@UGent.beP.BoeckxLaboratory of Applied Physical Chemistry(ISOFYS),Ghent University,Coupure Links653,9000Gent,BelgiumAppl Microbiol BiotechnolDOI10.1007/s00253-013-4744-xWWTP was achieved(Wett et al.2007).To fully recover the potential energy present in wastewater,a first idea of a new sustainable wastewater treatment concept was reported (Jetten et al.1997).Recently,a“ZeroWasteWater”concept was proposed which replaces the conventional activated sludge system by a highly loaded activated sludge step (A-step),bringing as much as organic carbon(chemical oxygen demand(COD))as possible to the solid fraction, and a second biological step(B-step)removing the residual nitrogen and COD with a minimal energy demand (Verstraete and Vlaeminck2011).Subsequently,energy is recovered via anaerobic digestion of the primary and sec-ondary sludge.For the B-step in the main line,OLAND would potentially be the best choice as this process can work at a low COD/N ratio,allowing maximum recovery of COD in the A-step.Moreover,it was calculated that if OLAND is implemented in the main water treatment line and a maximum COD recovery takes place in the A-step,a net energy gain of the WWTP of10Wh inhabitant equivalent (IE)−1day−1is feasible(De Clippeleir et al.2013).To allow this energy-positive sewage treatment,OLAND has to face some challenges compared with the treatment of highly loaded nitrogen streams(>250mg NL−1).A first difference is the lower nitrogen concentration to be removed by OLAND.Domestic wastewater after advanced concen-tration will still contain around30–100mg NL−1and113–300mg CODL−1(Metcalf and Eddy2003;Tchobanoglous et al.2003;Henze et al.2008).High nitrogen conversion rates(around400mg NL−1day−1)by the OLAND process can be obtained at nitrogen concentrations of30–60mg N L−1and at low hydraulic retention times(HRT)of1–2h(De Clippeleir et al.2011).A second challenge is the low tem-perature at which OLAND should be operated(10–15°C compared with34°C).Several studies already described the effect of temperature on the activity of the separate micro-bial groups(Dosta et al.2008;Guo et al.2010;Hendrickx et al.2012).Only a few studies showed the long-term effect of a temperature decrease below20°C on the microbial bal-ances of anoxic and aerobic ammonium-oxidizing bacteria (AnAOB and AerAOB)and nitrite-oxidizing bacteria (NOB)at nitrogen concentrations above100mg NL−1 (Vazquez-Padin et al.2011;Winkler et al.2011).However, the combination of low temperature and low nitrogen con-centration was never tested on a co-culture of AerAOB, AnAOB,and NOB before.At temperatures around15°C, maintaining the balance between NOB and AnAOB and the balance between NOB and AerAOB will get more challeng-ing since the growth rate of NOB will become higher than the growth rate of AerAOB(Hellinga et al.1998). Therefore,it will not be possible to wash out NOB based on overall or even selective sludge retention.The third and main challenge in this application will therefore be the suppression of NOB at temperature ranges of10–20°C and at nitrogen concentration ranges of30–60mg NL−1 (low free ammonia and low nitrous acid),which was not shown before.A final fourth challenge will include the higher input of organics at moderate levels of90–240mg biodegradable CODL−1in the wastewater.Depending on the raw sewage strength,COD/N ratios between2and3are expected after the concentration step,which is on the edge of the described limit for successful OLAND(Lackner et al. 2008).The presence of organics could result in an extra competition of heterotrophic denitrifiers with AerAOB for oxygen or with AnAOB for nitrite or organics,since certain AnAOB can denitrify consuming organic acids (Kartal et al.2007).In this study,the challenges2to4,were evaluated in an OLAND rotating biological contactor(RBC).This reactor at 29°C was gradually adapted over24,22,and17to15°C under synthetic wastewater conditions(60mg N L−1, COD/N of0).Additionally,the COD/N ratio of the influent was increased to2by supplementing NH4+to diluted sewage to simulate pretreated sewage.The effect of the operational conditions and feeding strategies on the reactor cycle balan-ces,including gas emissions and microbial activities were studied in detail.An alternative strategy to inhibit NOB activity and as a consequence increase AnAOB activity at low temperatures based on NO production was proposed. Materials and methodsOLAND RBCThe lab-scale RBC described by De Clippeleir et al.(2011) was further optimized at29°C by an increase in the influent nitrogen concentration from30to60mg NL−1and a limitation of the oxygen input through the atmosphere by covering the reactor before this test was started.The reactor was based on an air washer LW14(Venta,Weingarten, Germany)with a rotor consisting of40discs interspaced at 3mm,resulting in a disc contact surface of1.32m2.The reactor had a liquid volume of2.5L,immersing the discs for 55%.The latter was varied over the time of the experiment. The reactor was placed in a temperature-controlled room. The DO concentration was not directly controlled.In this work,continuous rotation was applied at a constant rotation speed of3rpm,which allowed mixing of the water phase. RBC operationThe RBC was fed with synthetic wastewater during phases I to VII.From phase VIII onwards,the COD/N was gradually increased(phases VIII–X)to2(phases XI–XIII).The syn-thetic influent of an OLAND RBC,consisted of(NH4)2SO4 (55–60mg NL−1),NaHCO3(16mg NaHCO3mg−1N),andAppl Microbiol BiotechnolKH2PO4(10mg PL−1).Pretreated sewage was simulated by diluting raw sewage of the communal WWTP of Gent, Belgium(Aquafin).The raw wastewater after storage at 4°C and settlement contained23–46mg NH4+–NL−1, 0.2–0.4mg NO2−–NL−1,0.4–2.7mg NO3−–NL−1,23–46mgKjeldahl–NL−1,3.8–3.9mg PO43−–PL-1,26–27mg SO42−–S L−1,141–303mg COD tot L−1,and74–145mg COD sol L−1.The raw sewage was diluted by factors2–3to obtain COD values around110mg COD tot L−1and by addition of(NH4)2SO4to obtain final COD/N values around2.The reactor was fed in a semi-continuous mode:two periods of around10min/h for phases I–XI and one period of20min/h for phases XII and XIII.The influent flow range varied from47to65Lday−1and the reactor volume from3.7to2.5L(during78and55% submersion,respectively).Corresponding HRTare displayed in Tables1and2.Reactor pH,DO,and temperature were daily monitored and influent and effluent samples were taken at least thrice a week for ammonium,nitrite,nitrate,and COD analyses. Detection of AerAOB,NOB,and AnAOB with FISHand qPCRFor NOB and AnAOB,a first genus screening among the most commonly present organisms was performed by fluo-rescent in-situ hybridization(FISH)on biomass of days1 (high temperature)and435(low temperature and COD presence).A paraformaldehyde(4%)solution was used for biofilm fixation,and FISH was performed according to Amann et al.(1990).The Sca1309and Amx820probes were used for the detection of Cand.Scalindua and Cand. Kuenenia&Brocadia,respectively,and the NIT3and Ntspa662probes and their competitors for Nitrobacter and Nitrospira,respectively(Loy et al.2003).This showed the absence of Nitrobacter and Scalindua(Table S1in the Electronic supplementary material(ESM)).Biomass sam-ples(approximately5g)for nucleic acid analysis were taken from the OLAND RBC at days1,60,174,202,306,385, 399,and413of the operation.DNA was extracted using FastDNA®SPIN Kit for Soil(MP Biomedicals,LLC), according to the manufacturer’s instructions.The obtained DNA was purified with the Wizard®DNA Clean-up System (Promega,USA)and its final concentration was measured spectrophotometrically using a NanoDrop ND-1000spec-trophotometer(Nanodrop Technologies).The SYBR Green assay(Power SyBr Green,Applied Biosystems)was used to quantify the16S rRNA of AnAOB and Nitrospira sp.and the functional amoA gene for AerAOB.The primers for quantitative polymerase chain reactions(qPCR)for detection of AerAOB,NOB,and AnAOB were amoA-1F–amoA-2R (Rotthauwe et al.1997),NSR1113f–NSR1264r(Dionisi et al. 2002),and Amx818f–Amx1066r(Tsushima et al.2007),re-spectively.For bacterial amoA gene,PCR conditions were: 40cycles of94°C for1min,55°C for1min,and60°C for 2min.For the amplification of Nitrospira sp.16S rRNA gene, 40cycles of95°C for1min,50°C for1min,and60°C for 1min were used while for AnAOB16S rRNA the PCR temperature program was performed by40cycles of15s at 94°C and1min at60°C.Plasmid DNAs carrying NitrospiraTable1Effect of temperature decrease on the operational conditions and performance of OLAND RBC reactorPhase I II III IV V VI VIIPeriod(days)1–2122–3536–6162–210210–263263–274275–306 Immersion level(%)78787878557855 Temperature(°C)29±224±122±0.617±1.216±0.915±0.814±0.4 Operational conditionsDO(mg O2L−1) 1.1±0.2 1.3±0.2 1.4±0.1 1.7±0.3 2.8±0.4 2.4±0.2 3.1±0.2 pH(−)7.5±0.17.5±0.17.5±0.17.6±0.17.7±0.17.7±0.17.8±0.1 HRT(h) 1.85±0.04 1.84±0.09 1.73±0.04 1.86±0.11 1.09±0.02 1.57±0.02 1.09±0.02 FA(mg NL−1)0.35±0.180.36±0.180.34±0.140.36±0.130.25±0.160.33±0.170.13±0.04 FNA(μg NL−1)0.3±0.10.3±0.20.4±0.20.4±0.10.9±0.40.6±0.10.9±0.2 PerformanceTotal N removal efficiency(%)54±552±549±934±936±936±942±4 Relative NO3−prod(%of NH4+cons a)7±17±17±114±618±916±321±4 Relative NO2−accum(%of NH4+cons)2±43±45±515±530±826±631±5 AerAOB activity(mg NH4+–NL−1day−1)267±38267±49260±52260±53811±229460±44986±71 NOB activity(mg NO2–NL−1day−1)0±00±00±09±1260±9420±585±25 AnAOB activity(mg N tot L−1day−1)412±38403±37368±76248±67448±117305±74529±75DO dissolved oxygen,HRT hydraulic retention time,F A free ammonia,FNA free nitrous acid,cons consumption,prod production,accum accumulation,tot totala NH4+consumption is corrected for nitrite accumulationAppl Microbiol Biotechnoland AnAOB16S rRNA gene and AerAOB functional AmoA gene,respectively,were used as standards for qPCR.All the amplification reactions had a high correlation coefficient (R2>0.98)and slopes between−3.0and−3.3.Detailed reactor cycle balancesFor the measurements of the total nitrogen balance,including the NO and N2O emissions,the OLAND RBC was placed in a vessel(34L)which had a small opening at the top(5cm2).In this vessel,a constant upward air flow(around1ms−1or0.5L s-1)was generated to allow calculations of emission rates.On the top of the vessel(air outlet),the NO and N2O concentra-tion was measured,off-and online,respectively.NH3emis-sions were negligible in a RBC operated at about2mg NH3–NL−1(Pynaert et al.2003).Since FA levels in the currentstudy are about ten times lower,NH3emissions were not included.In the water phase,ammonium,nitrite,nitrate,hy-droxylamine(NH2OH),N2O,and COD concentrations were measured.Moreover,DO concentration and pH values were monitored.The air flow was measured with Testo425hand probe(Testo,Ternat,Belgium).Chemical analysesAmmonium(Nessler method)was determined according to standard methods(Greenberg et al.1992).Nitrite and nitrate were determined on a761compact ion chromatograph equipped with a conductivity detector(Metrohm,Zofingen, Switzerland).Hydroxylamine was measured spectrophoto-metrically(Frear and Burrell1955).The COD was determined with NANOCOLOR®COD1500en NANOCOLOR®COD 160kits(Macherey-Nagel,Düren,Germany).The volumetric nitrogen conversion rates by AerAOB,NOB,and AnAOB were calculated based on the measured influent and effluent compositions and the described stoichiometries,underestimat-ing the activity of AnAOB by assuming that all COD removed was anoxically converted with nitrate to nitrogen gas (Vlaeminck et al.2012).DO and pH were measured with respectively,a HQ30d DO meter(Hach Lange,Düsseldorf, Germany)and an electrode installed on a C833meter (Consort,Turnhout,Belgium).Gaseous N2O concentrations were measured online at a time interval of3min with a photo-acoustic infrared multi-gas monitor(Brüel&Kjær, Model1302,Nærem,Denmark).Gas grab samples were taken during the detailed cycle balance tests for NO detec-tion using Eco Physics CLD77AM(Eco Physics AG, Duernten,Switzerland),which is based on the principle of chemiluminescence.For dissolved N2O measurements,a1-mL filtered(0.45μm)sample was brought into a7-mL vacutainer(−900hPa)and measured afterwards by pressure adjustment with He and immediate injection at21°C in a gas chromatograph equipped with an electron capture detector (Shimadzu GC-14B,Japan).Table2Effect of COD/N increase on the operational conditions and performance of OLAND RBC reactorPhase VIII IX X XI XII XIIIPeriod(days)355–361362–369370–374375–406407–421422–435 Immersion level(%)555555555555COD/N(-)0.51 1.5222 Feeding regime(pulsesh−1)222211 Operational conditionsDO(mg O2L−1) 2.9±0.3 2.5±0.6 2.4±0.3 3.0±0.7 3.6±0.3 3.2±0.3 pH(−)7.8±0.027.7±0.17.6±0.027.6±0.17.6±0.27.6±0.1 HRT(h) 1.06±0.11 1.03±0.020.92±0.020.94±0.05 1.10±0.05 1.06±0.2 FA(mg NL−1)0.10±0.050.04±0.050.15±0.050.21±0.100.23±0.120.04±0.02 FNA(μg NL−1)0.4±0.10.2±0.20.2±0.010.3±0.10.2±0.10.6±0.2 PerformanceTotal N removal efficiency(%)36±545±1823±328±623±1342±3 Relative NO3−prod(%of NH4+cons a)42±543±1263±250±662±1846±6 Relative NO2−accum(%of NH4+cons)20±410±105±18±37±413±6 AerAOB activity(mg NH4+–NL−1day−1)592±15446±31238±28352±73289±138600±204 NOB activity(mg NO2−–NL−1day−1)257±19294±81465±60352±84427±115394±76 AnAOB activity(mg N tot L−1day−1)385±86452±205262±39355±73281±159481±73COD removal rates were negligible in all phasesDO dissolved oxygen,HRT hydraulic retention time,F A free ammonia,FNA free nitrous acid,cons consumption,prod production,accum accumulation,tot totala NH4+consumption is corrected for nitrite accumulationAppl Microbiol BiotechnolResultsEffect of temperature decreaseDuring the reference period (29°C),a well-balanced OLAND performance (Fig.1;Table 1)was reached with minimal nitrite accumulation (2%)and minimal nitrate production (7%).This was reflected in an AerAOB/AnAOB activity ratio of 0.6(Table 1,phase I).The total nitrogen removal rate was on average 470mg N L −1day −1or 1314mg Nm −2day −1,and the total nitrogen removal efficiency was 54%.Decreasing the temperature from 29to 24°C and further to 22°C over the following 40days,did not result in anysignificant changes of the operational conditions (Table 1;phases I –III),performance of the reactor (Fig.1)or abun-dance of the bacterial groups (qPCR;Fig.S1in the ESM ).However at 17°C,a decrease in total nitrogen removal efficiency was observed (Table 1;phase IV).An imbalance between the AerAOB and the AnAOB was apparent from a stable AerAOB activity yet a declining AnAOB activity.Moreover,NOB activity was for the first time detected in spite of free ammonia (FA)and free nitrous acid (FNA)con-centrations did not change (Table 1;phase IV).Moreover,no significant differences in abundance of NOB,AerAOB,and AnAOB could be detected with qPCR (Fig.S1in the ESM ).However,DO concentrations started to increase during that period from 1.4to 1.7mg O 2L −1.As the availabilityofFig.1Phases I –VII:effect of temperature decrease on the volumetric rates (top )and nitrogen concentrations (bottom )Appl Microbiol Biotechnoloxygen through the liquid phase did not seem to be satisfac-tory to counteract the decrease in ammonium removal effi-ciency,the immersion level was lowered to55%to increase the availability of oxygen through more air-biofilm contact surface.Consequently,the volumetric loading rate increased (factor1.7)due to the decrease in reactor volume(day210, Fig.1).This action allowed higher ammonium removal effi-ciencies due to higher AerAOB activities(factor3).AnAOB activity increased with a similar factor as the volumetric loading rate(1.8compared with1.7)consequently resulting in an increased imbalance between these two groups of bac-teria(Table1;phase V).Moreover,although the FNA in-creased with a factor2,the NOB activity increased with a factor7,resulting in a relative nitrate production of30% (Table1;phase V).As NOB activity prevented good total nitrogen removal efficiencies,the immersion level was in-creased again to78%(day263;Fig.1).This resulted indeed in a lower NOB activity(Table1;phase VI).However,also the AerAOB activity decreased with the same factor,due to the lower availability of atmospheric oxygen.Therefore,the reactor was subsequently operated again at the lower immer-sion level(55%)to allow sufficient aerobic ammonium conversion.The latter allowed a stable removal efficiency of 42%.The AnAOB activity gradually increased to a stable anoxic ammonium conversion rate of529mg NL−1day−1. During the synthetic phase,no changes in AerAOB, AnAOB,and NOB abundance were measured with qPCR (Fig.S1in the ESM).The effluent quality was however not optimal as still high nitrite(around15mg NL−1)and nitrate (around13mg NL−1)levels were detected.Effect of COD/N increaseThe synthetic feed was gradually changed into pretreated sewage by diluting raw sewage and adding additional nitro-gen to obtain a certain COD/N ratio.During the first3weeks of this period(Fig.2),the COD/N ratio was gradually increased from0.5to2.Due to the short adaptation periods (1week per COD/N regime),the performance was unstable (Fig.2;Table2,phases VIII–XI).Compared with the end of the synthetic period(phase VII),operation at a COD/N ratio of2(phase XI)resulted in a sharp decrease in nitrite accu-mulation(Fig.2)and an increase in the ammonium and nitrate levels.This indicated increased NOB activity(factor 4),decreased AerAOB(factor3)and decreased AnAOB (factor2)activity(Tables1and2).To allow higher nitrogen removal rates,the HRT was increased from0.94to1.1h,by decreasing the influent flow rate.Moreover,the feeding regime was changed from two pulses of10min in1h to one period of20min/h.These actions did not significantly decrease the effluent nitrogen concentration(Fig.2)and did not influence the microbial activities(Table2,phase XII). Therefore the loading rate was again increased to the levels before phase XII.However,the single-pulse feeding wasmaintained.This resulted in high ammonium removal effi-ciencies and therefore low ammonium effluent concentra-tion around dischargeable level(4±1mg NH4+–NL−1; Fig.2).Nitrate and nitrite accumulation were not counter-acted by denitrification as only0.02mg CODL−1day−1wasremoved.Therefore,nitrite and nitrate levels were still toohigh to allow effluent discharge.The total nitrogen removalefficiency(42%)and rate(549±83mg NL−1day−1or1,098±106mgNm−2day−1)at COD/N ratios of2wassimilar as during the synthetic period(phase VII).Comparedwith the reference period at29°C,the total nitrogen removalrate did not changed significantly(470±43versus549±83mgNL−1day−1at high and low temperatures,respectively).The22%lowered removal efficiency was merely due to anincreased nitrogen loading rate.Nitratation and NO/N2O emissionsAt the end of the synthetic phase(phase VII)and the end ofthe experiment(phase XIII),the total nitrogen balance of thereactor was measured.A total nitrogen balance was obtainedby measuring all nitrogen species(NH4+,NO2−,NO3−,NH2OH,and N2O)in the liquid phase and N2O and NO inthe gas phase.A constant air flow,diluting the emitted N2Oand NO concentrations was created over the reactor tomeasure gas fluxes over time.The effect of the loading rate,feeding pattern,and concentration of nitrite and ammoniumon the total nitrogen balance in the reactor were tested(Table3).NH2OH measurements showed low concentra-tions(<0.2mg NL−1)in all tests,making it difficult to linkthe profiles with the N2O emission.Lowering the loading rate by increasing the HRT(Table3,test B)increased the DO values and allowed higherDO fluctuations over time at synthetic conditions.Moreover,NOB activity increased significantly resultingin lower total nitrogen removal efficiencies and high levelsof nitrate in the effluent(Table3,test B).The relative N2Oemissions did not change and were relatively high(6%of Nload).However,the concentration of N2O in the liquid andin the gas phase decreased with a factor2(Table3).When pretreated sewage was fed to the reactor,theOLAND RBC was operated at lower nitrite concentration,while similar ammonium and nitrate concentrations wereobtained(Table3,test C).The lower nitrite concentrationshowever did not result in lower N2O emission rates.Whenthe feeding regime was changed to a more continuous-likeoperation(4pulses/h),the N2O emission increased signifi-cantly,while NO emission remained constant(Table3,testD).Due to the lower ammonium removal efficiency(65compared with81%),but similar relative nitrite and nitrateaccumulation rate,the total nitrogen removal efficiencydecreased.Appl Microbiol BiotechnolWhen a nitrite pulse was added just after feeding,about 20mg NO 2−–NL −1was obtained in the reactor.This did increase the NO and N 2O emissions significantly (p <0.05)compared with the same feeding pattern (Table 3,tests C –E).Although similar constant total nitrogen removal efficien-cies were obtained during this operation,a significant (p <0.05)decrease in the relative nitrate production was observed.The latter was mainly caused by a global increase in AnAOB activity.In the last test (F),the influent ammo-nium concentration was doubled,leading to higher ammo-nium and also FA concentrations (1±0.4mg N L −1compared with 0.1±0.4mg NL −1).Due to overloading of the system,the total nitrogen removal efficiency decreased.However,at these conditions a lower relative nitrate pro-duction was obtained;due to a decrease in NOB and in-crease in AnAOB activity (Table 3,test F).Together with this,increased NO and N 2O emissions were observed.As the influence of the nitrogen loading and DO concentration could be considered minor in this test range (Fig.S2in the ESM ),these tests show a relation between increased NO emissions and decreased relative nitrate productions (Table 3).When the activity during the feeding cycle was studied in more detail,it could be concluded that the highest nitrogen conversion rates took place during the feeding period,which was characterized by a high substrate availability and high turbulence (Fig.3).As the HRT is only 1h,the reactor volume is exchanged in 20min.During this phase,ammo-nium increased,while nitrite and nitrate concentrations de-creased due to dilution (Figs.S3,S4,and S5in the ESM ).The NOB/AnAOB ratio was around 1,which means that NOB were able to take twice as much nitrite thanAnAOBFig.2Phases VIII –XIII:effect of COD/N increase on the volumetric rates (top )and nitrogen concentrations (bottom ).Data during the N balance tests (days 424–431)were not incorporated in the figure but are shown in Table 3Appl Microbiol BiotechnolTable 3Operational parameters and nitrogen conversion rates during the six different RBC operations which differ from feeding composition and feeding regime (volume at 2.5L and 50%immersion of the discs,days 307–309for synthetic feed,and days 424–431)Reactor phaseVII (synthetic)XIII (pretreated sewage)Test A a B C a D E -F Additive––––NO 2−NH 4+Feeding regime (pulses/h)221411Total N loading rate (mg NL −1day −1)1,1695851,3401,5541,7372,718Temperature water (°C)15±0.316±0.2*14±0.415±0.1*16±0.1*15±0.4DO (mg O 2L −1) 2.9±0.1 3.7±0.6* 4.0±0.1 3.2±0.1* 3.3±0.1* 3.2±0.1*pH (-)7.6±0.067.6±0.057.6±0.047.6±0.017.6±0.027.8±0.02*Ammonium out (mg NL −1)9±1 1.4±1*11±319±3*12±158±4*Nitrite out (mg NL −1)14±213±16±16±0.418±2*9±0.3*Nitrate out (mg NL −1)17±337±6*18±216±1*18±0.420±0.4NH 4+oxidation rate (mg NL −1day −1)895±22509±2*1,051±73957±891,053±161,285±93*Relative nitrite accumulation (%)25±320±1*14±315±18±4*15±1Relative nitrate production (%)36±876±6*48±147±342±2*34±3*Total efficiency (%)38±417±4*35±328±4*32±227±4*AerAOB activity (mg NH 4+–NL −1day −1)658±88469±17*827±44781±57795±30938±46*NOB activity (mg NO 2−–NL −1day −1)174±59299±28*375±38342±24*362±13277±18*AnAOB activity (mg N tot L −1day −1)205±3849±13*234±20218±29263±15*354±49*N 2O in liquid (μg NL −1)64±4630±22*78±12104±29*61±1374±4NO emission (mg Nday −1)0.53±0.03n.d.0.66±0.060.74±0.08 1.65±0.18*0.82±0.1*N 2O emission (mg Nday −1)151±2893±23*170±19179±6*274±37*202±18*%N 2O emission on loading5.1±1.06.4±1.6*5.0±0.64.5±0.2*6.2±0.8*3.0±0.3*aReference period for synthetic and pretreated sewage*p <0.05,significant differences compared with referenceperiod Fig.3Detailed NO/N 2Omonitoring during the reference test (Table 3,test C)and when nitrite was pulsed (Table 3,test E)and effect on AerAOB,AnAOB,and NOB activity during the different phases of the feeding cycle.Significant differences in AerAOB,AnAOB,NOB,and NO/N 2O concentration compared with the reference period areindicated with asterisks ,circles ,double quotation mark ,and plus sign ,respectivelyAppl Microbiol Biotechnol。

污水处理外文翻译带原文

Study on Disinfection and Anti –microbial Technologies for Drinking WaterZHU Kun, FU Xiao Yong(Dept. of Environmental Engineering, LAN Zhou Railway University, LAN Zhou 730070, China)Abstract: Disinfection by-products produced by the reaction between chlorine and dissolved organic compounds and other chemicals are considered as a worrying problem in the drinking water treatment process since a series of mutagenic carcinogen substances are formed including trihalomethanes (THMs). Among the tested disinfectants(chlorine , ozone , chlorine dioxide , potassium permanganate , chloramines and hydrogen peroxide etc. ) , chlorine dioxide has proved to be the most feasible and effective oxidant for drinking water treatment and removal of pathogens due to its oxidation efficiency , low cost and simple way of utilization. A series of experiments indicate that chlorine dioxide can significantly restrain production of trihalomethanes (THMs) and control bacteria growth particularly for Cryptosporidium oocysts. The experiments verified that both ozone and chlorine dioxide are absolutely vital to ensure thtion of water storage are destroyed. The paper discusses oxidation capacity of chlorine dioxide, especially for removing petroleum compounds, which is affected by reaction time, gas injection way, and pH of treated water.Key words: disinfection; oxidants; water treatment; pathogens; chlorine dioxideCLC number: X523 Document code: A1 IntroductionChemical and filtration processes are two main methods used in China for treating drinking water meanwhile UV radiation has been used successfully for water treatment with relatively low flow rate. On the individual family level, usually chemical treatment is a feasible alternative. The following guidelines exist for the selection of suitablal of contaminants should be done by decomposition, evaporation or precipitation etc, to eliminate or decrease the toxicity, oxidants or reactionby-products should not be harmful to human health, and the purification processes should be practical and economical. The objective of this paper is to evaluate and discuss available disinfectants for drinking water treatment. The different disinfectants are compared regarding purification efficiencies and application approaches.2 Comparison ofO3 > ClO2 > HOCl > OCl - > NHCl2 > NH2ClReferring to Fiessinger′s [2] suggestion, the properties of these disinfectants are compared in Tab. 1. Chlorine is shown to be an excellent disinfectant to prevent waterborne diseases such as typhoid fever over long periods. Chlorine reacts not only within oxidation, but also by electrophilic substitution to produce a variety of chlorinated organic by - products, particularly trihalomethanes (THMs) and other mutagens. Here THMs mainly refer to chloroform, bromoform, dibromochloromathane and bromodichloromathane etc. Since the 1970`s, the usage of Cl2 in drinking water disinfection has been questioned with ozone being substituted as the preferred disinfectant in the water supply plants. But , ozone could not be introduced to the rural farmer community due to its high costs and short half - life (15～20 min. ) . As with other disinfectants, ozonation also leads to formation of organic by - product s such as aldehyde, ketones, and carboxylic acids, and also mutagenicity may be induced if bromic anion exists.Tab. 1 Comparison of various oxidants- no effect ; + little effect ; + + effect ; + + + largest effectMany studies have pointed out that disinfection is absolutely vital to ensure that any microorganisms arising from fecal contamination of water storage are destroyed. The selection of the available disinfectant s must concern to reduce risk from microbial contamination of drinking water and the potential increase in risk from chemical contamination that result from using any of the disinfectant s. The biocidal efficiency of commonly used disinfectants - ozone, chlorine dioxide, chlorine and chloramines are ranked almost with the same order as the oxidizing capacity, but the stability of those are following the order as [3]:Chloramines > Chlorine dioxide > Chlorine > Ozone3 Purification of organic pollutants by chlorine dioxideAccording to WHO guideline for drinking water quality, much consideration should be paid to benzene homologous compounds; therefore, the study on purification effect s of chlorine dioxide is focused on petrochemical pollutants. A series of experiment s were carried out to simulate the oxidation processes of contaminated water. The polluted solutions were prepared in a dark barrel (10L capacity) of seven kinds of benzene homologous compounds-Benzene , toluene , ethyl benzene , p-phenylmethane, o-phenylmethane, m-phenylmethane and styrene. Samples were taken to determine the initial concentration of the compounds prior to the test s. Standard chlorine dioxide solution was produced from sodium chlorite reacted with HCl solution of 10% [4]. The GR - 16A Gas - chromatograph with FID detector Shenyang LZ-2000 was used for measurement of Cl2, ClO2, ClO-2 and ClO-3[5]. Oil concentrations were determined with an UV -120-20 spectrophotometer (Shimadzu) following the procedure described by APHA [4]. Organic compounds in the water samples were measured with a GC-MS (QP-1000A). ClO2and O3were standardized by iodimetric titration at pH7.For the purpose of chemical disinfection for drinking water, chlorine was instantaneously ignored due to the formation of THMs and other mutagenic substances. The results indicated that potassium permanganate and hydrogen peroxide did not have enough oxidation capability to decompose petroleum contaminant s achieving only 46 %, and 5.7% decomposition of styrene, respectively. Ozone could not be selected due to it s high cost, complex operation and short half-life although it is an excellent oxidant for water treatment. Chlorine dioxide was the next most successful alternative for disinfection. The benefit s include-effective oxidation capacity, algicidal effect and negligible formation of halogenated by-products. Based on economic and operational requirement, the mixing gas method is easily used. The results obtained suggest that disinfection of drinking water with ozone and or chlorine dioxide seems to be a suitable alternatives to the use of NaClO for cont rolling the formation of non-volatile mutagens[6].In the laboratory experiments, the oxidants ozone, chlorine dioxide, potassium permanganate and the mixing gas (mainly contained ClO2 and a certain amount of Cl2, O3 and H2O2) were tested for removal of the petroleum compounds, and results are shown in Tab. 2.Tab. 2 Comparison of oxidation capacity for the various oxidantsA study was conducted to elucidate the decay pathway of monochloramine in thepresence and absence of natural organic matter (NOM) [7]. It was found that natural organic matter acted primarily as a reductant rather than catalyst. This conclusion was verified using a redox balance, and much of oxidizing capacity of monochloramine goes towards NOM oxidation. Cleaning agents and disinfectants from house keeping, hospitals, kitchens are sources of absorbable halogenated organic compounds (AOX) in municipal wastewater. The amount of AOX generated strongly depends on the nature and concentrations of dissolved and solid organic compounds, the concentration of active substances, temperature, pH and reaction time [8] When the mixing gases react with water molecules and organic micro-pollutants, hypochlorous acid is formed by chlorine, chlorite and chlorate ions are produced from chlorine dioxide in a series of redox reactions. The principal reactions are summarized as follows:ClO2+ organic →ClO -² + oxidized organic (1)2ClO -² + Cl2 = 2ClO2 + 2Cl - (2)2ClO -²+ HOCl = 2ClO2 + 2Cl - + OH- (3)2ClO2 + HOCl + H2O = 2ClO - ³ + HCl + 2H+ (4)The rate of chlorate yield can be described by Equation (5):d [ClO3]/ d t = 2 k [ClO2] [HOCl] (5)in which k = 1.28 M/ min at 25 ℃ [9].The stoichiometry of the undesirable reactions that form chlorate in low concentration of chlorite or presents of excess chlorine is given as:ClO -² + Cl2 + H2O = ClO - ³ + 2Cl - + 2H+ (6)ClO - ² + HOCl = ClO - ³ + Cl - + H+ (7)At alkaline conditions:ClO -² + HOCl + OH- = ClO - ³ + Cl - + H2O (8)Typically, chlorine dioxide is used in drinking water treatment and the concentrations are ranging from 0.1 to 2.0 mg/L [10]. However, the relevant by - products of chlorine dioxide treatment-chlorite and chlorate have been found to induce methemoglobinemia in the human body when concentrations are more than 100 mg/L [11]. The oxidation results of the organic contaminants were affected byreaction time. The initial concentrations and removal rate at different times are listed in Tab. 3. It is shown that chlorine dioxide has a very strong oxidation capability including the break down of the benzene ring. There are no other commonly used oxidants to do like this except for ozone.Tab. 3 Removal rate of tested organic compounds at different operating time (at pH7)The injecting method for chlorine dioxide gas into the solution also has an apparent influence on the removal rate. With the indirect method, the gas firstly was dissolved in a certain amount of distilled water, and then added to the tested organic solutions, as a result, removal rates appear lower than for the direct blowing method. The main reason for the difference is due to the conversion and decomposition of chlorine dioxide in the dissolving process before the reaction. It is confirmed from Tab. 3 that the removal rate was proportional to operating time. Since chlorine dioxide showed very strong oxidation capability for organic chemicals but was reduced to chlorite anion according to Equation (4), and the removal rate initially appeared quite high. Then, chlorite keeps the oxidation capacity at a level, which allows decomposition of the organic compounds to continue even though the oxidation reaction gradually became weaker with reaction time. The experiment indicated that pH values significantly influenced the removal rate of the organic compounds. The differences of degradation rates in a variety of pH through indirect input way areshown in Tab. 4.Tab. 4 Degradation rate of benzene homologous compounds with indirect method at different pH (after 15 min)There are, however, some disadvantages with ClO2, such as easy loss from solution due to volatilization, and disproportionation above pH 10 into chlorate and chlorite ions that are of certain oxidation capacity, but reported to be harmful to health if the concentration is too high. Chlorine dioxide was unstable in the solution even though it has a stronger oxidation capability than chlorite and chlorate as the two resulted in anions being dominant in the oxidation processes. The actual concentration of chlorine dioxide depended on the existence of chlorine, chlorite and chlorate whose concentrations were determined by pH values of the solution according to Equations (6) and (8) respectively. Consequently, the pH is the critical controlling factor in the concentrations of chlorine dioxide, chlorite and chlorate. The latter two harmful ions can be removed quite quickly by treatment with a reducing agent such as sulfur dioxide - sulfite ion at pH values of 5～7[10 ,12]. Fe (II) can be used to eliminate chlorite from the water , and the redox reaction is kinetically more rapid at pH 5～7 as well[13]. It was evident that the decomposition in acidic conditions was much better than that in alkaline conditions because a disproportional amount of chlorine dioxide was consumed by the reactions under alkaline conditions. For drinking water treatment, it has been suggested that the mixture of chlorine 0.8 mg/L and chlorinedioxide 0.5 mg/L will achieve disinfection and control THMs formation in preference to use of pure chlorine dioxide[14]. According to USEPA drinking water standard, the residue of ClO2 is limited as 0.8 mg/L that tends to the goal of 0.4 mg/L.4 Control of pathogens with disinfectantsHuman pathogens that are transmitted by water including bacteria, viruses and protozoa. Organisms transmitted by water usually grow in the intestinal tract and leave the body in the feces. Thus, they are infections. Fecal pollution of water supplies may then occur, and if the water is not properly treated, the pathogens enter a new host when the water is consumed, therefore, it may be infectious even if it contains only a small number of pathogenic organisms. Most outbreaks of waterborne diseases are due to breakdowns in treatment systems or are a result of post contamination in pipelines.The microorganisms of concern are those which can cause human discomfort, illness or diseases. These microbes are comprised of numerous pathogenic bacteria, viruses, certain algae and protozoa etc. The disinfection efficiency is typically measured as a specific level of cyst inactivation. Protozoan cysts are the most difficult to destroy. Bacteria and viral inactivation are considered adequate if the requirement for cyst inactivation is met. Therefore, water quality standard for the disinfection of water have been set at microorganisms, usually take the protozoan cysts as indicator, so viruses will be adequately controlled under the same operation conditions required for inactivation of protozoan cysts. The widely found drinking water contamination is caused by protozoan that is a significant intestinal pathogens in diary cattle, likely a source of this outbreak.There are two of the most important protozoa - Cryptosporidium and Giardia cysts those are known to outbreak diseases, frequently are found in nature and drinking water storage ponds. Protozoa form protective stages like oocysts that allow them to survive for long periods in water while waiting to be ingested by a host. Protozoa cysts are not effectively removed by storing water because of their small size and density. Cryptosporidium oocysts have a setting velocity of 0.5 um/s. Therefore, if the water tank is 2 m deep, it will take the oocyst 46 days to settle to thebottom. Giardia cysts are much large and have a great settling velocity of 5.5um/s. It was evident that chlorine and chloramines were ineffective against Cryptosporidium oocysts, which was discovered to be amazingly resistant to chlorine, and only ozone and chlorine dioxide may be suitable disinfectants [15]. The investigations have verified that Cryptosporidium is highly resistant to chorine, even up 14 times as resistant as the chlorine resistant Giardia, therefore methods for removing it in past rely on sedimentation and filtration. Watson′s Law to study protozoan disinfection, reads as follows:K = Cηt (9)In the formula:K ——constant for a given microorganism exposed to a disinfectant under a fixed set of pH and temperature conditions;C ——disinfectant concentration (mg/ L);η——empirical coefficient of dilution ;t ——time required to achieve the fixed percentage inactivation.For the preoxidation and reduction of organic pollutants , the recommended dosages are between 0. 5～2. 0 mg/ L with contact time as 15～30 min depending on the pollutants characteristics in the water. In the case of post - disinfection , the safe dosages of ClO2 are 0. 2～0.4 mg/L. At these dosages, the potential by - products chlorite and chlorate do not constitute any health hazard [16]. The relation between disinfectant concentration and contact time can be established by using Ct products based on the experimental data. From this the effectiveness of disinfectants can be evaluated based on temperature, pH value and contact time. Since Cryptosporidium has become a focus of regulatory agencies in the United States and United Kingdom, the prospects of controlling this pathogen show more considerable. The comparison of the Ct values by using ozone , chlorine dioxide , chlorine and chloramines for Giardia and Cryptosporidium cyst s are listed in Tab. 5[17 ,18 ] , and for some microorganisms disinfection are displayed in Tab. 6[19 ] .Tab. 5 Ct values (mg·min/ L.) for disinfection of Giardia and Cryptosporidium cysts by using 4 disinfectantsTab. 6 Comparison of value intervals for the product Ct (mg·min/ L) for the inactivation of various microorganisms by using 4 disinfectantsThe mean Ct value for ClO2 at pH 7 and 5 ℃was 11. 9 mg·min/ L, and dropped to 5.2 at pH 7 and 25 ℃. High temperatures normally enhance the efficiency of disinfectants while lower temperatures have opposite effects requiring additional contact time or extra quantity of disinfectants. The best performance for ClO2 is at pH 9 and 25 ℃, which yields a Ct product of 2.8 mg·min/ L [20]. Chlorine dioxide appears to be more efficient for Cryptosporidium oocysts than either chlorine or monochloramine. Exposure of oocysts to 1.3 mg·min/ L at pH 7 reduces excystation from 87 % to 5 % in a hour at 25 ℃. Based on this result, Ct product of 78 mg·min/ L was calculated. However, the Ct product for ozone to do this work was examined as 5 - 10 mg·min/ L from observation that excystation decreased from 84 % to 0 % after 5 minutes with the ozone concentration of 1 mg/ L [15]. As with other disinfectants, increasing temperature decreased the Ct values and improved the cysticidal action. Increasing temperature unexpectedly reduced the Ct values from a high of 6.35 mg·min/ L at pH5 to a low of 2.91 mg·min/ L at pH 9[20]. It is generally the rule, that for protozoa ozone is the best cysticide, chlorine dioxide is superior to chlorine andiodine, but chlorine, in overall, is much superior to chloramines [21].Although disinfection efficiency of ozone is higher than chlorine dioxide, this difference can be compensated by the contact time. The experiment indicated that chlorine dioxide could reach the same results for disinfection of coliform bacteria as ozone did if time lasted long enough, which can be seen in Fig. 1. The added concentrations of both of ozone and chlorine dioxide were 2 mg/ L.Control of Cryptosporidium oocysts in potable water requires an integrated multiple barrier approach. Coagulation is critical in the effective control of Cryptosporidium by clarification and filtration. Dissolved air floatation can achieve oocysts removal of 3 logs compared to about 1 log by sedimentation. Dissolved air floatation and filtration provide two effective barriers to Cryptosporidium oocysts with cumulative log removal of 4 to 5 compared to log removals of 3 to 4 by sedimentation and filtration [22].Fig. 1 Comparison of disinfection efficiency between ozone and chlorine dioxide on coliform bacteria5 Tendency of disinfection for drinking waterIn the future, the burden of producing water with low pathogen level and low tastes and odor will be allocated to a combination of steps, including source water protection, coagulation - flocculation - sedimentation, filtration, floatation, membrane processes and adsorption. Some form of terminal treatment with chlorine, chlorine dioxide, ozone, UV, or other agents will also be required. No single step can or should be expected to shoulder the entire burden to controlling a given contaminant. With the development of techniques, new chemical and physical agents will meet tests of practicability for use in water treatment and will reduce pathogens. These may include electromagnetic fields and other forms of treatment with light or sonic energy [23].In light of availability, efficacy, operability and costs, the priority should be given to ultraviolet method among all of the currently utilized disinfection technologies, particularly in developing countries. The medium and low - pressure UV extends tremendous potential promise for adaptation into various scale water supply plants. The researches have validated that extremely low dosage of UV can behighly effective for inactivate oocysts [24]. Furthermore, comparison of medium and low - pressure lamps demonstrated no significant differences. By using low - pressure UV at the dosage of 3 , 6 and 9 mJ/ cm2 , oocyst inactivation levels were yielded between 3.4 and 3.7 log. In the trials of UV in water with turbidity of more than 1 NTU, the ability of medium –pressure was not affected, and high level of oocysts inactivation could still be achieved.6 ConclusionsTo purify drinking water, chlorine dioxide can be chosen instead of chlorine, ozone and other disinfectants because of it s advantages of high efficiency of disinfection, competent stability, low cost and simple utilizing way etc. Both ozone and ClO2 are absolutely vital to ensure that any microorganisms arising from fecal contamination of water storage are destroyed. The utilization of chlorine dioxide has been found to efficiently restrict protozoa growth, to disinfect from bacteria and viruses. Taking the protozoan cysts as indicator in which Cryptosporidium oocysts were solidly resistant to chlorine, but chlorine dioxide may be suitable disinfectants to mutilate. Thus, viruses will be adequately controlled by chlorine dioxide under the same operation conditions required for inactivation of protozoan cysts. The experiment indicated that chlorine dioxide could reach the same results for disinfection of coliform bacteria as ozone did if time lasted long enough although disinfection efficiency of ozone is higher than chlorine dioxide.It is an obvious preference for chlorine dioxide to pragmatically remove oil and benzene homologous compounds in water treatment meanwhile the formation of mutagenic and toxic substances is limited. The degradation rate was proportional to input amount of oxidants and increase of operating time. The dosage input , in overall , is suggested to range between 0. 5～2.0 mg/ L. The effective pH at which reactions occur is in the slightly acid range of 5 to 7 at which formation of chlorite and chlorate is minimized. The chlorine dioxide gas should be injected directly into the treated water body, so that high concentrations of ClO2 can be kept in the solution. Under these conditions, the elimination rate for organic pollutants will be much higher. For the storage system, input dosage of chlorine dioxide concentration should be higherthan that in laboratory studies due to complex pollutants in treated water. References:[1 ] Katz J . Ozone and chlorine dioxide technology for disinfection of drinking water [M]. Noyes New Jersey: Data Corporation, 1980.[2] Fiessinger F. Organic micropollutants in drinking water and health [M] . Publisher, N. Y., U. S. A: Elsevier Sci., 1985.[3 ] Hoff J C , Geldreich E E. Comparison of the biocidal efficiency of alternative disinfectants [C] . In Proceedings AWWA seminar, Atlanta, Georgia, 1980.[4 ] APHA , American Public Health Association. American Water Works Association and Water Pollution Control Federation. Standard Methods for the Examination of Water and Wastewater. (16th Edition) [M]. Washington D. C., 1989.[5] Dietrich A M. Determination of chlorite and chlorate in chlorinated and chloraminated drinking water by flow injection analysis and ion chromatography[J ] .A nal. Chem., 1992, 64:496 - 502.[6] Monarca S. Mutagenicity of extracts of lake drinking water treated with different disinfectants in bacterial and plant tests[J ] . Water Res, 1998, (32):2 689 - 2 695.[7] Vikesland P , Ozekin K, Valentine R L. Effect of natural organic matter on monochloramine decomposition : pathway elucidation through the use of mass and redox balance[J ] . Envi ron. Sci. Tech., 1998, 32 (10):1 409 - 1 416.[8] Schulz S , Hahn H H. Generation of halogenated organic compounds in municipal wastewater [M] . Proc. 2nd Int. Assoc. Water Qual. Int. Conf. Sewer Phys. Chem. Bio. Reactor, Aalborg, Denmark, 1998.[9 ] Aieta E M. A review of chlorine dioxide in drinking water treatment [J]. J. A WWA, 1986, 78 (6): 62 - 72.[10 ] Gordon G Minimizing chlorine ion and chlorate ion in water treatment with chlorine dioxide[J ] . J. A WWA, 1990, 82 (4):160 - 165.[11] Kmorita J D , Snoeyink V L. Monochloramine removal from water by activated carbon[J ] . J. A WWA, 1985, (1):62 - 64.[12] Gordon G, Adam I , Bubnis B. Minimizing chlorate information[J ] . J. AWWA, 1995, 87, (6): 97 - 106.[13] Iatrou A. Removing chlorite by the addition of ferrous iron[J ] . J. A WWA, 1992, 84 (11): 63 - 68.[14 ] Schalekamp Maarten. Pre - and intermediate oxidation of drinking water with ozone, chlorine and chlorine dioxide [J]. J. Ozone Science and Engineering, 1986, 8: 151 - 186[15 ] Korich D G, Mead J R , Madore M S , et al . Effects of ozone, chlorine dioxide, chlorine and monochramine on Cryptosporidium parvum oosyst viability [J]. Applied and Environmental Microbiology, 1990, 56: 1 423 - 1 428.[16 ] AWWA Research Foundation. Chlorine dioxide; drinking water issues, 2nd International Symposium [R]. Houston, TX, 1992.[17] Lykins B W, Griese H G. Using chlorine dioxide for trihalomethane control[J ] . J, A WWA, 1986, 71 (6): 88 - 93.[18] Regli S. Chlorine dioxide , drinking water issues , 2nd International Symposium [ R ] . Houston, TX, AWWA Research Foundation, 1992.[19] Hoff J C. Inactivation of microbial agents by chemical disinfectants[J] . US EPA, 1986.[ 20 ] Rubin A , Evers D , Eyman C , et al . Interaction of gerbil - cultured Giardia lamblia cysts by free chlorine dioxide [J]. Applied and Envi ronmental Microbiology, 1989, 55: 2 592 - 2 594.[ 21 ] Rusell A D , Hugo WB , Ayliffe GA J . Principes and Practice of Disinfection [M]. Preservation and Sterilization. Blackwell Scientific Publications, Oxford, U K, 1992.[22 ] Edzwald J K, Kelley M B. Control of Cryptosporidium from reservoirs to clarifiers to filters [C] . Proc. 1st IAWQ –IWSA Joint Specialist Conf. Reservoir Manage. Water Supply, Prague, Czech, 1998.[23] Haas Charles N. Disinfection in the Twenty - first century[J ] . J. A WWA, 2000, 92 (2): 72 - 73.[24 ] Clancy L , Jenneifer , Bukhari Z , et al , Using UV to Inactivate Gryptosporidium[J ] . J. A WWA, 2000, 92: 97 - 104.饮用水的消毒及杀菌技术研究朱琨伏小勇(兰州铁道学院环境工程系, 甘肃兰州730070)摘要:饮用水处理消毒过程中可产生一系列致癌物质,主要是氯与水中的有机物和其它化学成分反应的结果,其中典型产物有三氯甲烷. 通过对常用消毒剂液氯,臭氧,二氧化氯,高锰酸钾,氯胺及过氧化氢的实验对比,证明二氧化氯是高效,方便,廉价的消毒剂. 它不仅对一般病原菌类有明显的抑制和杀菌作用,对清除难以灭杀的潜原性病毒也有理想的效果. 在净化水中石油类有机物时,二氧化氯的效果受到反应时间,注入方式和pH 值的影响.关键词:消毒;氧化剂;水处理;病原菌;二氧化氯中图分类号:X523 文献标识码:A中文译文：饮用水消毒和杀菌技术的研究朱琨伏小勇（兰州铁道学院环境工程系，甘肃兰州，730070 中国）在饮用水处理过程中，通过氯与溶解性有机物和其他化合物的反应所产生的消毒副产物被看作一个令人担忧的问题，因为一系列诱变致癌的物质组成包括总卤甲烷。

(整理)污水处理英语词汇

污水处理英语词汇 AA/A/O 法anaerobic-anoxic-oxicprocess(厌氧-缺氧-好氧法)A-A-O 生物脱氮除磷工艺 A-A-O biological nitrogen andphosphorus removal process A-O 脱氮工艺 A-Onitrogen removal process A-O 除磷工艺 A-Ophosphorus removal process AB 法 Adsorption Biodegradation process(吸附生物降解法)总a 放射线 Total a radioactivity氨氮 ammonia-nitrogen 氨基酸 amino acid氨化反应 Nitragen铵盐 ammonium saltA/O 法(厌氧-好氧法)anaerobic-oxic process奥贝尔(Orbal)型氧化沟Orbal oxidation ditchB巴登福脱氮除磷工艺Ｂardenpho nitrogen and phosphorus removal process白水(漂洗废水) whitewater(bleaching water) 板框压滤 plate pressure filtration离心机 centrifugal machine半渗透膜semi-permeable membrane棒状杆菌属corynebacterium薄膜式淋水填料 filmpacking饱和常数(Ks) saturationconstant 暴雨公式 storm flowformula 暴雨径流 storm runoff溢流井 overflow well苯 benzene苯胺 aniline总B 放射性 Total Bradioactivity泵型叶轮暴气器 paddleimpeller aerator泵站 pumping stationBMTS 型一体化氧化沟BMTS intrachannel clarifieroxidation ditch 闭路循环 closed loop表面冲洗 surfacewashing表面负荷 surface load表面过滤 surfacefiltration 表面活性剂 surfactant表面活性物质 surface active additive agent表面曝气 surface aeration表面曝气器 surface aerator表面淹灌 surface flood irrigation表面冲洗装置 surface washing facility丙烯酸 acrylic acid 丙烯腈 acrylonitrile病毒 virus病原菌(致病菌) pathogen 病原微生物 pathogen microorganismBOD-污泥负荷BOD-sludge load补充水 make-up water 布朗运动 Brownian movement C财务评价 financial evaluation配水系统 distribution system侧渠型一体化氧化沟 integrated oxidation ditchwith side ditch产氢气乙酸菌 Rydrogenes and acetic aidgenes产甲烷细菌methanogenes产率系数 yield coefficient常规给水处理工艺 conventional water treatmentprocesses敞开式循环冷却水系统 opened recirculating coolingwater system超高纯水ultra-high-purify water超过滤 ultrafiltration超过滤膜法ultrafiltration membrane process沉淀 precipitation, sedimentation沉淀池 sedimentationtank沉砂池 grit chamber城市废水 municipalwastewater城市废水处理 municipal wastewater treatment澄清 clalification可持续发展 sustainable development充满度 degree of fullness重现期 exceedion interval, period of recurrence抽风式机械通风冷却塔 induced draft mechanical cooling tower臭氧发生器 ozone generator臭氧法 ozonation process臭氧消毒 ozonedisinfection 初次(级)沉淀池 primary clarifier, primarysedimentation tank除水器 drift eliminator除铁除锰 iron and manganese removal 除盐水(脱盐水) desalted water,demineralized water 除渣 desilication, silica removal除藻 algal removal 除氟 algal fluorine穿透曲线 penetration curve活性污泥法 activatedsludge process 生物脱氮工艺 biological nitrogen remo process船型一体化氧化沟 BoatType in intrachannelclarifier oxidation ditc纯(富)氧曝气法pure-oxygen aeration pro磁凝结 magnetic coagulation磁盘法 magnetic diskprocess 磁过滤法 magneticfierration process萃取 extraction萃取剂 extractant D 达西定律 Darcy ’s law大肠菌群Coliform-group bacteria大气泡曝气装置 large bubble aerator代谢 metabolism带式过滤 belt press filtration]单级传统消化池 single-stage conventional digester单螺旋式曝气装置single spiral aerator 氮 nitrogen氮循环 nitrogen cycle 蛋白质 protein倒虹管 inverted siphon 低放射性废物 low-level radio active waste 制浆废水 kraft mill wastewater敌百虫 dipterex敌敌畏 dichlorvos 涤纶纤维 polyester fiber地表漫流系统 overland flow system(OF)地表水 surface water地面（表）水环境质量标准 environmental quality standard for surface water地下滤场 underground filtration field地下渗漏 underground percolation地下渗滤系统 subsurface infiltrationsystem地下水 groundwater人工湿地系统artificial(constructed)wetland再生水回流地下水质标准water quality standard forrecharging parifiedwastewater water into groundwateraquifer地下水位 underground water level淀粉生产废水 starch producing wastewater点滴-薄膜式淋水填料splash-film packing点滴式淋水填料 splash packing 点污染源 pointpollufion source 电动电位electromotance potential电镀废水electroplating wastewater电极 electrode电解法 electrolyticalprocess电流密度 eletronic density电渗析 electrodialysis 电渗析器electrodialyzer电晕放电 brush discharge动态年成本 dynamic annual cost动植物油 oil and grease 对硫磷 parathion 多层床 multibed 多环芳烃 polycyclichydracarban 多氯联苯polychlorinated biphenyls(PCBs) E二次(级)沉淀池secondary clarifier, secondary sedimentation 二级处理 secondarytratament F 乏燃料 spent fuel 反冲洗 black washing反渗透（逆渗透）reverse osmosis 反渗透法 reverseosmosis process反渗透膜 reverse osmosis membrane反硝化，脱氮denitrification防止腐蚀 corrosion prevention纺丝 spining 纺织废水 textile wastewater放射性半衰期radioactive half-life放射性废水处理 radioactive wastewatertreatment放射性排出物radioactive effluent非点源污染（面源污染）non-point source pollution非离子氨 non-ionic ammonia废水处理 wastewater treatment废水中和neutralization of wastewaters分离 separation分流制 separate system分流排水系统separated sewer system酚 phenol焚烧 incineration 风吹损失 windageloss风筒式冷却塔chimmey cooling tower封闭循环系统 closedrecirculation system氟化物 fluoride辐射流沉淀池 radial flow sedimentation tank浮盖式消化池floating-cover digester气浮 flotation 福斯特利帕除磷工艺 Phostrip phosphorus removal process福列德克斯脱氮除磷工艺 Phoredox nitrogen and phosphorus removal process 腐蚀 corrosion富营养化eutrophication富营养化湖泊、水库 eutrophic lake,eutrophicreservoirGr 射线 gamma rays 甘蔗废水 sugarcanewastewater 干化 drying干化床 drying bed冷却塔 cooling tower钢铁工业废水 iron and steel mill wastewater高纯水 ultrapure water 高放废物 high-level radio active wastes高份子电解质polymolecular electrolye高份子絮凝剂polymolecular floc高负荷活性污泥法 high-loading activatedsludge method高负荷生物滤池 high loading biological filte高炉煤气洗涤水wastewater produced fromscrubbing blast furnacegas高锰酸盐指数 potassium permanganate index高速消化池 high-rate digester高梯度磁分离器(HGMS) high grade magnegic separator高浊度水 high turbiditywater 格栅 bar screen 隔板反应池 bafflereaction tank隔板式混合槽 baffle mixer隔油池 oil separator 镉 cadmium铬 chromium给水泵站 water pumping station给水处理 water treatment给水网管系统 water supply system工业水处理与循环系统industrial water treatment and recirculation system工业废水 industrial wastewater汞 mercury鼓风曝气 blast aeration 鼓风式机械通风冷却塔 forced draft mechanicalcooling tower固定螺旋式曝气装置fixed spiral aerator景观、娱乐水体landscape and recreation waterbody管道接口 conduit joint 给水配水系统 watersupply piping distribution system网管平差 balancingnetwok 罐头生产废水 Cannerywastewater硅藻土 cilicious mar H海水淡化demineralization of sea water含酚废水 phenol contained wastewater含水量 moisture content含盐量 saline capacity 含油废水 oily wastewater旱流污水量(DWF)dry-weather flow 好氧生物处理 aerobicbiological treatment 好氧塘 aerobic pond 好氧稳定 aerobic stabilization合成洗涤剂 synthetic detergent合成纤维 synthetic fiber合成纤维废水 synthetic fiber wastewater 合成橡胶 synthetic rubber合流城市废水 combinedmunicipal wastewater合流制排水系统combined sewer system水体功能分类 waterbodyfunction classification核能工厂 nuclear power station核燃料循环 nuclear fuel cycle核素 nuclide冶金工业废水metallurgical industrywastewater黑液 black liquor 黑液除硅sillica-elimination fromblack liquid虹吸滤池 siphon filter 化学处理 chemicaltreatment化学工业 chemicalindustry化学吸附 chemicaladsorption 化学纤维 chemical fiber化学需氧量 chemicaloxygen demand (COD)环状管网系统 grid pipe network system缓蚀 corrosion inhibition缓蚀剂 corrosion inhibitor磺化煤 sulfonated coal 挥发酚 volatile phenol 回流比 recycle ratio 回流污泥率 return sludge ratio汇水面积 catchment area, collection area混合 mixing混合床 miced bed 混合液挥发性悬浮固体mixed liquor volatile suspended solids(MLVSS) 混合液悬浮固体 mixed liquor suspended solids(MLSS)混凝 coagulation 混凝沉淀coagulation-sedimentation 混凝剂 coagulant 浑浊度 tubidity活化产物 activation products硅酸钠 sodium silicate 活性剂 activator活性染料 active dye 活性炭 activated carbon活性炭的再生re-generation of activated carbon活性炭吸附 activecarbon adsorption活性污泥 activated sludge 活性污泥法 activatedsludge process 活性污泥负荷 activatedsludge loading活性污泥驯化acclimation of activatedsludge J机械反应池 mechanicalreactor机械剪切曝气装置mechanical shearing aerator机械搅拌 mechanicalmixing机械搅拌澄清池accelerator机械曝气 mechanicalaeration机械通风冷却塔mechanical draft cooling tower 机械脱水 mechanicaldewatering极化现象 polarization级配 granularcomposition集水池 collection well集中处理(合并处理)joint treatment计算机 computer 计算机辅助设计computer aid design加速过滤器accelo-filter加压气化 pressure-gasification甲基对硫磷 parathion methyl甲醛 formaldehyde甲烷 methane甲烷发酵 methane fermentation 甲烷气体 methane gas间歇式活性污泥系统sequencing batch reactoractivated sludge system(蒹性塘 facultative pond检查井 manhole 减压薄膜蒸发法decreasing pressure andthin-film evaporation process碱法制浆 soda pulping process浆粕 pulp降雨历时 duration of rainfall降雨量,降水precipitation浇洒道路用水 street flushing water焦化废水 coking wastewater交替工作式氧化沟alternative operating oxidation ditch交替运行的生物滤池alternative operating trickling filter胶体 colloid阶段曝气 step aeration 接触池 contact chamber 接触氧化法 contactoxidation process 结垢 scale节水 water saving 锦纶纤维 polyamide fiber腈纶纤维 acrylic fiber 精制塘(深度处理塘) polishing pond经济效益 economic benefit径流系数 runoff coefficent静态年成本 static annuity cost景观娱乐用水水质标准 water quality standard forlandscape and recreation area酒精工业 alcoholdistilery就地处理系统(小型处理)on-site treatment systems(small scale facilities)聚丙烯酰胺polyacrylamide聚丙烯酰胺水解体polyacrylamide hydrolysis product聚合 polymerize聚合度 polymerizingdegree聚合氯化铝polyaluminum chloride均衡池(塘) equalizaliontank(basin,lagoon)K卡罗塞式氧化沟Corrousel oxidation ditchK 型叶轮曝气机 K type impeller aerator凯式氮 kjeldahlnitrogen空气驱动式生物转盘aero biological disks孔隙率 porosity快滤池 rapid filter快速渗滤系统 rapid infiltration system(RI) 矿井 shaft(mine)矿区 mining area 矿区环境 mining area environment 矿山废水 minery wasterwater矿山酸性废水 acid minewastewater 扩散板 diffusion plate扩散管 diffusion tube扩散盘(罩) diffusion disc(cover) L乐果 dimethoate冷凝 condensation 冷凝水 condensate water 冷却 cooling冷却池 cooling pond 冷却塔 cooling tower 冷却塔配水系统 coolingtower distribution system 冷却循环水 circulated cooling water冷轧 cold steel -rolling离心泵 centrifugal pump 离心 centrifugation force离心机 centrifugal machine离心脱水 centrifugal dewatering离心作用centrifugation离子交换 ion exchange离子交换剂 ion exchanger离子交换膜 ion exchangemembrane离子交换树脂 ion exchange resin粒径 grain size砾石承托层 gravel support炼钢厂废水steel-making process wastewater炼铁 iron-smelting 炼铁(高炉)废水 blast furnace wastewater炼油厂废水 refineryprocessing waserwater淋滤 leaching淋水密度 waterdrenching density淋水面积 waterdrenching aera淋水填料 packing磷 phosphorus 磷酸盐 phosphate生物流化床 Biologicalfluidized bed硫化物 sulphide硫化物沉淀法 precipitation with sulphide硫酸铵 ammonium sulfate硫酸钙 Calcium sulfate 硫酸铝 aluminum sulfate 硫酸镁 magnesiumsulfate硫酸铁 ferric sulfate 硫酸亚铁 ferrous sulfate硫酸盐 sulfate 硫循环 sulphur cycle 铝酸钠 sodium aluminate 滤层 filter layer滤池冲洗水量 filter washing water consumptio滤池配水系统 filterunderdrain system滤池运行周期 filtercycle time滤床 filter bed 滤料 filtering medium滤速 filtration rate 滤液 filtrate 氯 chlorine氯-氨法chlorine-ammonia process氯化,加氯处理 chlorination氯化物 Chlorides螺旋桨式快速搅拌机 propeller-type high speeagitatorM马拉硫磷 malathion脉冲澄清池 pulsator慢滤池 slowfilter慢速渗滤系统 slow rate infiltration system (SR) 煤气 coal gas 煤气厂 gas work煤气发生器 coal gas generator煤气发生站 gasgeneration station 煤气净化 coal gas purification煤炭 coal 锰 manganse米门公式 Michaelis - Menten equation莫诺德公式 Monod equation密闭式循环冷却水系统closed recirculating cooling water system密集多喷嘴曝气装置compact multinozzle aerator 面污染源 non-point pollution source敏感性分析 sensitivity analysis膜分离装置 membrane seperator膜选择性 membrane selectivity膜污染 membrane foulting膜中毒 membrane poisoningN难生物降解有机物nonbiodegradable organies 尼龙 nylon逆流漂洗counter-current washing 逆流式冷却塔counterflow cooling tower逆流再生counter-current regeneration粘胶 rayon酿酒废水 winery wastewater酿造与发酵工业废水 brewery and fermentation industrial wastewater凝结 coagulation凝结剂 coagulant牛奶生产废水 dairywastewater 浓缩 concentration浓缩倍数 cycle of concentration浓缩池 thickening tank浓缩污泥 concentrated sludge农田灌溉水质标准 standards for irrigationwater quality农用污泥中污染物控制标准 contaminants controlstandard for sludge farm农药 pesticide 农药厂废水 pesticideplant wastewaterP排泥系统 sludge - discharge system排水量 discharge排水管 drain pipe排水口 outlet排水系统 sewer system排污 blowdown泡沫分离 foam phaseseparation配水网管 distributionsystem ,pipe system 喷灌 spray irrigation喷水池 spray pond 皮革 leather 啤酒废水 brewery wastewater啤酒废水处理 brewery wastewater treatment漂白 bleaching平板式膜 plate membrane平板式叶轮曝气器 plate impellar aerator平衡吸附容量equilibrium adsorption capacity平流式沉砂池 horizontal flow grlt removal tank平流式沉淀池horizontal flow sedimentation tank 普通生物滤池biological filter,trickling filter曝气 aeration曝气沉砂池 aerationgrit chamber曝气池 aeration tank曝气栅 aeration boom曝气设备 aerationequipment曝气时间 aeration time曝气装置,曝气机aerator居民生活垃圾 HouseholdWaste庫底平整線 bottom flattingline of the site庫區填埋邊線 landfill sideline of the site庫容 Storage capacity垃圾 Waste ，Solid Waste 垃圾壩 waste dam 垃圾殘渣 residue垃圾槽 waste chute 垃圾層 waste layer 垃圾產量 Waste output垃圾堆肥場 waste compostingfield 垃圾堆體 waste pile 垃圾副壩 secondary waste dam 垃圾揀選場 Waste Sorting Site垃圾氣化 waste gasification垃圾采集車 waste collector垃圾桶 garbage ，rubbishbarrel垃圾箱 garbage container 垃圾壓實系統 wastecompactor system垃圾衍生燃料 Refuse-derivedfuel (RDF)垃圾衍生燃料 waste derivedfuel垃圾轉運車 waste transfer truck垃圾轉運站 waste transferstation垃圾裝卸坡 waste loadingramp離心脫水機 centrifugaldewaterer鈉基膨潤土 sodium bentonite農業廢棄物 AgriculturalWaste 濃縮池 thickening tank 排放 discharge排泥閥 sludge valve排水口 Drain Outlet 膨潤土 bentonite熱解 Pyrolysis 溶解氧測定儀（DO 計） dissolved oxygen meter （DO meter ）砂水分離機 grit-water splitter 商業垃圾 Commercial Waste 上橫沖填埋場 ShanghengchongLandfill Site上清液 supernatant liquor設備選型 Type selection of equipment 滲濾液（垃圾滲濾液） leachate 滲濾液處理 leachatetreatment滲濾液處理站 Leachate Treatment Station滲濾液采集及導排氣系統平面圖 Plan of Leachate Collection and Guiding a Exhaust System 滲濾液采集盲溝 blind drain for leachate collection精品文档精品文档生活垃圾 Domestic waste 生活垃圾焚燒污染控制標准 Standard for Pollution Control on the Municipal Solid Waste Incineration 剩余污泥 excess sludge 剩余污泥泵 excess sludge pump 輸渣機 clinker conveyer 豎向石籠 vertical stone cage雙層防滲結構 double-linersystem水位 water level提升泵站 lift pumpingstation填埋（垃圾） Landfill填埋場 Landfill site填埋場封場 seal of landfillsite填埋場總體布置圖 GeneralLayout of Landfill Site填埋場縱斷面示意圖 SketchMap of Landfill Site VerticalSection填埋庫區 Landfill Area填埋庫區平面布置圖 PlaneLayout of Landfill Area1:1000填埋氣 Landfill gas砼 concrete圖例 legend土工合成材料黏土墊層Geosynthetics Clay Liner(GCL)土工膜 geomembrane脫水機 dewaterer脫水機房 dewatering house衛生填埋 sanitary landfill渦流沉砂池（旋流沉砂池）vortex grit tank污泥泵房 sludge pumping room污泥處理 sludge treatment污泥處理流程示意圖 FlowChart of Sewage TreatmentProcess污泥管線 sludge pipeline 污泥濃度計（MLSS 計） sludge concentration meter （MLSS meter ）污泥濃縮及脫水機房 Sludge Thickening & Dewatering House污泥脫水車間 sludge dewatering workshop 污水泵 sewage pump 污水處理 sewage treatment 污水處理厂 Wastewater Treatment Plant 污水處理流程示意圖 Sewage Treatment Process Sketch Map 污水管線 sewage pipeline 污水水面 wastewater surface 無線傳輸 wireless transmission 吸水井 suction well 消毒池 disinfecting tank 新聯村熊家窯 Xiongjiayao, Xinliancun 序批式活性污泥法（SBR 法） Sequence Batch Reactor 選型 Type selection 壓縮式垃圾車 waste compactors 厭氧、缺氧、好氧 Anaerobic, Anoxic, Aerobic Underwater Blender 厭氧堆肥 anaerobic composting 厭氧發酵 methane fermentation; anaerobic fermentation 厭氧流化床反應器 anaerobic fluidized bed 厭氧流化床反應器 anaerobic fluidized bed 氧化溝 oxidation ditch 氧化溝 oxidation ditch 葉輪曝氣機 impeller aerator 一級發酵（初級發酵） primary fermentation醫院垃圾 Hospital Waste 營養土層 nutritious soil layer預留垃圾綜合利用生產用地Reserved Waste Comprehensive Utility and Production L再生 reclamation 柵渣 sediment 黏土層 clay layer 支盲溝 blind sub-drain 至垃圾填埋場 to the waste landfill site 終期覆土 terminal earth covering 主盲溝 main blind drain 自控系統 autonomous system 自然土層 natural soil layer。

污水处理英文

污水sewage污水处理 sewage treatment一级处理 primary treatment二级处理 secondary treatment生物处理 biological treatment活性污泥法 activated sludge process曝气池 aeration tank曝气 aeration充氧oxygenation好氧消化 aerobic digestion厌氧消化 anaerobic digestion溶解氧dissolved oxygen沉淀 sedimentation搅拌agitation氯化 chlorination余氯 residual chlorine污泥 sludge泥龄sludge age回流污泥 returned sludge剩余污泥 surplus sludge消化污泥 digested sludge活性污泥 activated sludge污泥浓缩 sludge thickening污泥脱水 sludge dehydrating絮凝 flocculation水头Flood peak水头损失 head loss液面负荷 surface load、工艺参数类设计流量 Design flow泵流量pump flow栅前水深 water depth of ahead grille过栅流速Crosses the grille speed of flow栅条间隙Grille gap过栅水头损失head loss of crosses the grille 格栅倾角 Grille inclination angle过栅流量 flow of grille齿耙运行速度 rake speed有效水深Effective water depth水力停留时间HRT hydraulic residence time水力表面负荷Hydraulic load surface污泥浓度sludge concentration污泥回流比sludge reflux ratio机械设备类粗格栅 coarse screen回转格栅除污机grille decontaminating equipment 无轴螺旋输送机shaftless screw conveyor无轴螺旋压榨机 shaftless screw compressor潜污泵submersible sewage pump细格栅fine screen旋流沉砂器rotational sand processor砂水分离器 grit-water separator潜水搅拌器submersible agitator潜水推流器 submersible water impeller可调堰门adjustable weir曝气转刷aeration brushes吸刮泥机aspiration sludge scraper离心脱水机Decanter Centrifuge切碎机Macerator转鼓浓缩机Drum thickener絮凝剂投配单元polymer make-up &dosing unit圆形闸门Circular gate蝶阀 butterfly valve闸阀 gate valve球阀 Ball valve止回阀 Check Valve放空阀 Emptying valve微阻缓闭止回阀 Tiny Drag Slow Shut Check Valves 电磁阀 Mgnetic valve电动阀 Mortor operated valve法兰 Flange主轴承main bearing减速机gearbox超声波流量计supersonic flow meter电磁流量计electromagnetic flow meter阅读全文monitored control system 监察控制系统sewage treatment 污水处理Welcome to Danone monitored control system of sewage treatment。

污水专业英语翻译大全

污水处理专业英语翻译大全专有名词病毒细菌Campylobacteria Jejuni 弯曲菌Coliform-group bacteria 大肠菌群Corynebacterium 棒状杆菌属Cryptosporidium 隐孢子虫Escherichia Coli 大肠杆菌Dipterex 敌百虫Giardia 贾第鞭毛虫Legionella 军团菌Methanogenes 产甲烷细菌Norovirus 诺罗病毒Pathogen 病原菌(致病菌)Rydrogenes and acetic aid genes 产氢气乙酸菌自建字库A/A/O法 anaerobic-anoxic-oxic process (厌氧-缺氧-好氧法)A-A-O生物脱氮除磷工艺 A-A-O biological nitrogen and phosphorus removal process Activated sludge process 活性污泥法Adsorption 吸附Aeration 曝气Aerobinen bakteeri 需氧微生物A-O脱氮工艺 A-O nitrogen removal processA-O除磷工艺 A-O phosphorus removal processAB法Adsorption Biodegradation process (吸附生物降解法)ammonia-nitrogen 氨氮ammonium salt 铵盐amino acid 氨基酸Anaerobinen bakteeri 厌氧微生物A/O法(厌氧-好氧法) anaerobic-oxic processBackwater 回用水Biofilm 生物膜法Biological aerated 生物曝气BOD (Biochemical oxygen demand) 生物需氧量Campylobacteria Jejuni 弯曲菌Carrousel Oxidation ditch 卡鲁塞尔氧化沟（荷兰DHV1967研制）CAST回圈式活性污泥法(Cyclic Activated Sludge T echnology，简称CAST) Cesspool 污水池COD（chemical oxygen demand）化学需氧量Colloid 胶体Corrosion腐蚀Cryptosporidium 隐孢子虫Giardia 贾第鞭毛虫Escherichia Coli 大肠杆菌Eutrophication 富营养化Flocculation 絮凝Flotation 悬浮法= flotaatioHBR （high compound biological reactor）高效复合生物反应器Hydrogen sulfide 硫化氢= rikkivetykaasuICEAS间歇循环延时曝气系统(Intermittent Cycle Extended Aeration System)Ion Exchange 离子交换Legionella 军团菌Microbiology 微生物Nitragen氨化反应Norovirus 诺罗病毒Nutrients 营养物Orbal oxidation ditch奥贝尔(Orbal)型氧化沟ozone generator臭氧发生器ozonation process臭氧法ozone disinfection臭氧消毒Pathogen病原菌(致病菌)pathogen microorganism病原微生物primary treatment, 一级处理SBR序列间歇式活性污泥法（Sequencing Batch Reactor Activated Sludge Process）secondary treatment 二级处理Sedimentation tank 沉淀池Sewage 污水Sewage treatment 污水处理sewage treatment rate 污水处理率Suspended solids 悬浮物Tertiary treatment 三级处理Total a radioactivity总a放射线Unitank好氧生物污水处理法Wastewater 污水B巴登福脱氮除磷工艺Ｂardenpho nitrogen and phosphorus removal process白水(漂洗废水) white water(bleaching water)板框压滤 plate pressure filtration离心机 centrifugal machine半渗透膜 semi-permeable membrane棒状杆菌属 corynebacterium薄膜式淋水填料 film packing饱和常数(Ks) saturation constant暴雨公式 storm flow formula暴雨径流 storm runoff溢流井 overflow well苯 benzene苯胺 aniline总B放射性 Total B radioactivity泵型叶轮暴气器paddle impeller aerator泵站 pumping stationBMTS型一体化氧化沟 BMTS intrachannel clarifier oxidation ditch 闭路循环closed loop表面冲洗surface washing表面负荷surface load表面过滤surface filtration表面活性剂 surfactant表面活性物质 surface active additive agent表面曝气 surface aeration表面曝气器surface aerator表面淹灌 surface flood irrigation表面冲洗装置 surface washing facility丙烯酸acrylic acid丙烯腈acrylonitrile病毒virus病原菌(致病菌) pathogen病原微生物pathogen microorganismBOD-污泥负荷 BOD-sludge load补充水 make-up water布朗运动 Brownian movementBOD (Biochemical oxygen demand) 生物需氧量Campylobacteria Jejuni 弯曲菌Carrousel Oxidation ditch 卡鲁塞尔氧化沟（荷兰DHV1967研制）Cast活性污泥法之一Cintinuous Loop Reator,简称CLR连续环式反应池COD（chemicaloxygendemand）化学需氧量C财务评价 financial evaluation配水系统 distribution system侧渠型一体化氧化沟 integrated oxidation ditch with side ditch产氢气乙酸菌 Rydrogenes and acetic aid genes产甲烷细菌 methanogenes产率系数 yield coefficient常规给水处理工艺 conventional water treatment processes敞开式循环冷却水系统 opened recirculating cooling water system 超高纯水ultra-high-purify water超过滤 ultrafiltration超过滤膜法ultrafiltration membrane process沉淀 precipitation, sedimentation沉淀池 sedimentation tank沉砂池 grit chamber城市废水 municipal wastewater城市废水处理 municipal wastewater treatment澄清clalification可持续发展sustainable development充满度 degree of fullness重现期 exceedion interval, period of recurrence抽风式机械通风冷却塔 induced draft mechanical cooling tower臭氧发生器 ozone generator臭氧法 ozonation process臭氧消毒 ozone disinfection初次(级)沉淀池 primary clarifier, primary sedimentation tank除水器 drift eliminator除铁除锰 iron and manganese removal除盐水(脱盐水) desalted water,demineralized water除渣 desilication, silica removal除藻 algal removal除氟 algal fluorine穿透曲线 penetration curve活性污泥法 activated sludge process生物脱氮工艺 biological nitrogen removal process船型一体化氧化沟 Boat Type in intrachannel clarifier oxidation ditch 纯(富)氧曝气法 pure-oxygen aeration process磁凝聚 magnetic coagulation磁盘法 magnetic disk process磁过滤法 magnetic fierration process萃取extraction萃取剂 extractantD达西定律Darcy’s law大肠菌群 Coliform-group bacteria大气泡曝气装置 large bubble aerator代谢 metabolism带式过滤 belt press filtration]单级传统消化池 single-stage conventional digester单螺旋式曝气装置 single spiral aerator氮 nitrogen氮循环 nitrogen cycle蛋白质 protein倒虹管 inverted siphon低放射性废物 low-level radio active waste制浆废水 kraft mill wastewater敌百虫dipterex敌敌畏dichlorvos涤纶纤维 polyester fiber地表漫流系统 overland flow system(OF)地表水 surface water地面（表）水环境质量标准 environmental quality standard for surface water 地下滤场 underground filtration field地下渗漏 underground percolation地下渗滤系统 subsurface infiltration system地下水 groundwater人工湿地系统artificial(constructed) wetland再生水回流地下水质标准 water quality standard for recharging parified wastewater water into groundwater aquifer地下水位 underground water level淀粉生产废水starch producing wastewater点滴-薄膜式淋水填料splash-film packing点滴式淋水填料splash packing点污染源 point pollufion source电动电位 electromotance potential电镀废水 electroplating wastewater电极 electrode电解法 electrolytical process电流密度 eletronic density电渗析 electrodialysis电渗析器 electrodialyzer电晕放电 brush discharge动态年成本 dynamic annual cost动植物油 oil and grease对硫磷parathion多层床 multibed多环芳烃 polycyclic hydracarban多氯联苯 polychlorinated biphenyls(PCBs)Dat－Ita 活性污泥法之一Decant 排水E二次(级)沉淀池secondary clarifier, secondary sedimentation tank二级处理secondary tratamentEceas 活性污泥法之一Escherichia Coli 大肠杆菌F乏燃料spent fuel反冲洗black washing反渗透（逆渗透）reverse osmosis反渗透法reverse osmosis process反渗透膜reverse osmosis membrane反硝化，脱氮denitrification防止腐蚀corrosion prevention纺丝spining纺织废水textile wastewater放射性半衰期radioactive half-life放射性废水处理radioactive wastewater treatment放射性排出物radioactive effluent非点源污染（面源污染）non-point source pollution非离子氨non-ionic ammonia废水处理wastewater treatment废水中和neutralization of wastewaters分离separation分流制separate system分流排水系统separated sewer system酚phenol焚烧incineration风吹损失windage loss风筒式冷却塔chimmey cooling tower封闭循环系统closed recirculation system氟化物fluoride辐射流沉淀池radial flow sedimentation tank浮盖式消化池floating-cover digester气浮flotation福斯特利帕除磷工艺Phostrip phosphorus removal process福列德克斯脱氮除磷工艺Phoredox nitrogen and phosphorus removal process 腐蚀corrosion富营养化eutrophication富营养化湖泊、水库eutrophic lake,eutrophic reservoirFlocculant 絮凝Gr射线 gamma rays甘蔗废水 sugarcane wastewater干化 drying干化床 drying bed冷却塔 cooling tower钢铁工业废水 iron and steel mill wastewater高纯水 ultrapure water高放废物 high-level radio active wastes高分子电解质 polymolecular electrolye高分子絮凝剂 polymolecular floc高负荷活性污泥法 high-loading activated sludge method高负荷生物滤池 high loading biological filter高炉煤气洗涤水 wastewater produced from scrubbing blast furnace top gas 高锰酸盐指数 potassium permanganate index高速消化池 high-rate digester高梯度磁分离器(HGMS) high grade magnegic separator高浊度水 high turbidity water格栅 bar screen隔板反应池 baffle reaction tank隔板式混合槽 baffle mixer隔油池 oil separator镉cadmium铬chromium给水泵站 water pumping station给水处理 water treatment给水网管系统 water supply system工业水处理与循环系统industrial water treatment and recirculation system 工业废水 industrial wastewater汞 mercury鼓风曝气 blast aeration鼓风式机械通风冷却塔 forced draft mechanical cooling tower固定螺旋式曝气装置 fixed spiral aerator景观、娱乐水体landscape and recreation waterbody管道接口 conduit joint给水配水系统 water supply piping distribution system 网管平差 balancing netwok罐头生产废水 Cannery wastewater硅藻土 cilicious marH海水淡化 demineralization of sea water含酚废水 phenol contained wastewater含水量moisture content含盐量saline capacity含油废水 oily wastewater旱流污水量(DWF) dry-weather flow好氧生物处理 aerobic biological treatment好氧塘aerobic pond好氧稳定 aerobic stabilization合成洗涤剂 synthetic detergent合成纤维 synthetic fiber合成纤维废水 synthetic fiber wastewater合成橡胶 synthetic rubber合流城市废水 combined municipal wastewater合流制排水系统 combined sewer system水体功能分类 waterbody function classification核能工厂 nuclear power station核燃料循环 nuclear fuel cycle核素nuclide冶金工业废水 metallurgical industry wastewater黑液 black liquor黑液除硅 sillica-elimination from black liquid虹吸滤池 siphon filter化学处理 chemical treatment化学工业 chemical industry化学吸附 chemical adsorption化学纤维 chemical fiber化学需氧量 chemical oxygen demand (COD)环状管网系统 grid pipe network system缓蚀 corrosion inhibition缓蚀剂corrosion inhibitor磺化煤sulfonated coal挥发酚volatile phenol回流比recycle ratio回流污泥率 return sludge ratio汇水面积 catchment area, collection area混合 mixing混合床 miced bed混合液挥发性悬浮固体 mixed liquor volatile suspended solids(MLVSS)混合液悬浮固体 mixed liquor suspended solids(MLSS)混凝 coagulation混凝沉淀 coagulation-sedimentation混凝剂 coagulant浑浊度 tubidity活化产物 activation products硅酸钠 sodium silicate活性剂 activator活性染料 active dye活性炭 activated carbon活性炭的再生 re-generation of activated carbon活性炭吸附 active carbon adsorption活性污泥activated sludge活性污泥法 activated sludge process活性污泥负荷 activated sludge loading活性污泥驯化 acclimation of activated sludgeIdle 闲置Legionella 军团杆菌Oxidation ditch 氧化沟, 又名连续循环曝气池（Continuous loop reactor）Ritilä格栅？SBR(Sequencing Batch Reactor Activated Sludge Process) 序列间歇式活性污泥法Settle 沉淀Unitank活性污泥法之一污水处理技术知识目前，国内外城市污水处理厂处理工艺大都采用一级处理和二级处理。

污水处理中英文名词对照表

RO RS RSSS RSV SBR SDI
Reverse Osmosis Return Sludge Return Sludge Suspended Solid Return Sludge Volume Sequencing Batch Reactor Sludge Density Index
SRT SS SV SVI TNT TOC TOD TN TKN TP TS TPM UASB UBF UCT UF UNITANK UV UV-A UV-B UV-C VFA VIP VS VSS
AB ABF AF ALK A/O A/O A2/O
Adsorption Biodegradation Activated Bio-filter Advanced Treatment Anaerobic Filter Alkali Anoxic/Oxic Anaerobic/Oxic Anaerobic/Anoxic/Oxic Bardenpho
Benzo（a）pyrene Bio- chemical Oxygen Demand Butylated Hydroxytoluene Carrousel
CASP CASS CAST CFS COD
Cyclic Activated Sludge process Cyclic Activated Sludge System Cyclic Activated Sludge Technology Continuous Flow System Chemical Oxygen Demand Cross-flow Demand Aeration Tank-Intermittent Aeration Tank Dead-end N，N-Diethyl-p-Phenylene Diamine Dissolved Solid

污水处理专用术语翻译

1,Regulating Pool 调节池2, Pumping Station 提升泵房3, Anaerobic Tank 厌氧池4, Facultative Tank 兼氧池(翻译把兼氧好氧池分开了) 5, Aerobic Tank 好氧池6, Biochemical Sedimentation Tank 生化沉淀池7, Reaction Tank 反应池8, Physical and Chemical Sedimentation Tank 物化沉淀池9, Fan Room 风机房10, Sludge Pool 污泥池11, The Sludge Concentration Pool 污泥浓缩池12, Sludge Dewatering Room 污泥脱水间Cids 酸Process Flow Chart 工艺流程图Wastewater 废水Emission On Standard 达标排放Overflow Into The Regulating Pool 溢液进调节池Sludge transport污泥外运Biogas 沼气Agent 药剂Bar Screen格栅Returned Slude污泥回流Boiler Room 锅炉房Switching Room 配电室Add The Pharmacy 配药间Office Lab 办公化验室Legend 图例Filter Press 板框压滤机Temperature（温度）pH(pH值)BOD5 at 20°C（五日生化需氧量）Total nitrogen (as N)（总氮）COD (mg O2 /l)（化学需氧量）Total phosphorus (as P)（总磷）Suspended solids （悬浮物SS）Total ammonia (as N) （总氨氮）Oils, fats & grease （动植物油类）Phenols （酚类）Mercury (as Hg)（汞）Nickel (as Ni)（镍）Cobalt (as Co)（钴）Lead (as Pb)（铅）Antimony (as Sb)（锑）Tin (as Sn)（锡）Chromium (as Cr VI)（六价铬）Chromium (as total Cr) （总铬）Arsenic (as As)（砷）Cadmium (as Cd)（镉）Zinc (as Zn)（锌）Copper (as Cu)（铜）"Mineral oils (Interceptors)（物理处理出水矿物油）" "Benzene, toluene & xylene (combined)（苯、甲苯、二甲苯总量）"Mineral oils (Biological Treatment)（生物处理出水矿物油）""Organochlorine pesticides (as Cl) （有机氯农药）" "Mothproofing agents (as Cl) (防蛀剂)""Organophosphorus pesticides (as P) （有机磷农药）" Adsorbable organic halogen compounds (AOX)（可吸附有机卤化物Sulphide(asS)（硫化物）Color (dilution ratio)（色度稀释倍数）Particulate matter（粉尘）Volatile organic carbons (as C) (excluding formaldehyde)（挥发性有机碳，不包含甲醛）Formaldehyde（甲醛）Isocyanates (as NCO)（异氰酸酯）Cyanide(氰化物)Silver总银Manganese总锰Selenium总硒Benzopyrene苯并芘Aniline苯胺类Nitrocompound总硝基化合物Malathion马拉硫磷Dimethoate乐果Parathion对硫磷Parathion-methyl甲基对硫磷Pentachlorophenol五氯酚Trichloromethane三氯甲烷Tetrachloromethane四氯甲烷Trichloro ethylene三氯乙烯Tetrachloroethylene四氯乙烯Close Xylene邻–二甲苯Face Xylene对–二甲苯Space Xylene间–二甲苯Ethylbenzene乙苯Chlorobenzene氯苯1,4-Dichlorobenzene1,4–二氯苯P-nitrchlorobenzene对硝基氯苯"2,4-Dinitrochlorobenzene2,4–二硝基氯苯"Phenol苯酚Space Cresol间–甲酚2,4-Dichlorophen2,4–二氯酚"2,4,6-Trichlorophenol2,4,6–三氯酚""Phthalic acid Dibutyl ester邻苯二甲酸二丁酯""Phthalic acid Dioctyl phthalate邻苯二甲酸二辛酯"Acrylonitrile丙烯晴给排水常用名词中英文对照1、给水工程water supply engineering 原水的取集和处理以及成品水输配的工程。

污水处理英语词汇

污水处理英语词汇AA/A/O法anaerobic-anoxic-oxic process(厌氧-缺氧-好氧法)A-A-O生物脱氮除磷工艺A-A-O biological nitrogen and phosphorus removal processA-O脱氮工艺 A-O nitrogen removal processA-O除磷工艺 A-O phosphorus removal processAB法 Adsorption Biodegradation process(吸附生物降解法)总a放射线 Total a radioactivity氨氮 ammonia-nitrogen氨基酸 amino acid氨化反应 Nitragen铵盐 ammonium saltA/O法(厌氧-好氧法) anaerobic-oxic process奥贝尔(Orbal)型氧化沟Orbal oxidation ditchB巴登福脱氮除磷工艺Ｂardenpho nitrogen and phosphorus removal process白水(漂洗废水) whitewater(bleaching water)板框压滤 plate pressurefiltration离心机 centrifugalmachine半渗透膜semi-permeable membrane棒状杆菌属corynebacterium薄膜式淋水填料 filmpacking饱和常数(Ks) saturationconstant暴雨公式 storm flowformula暴雨径流 storm runoff溢流井 overflow well苯 benzene苯胺 aniline总B放射性 Total Bradioactivity泵型叶轮暴气器 paddleimpeller aerator泵站 pumping stationBMTS型一体化氧化沟BMTS intrachannel clarifieroxidation ditch闭路循环 closed loop表面冲洗 surfacewashing表面负荷 surface load表面过滤 surfacefiltration表面活性剂 surfactant表面活性物质 surfaceactive additive agent表面曝气 surfaceaeration表面曝气器 surfaceaerator表面淹灌 surface floodirrigation表面冲洗装置 surfacewashing facility丙烯酸 acrylic acid丙烯腈 acrylonitrile病毒 virus病原菌(致病菌) pathogen病原微生物 pathogenmicroorganismBOD-污泥负荷BOD-sludge load补充水 make-up water布朗运动 BrownianmovementC财务评价 financial evaluation配水系统 distribution system侧渠型一体化氧化沟integrated oxidation ditch with side ditch产氢气乙酸菌Rydrogenes and acetic aid genes产甲烷细菌methanogenes产率系数 yield coefficient常规给水处理工艺conventional water treatment processes敞开式循环冷却水系统opened recirculating cooling water system超高纯水ultra-high-purify water超过滤 ultrafiltration超过滤膜法ultrafiltration membrane process沉淀 precipitation, sedimentation沉淀池 sedimentation tank沉砂池 grit chamber城市废水 municipalwastewater城市废水处理 municipalwastewater treatment澄清 clalification可持续发展 sustainabledevelopment充满度 degree offullness重现期 exceedioninterval, period ofrecurrence抽风式机械通风冷却塔induced draft mechanicalcooling tower臭氧发生器 ozonegenerator臭氧法 ozonationprocess臭氧消毒 ozonedisinfection初次(级)沉淀池 primaryclarifier, primarysedimentation tank除水器 drift eliminator除铁除锰 iron andmanganese removal除盐水(脱盐水) desaltedwater,demineralized water除渣 desilication,silica removal除藻 algal removal除氟 algal fluorine穿透曲线 penetrationcurve活性污泥法 activatedsludge process生物脱氮工艺biological nitrogen removalprocess船型一体化氧化沟 BoatType in intrachannelclarifier oxidation ditch纯(富)氧曝气法pure-oxygen aeration process磁凝聚 magneticcoagulation磁盘法 magnetic diskprocess磁过滤法 magneticfierration process萃取 extraction萃取剂 extractantD达西定律 Darcy’s law大肠菌群Coliform-group bacteria大气泡曝气装置 largebubble aerator代谢 metabolism带式过滤 belt press filtration]单级传统消化池single-stage conventional digester单螺旋式曝气装置single spiral aerator氮 nitrogen氮循环 nitrogen cycle蛋白质 protein倒虹管 inverted siphon低放射性废物 low-level radio active waste制浆废水 kraft mill wastewater敌百虫 dipterex敌敌畏 dichlorvos涤纶纤维 polyester fiber地表漫流系统 overland flow system(OF)地表水 surface water地面（表）水环境质量标准 environmental quality standard for surface water地下滤场 underground filtration field地下渗漏 underground percolation地下渗滤系统subsurface infiltrationsystem地下水 groundwater人工湿地系统artificial(constructed)wetland再生水回流地下水质标准water quality standard forrecharging parifiedwastewaterwater into groundwateraquifer地下水位 undergroundwater level淀粉生产废水 starchproducing wastewater点滴-薄膜式淋水填料splash-film packing点滴式淋水填料 splashpacking点污染源 pointpollufion source电动电位electromotance potential电镀废水electroplating wastewater电极 electrode电解法 electrolyticalprocess电流密度 eletronicdensity电渗析 electrodialysis电渗析器electrodialyzer电晕放电 brushdischarge动态年成本 dynamicannual cost动植物油 oil and grease对硫磷 parathion多层床 multibed多环芳烃 polycyclichydracarban多氯联苯polychlorinatedbiphenyls(PCBs)E二次(级)沉淀池secondary clarifier,secondary sedimentation tank二级处理 secondarytratamentF乏燃料spent fuel反冲洗black washing反渗透（逆渗透）reverse osmosis反渗透法reverseosmosis process反渗透膜reverse osmosis membrane反硝化，脱氮denitrification防止腐蚀corrosion prevention纺丝spining纺织废水textile wastewater放射性半衰期radioactive half-life放射性废水处理radioactive wastewater treatment放射性排出物radioactive effluent非点源污染（面源污染）non-point source pollution非离子氨non-ionic ammonia废水处理wastewater treatment废水中和neutralization of wastewaters分离separation分流制separate system分流排水系统separated sewer system酚phenol焚烧incineration风吹损失windageloss风筒式冷却塔chimmey cooling tower封闭循环系统closedrecirculation system氟化物fluoride辐射流沉淀池radialflow sedimentation tank浮盖式消化池floating-cover digester气浮flotation福斯特利帕除磷工艺Phostrip phosphorus removalprocess福列德克斯脱氮除磷工艺Phoredox nitrogen andphosphorus removal process腐蚀corrosion富营养化eutrophication富营养化湖泊、水库eutrophic lake,eutrophicreservoirGr射线 gamma rays甘蔗废水 sugarcanewastewater干化 drying干化床 drying bed冷却塔 cooling tower钢铁工业废水 iron andsteel mill wastewater高纯水 ultrapure water高放废物 high-levelradio active wastes高分子电解质polymolecular electrolye高分子絮凝剂polymolecular floc高负荷活性污泥法high-loading activatedsludge method高负荷生物滤池 highloading biological filter高炉煤气洗涤水wastewater produced fromscrubbing blast furnace topgas高锰酸盐指数 potassiumpermanganate index高速消化池 high-ratedigester高梯度磁分离器(HGMS)high grade magnegic separator高浊度水 high turbiditywater格栅 bar screen隔板反应池 bafflereaction tank隔板式混合槽 baffle mixer隔油池 oil separator镉 cadmium铬 chromium给水泵站 water pumping station给水处理 water treatment给水网管系统 water supply system工业水处理与循环系统industrial water treatment and recirculation system工业废水 industrial wastewater汞 mercury鼓风曝气 blast aeration鼓风式机械通风冷却塔forced draft mechanical cooling tower固定螺旋式曝气装置fixed spiral aerator景观、娱乐水体landscape and recreation waterbody管道接口 conduit joint给水配水系统 water supply piping distribution system网管平差 balancingnetwok罐头生产废水 Cannerywastewater硅藻土 cilicious marH海水淡化demineralization of sea water含酚废水 phenolcontained wastewater含水量 moisture content含盐量 saline capacity含油废水 oilywastewater旱流污水量(DWF)dry-weather flow好氧生物处理 aerobicbiological treatment好氧塘 aerobic pond好氧稳定 aerobicstabilization合成洗涤剂 syntheticdetergent合成纤维 syntheticfiber合成纤维废水 syntheticfiber wastewater合成橡胶 syntheticrubber合流城市废水 combinedmunicipal wastewater合流制排水系统combined sewer system水体功能分类 waterbodyfunction classification核能工厂 nuclear powerstation核燃料循环 nuclear fuelcycle核素 nuclide冶金工业废水metallurgical industrywastewater黑液 black liquor黑液除硅sillica-elimination fromblack liquid虹吸滤池 siphon filter化学处理 chemicaltreatment化学工业 chemicalindustry化学吸附 chemicaladsorption化学纤维 chemical fiber化学需氧量 chemicaloxygen demand (COD)环状管网系统 grid pipenetwork system缓蚀 corrosioninhibition缓蚀剂 corrosion inhibitor磺化煤 sulfonated coal挥发酚 volatile phenol回流比 recycle ratio回流污泥率 returnsludge ratio汇水面积 catchment area, collection area混合 mixing混合床 miced bed混合液挥发性悬浮固体mixed liquor volatile suspended solids(MLVSS)混合液悬浮固体 mixed liquor suspendedsolids(MLSS)混凝 coagulation混凝沉淀coagulation-sedimentation混凝剂 coagulant浑浊度 tubidity活化产物 activation products硅酸钠 sodium silicate活性剂 activator活性染料 active dye活性炭 activated carbon活性炭的再生re-generation of activatedcarbon活性炭吸附 activecarbon adsorption活性污泥 activatedsludge活性污泥法 activatedsludge process活性污泥负荷 activatedsludge loading活性污泥驯化acclimation of activatedsludgeJ机械反应池 mechanicalreactor机械剪切曝气装置mechanical shearing aerator机械搅拌 mechanicalmixing机械搅拌澄清池accelerator机械曝气 mechanicalaeration机械通风冷却塔mechanical draft coolingtower机械脱水 mechanicaldewatering极化现象 polarization级配 granularcomposition集水池 collection well集中处理(合并处理)joint treatment计算机 computer计算机辅助设计computer aid design加速过滤器accelo-filter加压气化pressure-gasification甲基对硫磷 parathionmethyl甲醛 formaldehyde甲烷 methane甲烷发酵 methanefermentation甲烷气体 methane gas间歇式活性污泥系统sequencing batch reactoractivated sludge system(SBR)蒹性塘 facultative pond检查井 manhole减压薄膜蒸发法decreasing pressure andthin-film evaporation process碱法制浆 soda pulping process浆粕 pulp降雨历时 duration of rainfall降雨量,降水precipitation浇洒道路用水 street flushing water焦化废水 coking wastewater交替工作式氧化沟alternative operating oxidation ditch交替运行的生物滤池alternative operating trickling filter胶体 colloid阶段曝气 step aeration接触池 contact chamber接触氧化法 contact oxidation process结垢 scale节水 water saving锦纶纤维 polyamide fiber腈纶纤维 acrylic fiber精制塘(深度处理塘)polishing pond经济效益 economicbenefit径流系数 runoffcoefficent静态年成本 staticannuity cost景观娱乐用水水质标准water quality standard forlandscape and recreation area酒精工业 alcoholdistilery就地处理系统(小型处理)on-site treatment systems(small scale facilities)聚丙烯酰胺polyacrylamide聚丙烯酰胺水解体polyacrylamide hydrolysisproduct聚合 polymerize聚合度 polymerizingdegree聚合氯化铝polyaluminum chloride均衡池(塘) equalizaliontank(basin,lagoon)K卡罗塞式氧化沟Corrousel oxidation ditchK型叶轮曝气机 K typeimpeller aerator凯式氮 kjeldahlnitrogen空气驱动式生物转盘aero biological disks孔隙率 porosity快滤池 rapid filter快速渗滤系统 rapidinfiltration system(RI)矿井 shaft(mine)矿区 mining area矿区环境 mining areaenvironment矿山废水 minerywasterwater矿山酸性废水 acid minewastewater扩散板 diffusion plate扩散管 diffusion tube扩散盘(罩) diffusiondisc(cover)L乐果 dimethoate冷凝 condensation冷凝水 condensate water冷却 cooling冷却池 cooling pond冷却塔 cooling tower冷却塔配水系统 cooling tower distribution system冷却循环水 circulated cooling water冷轧 cold steel-rolling离心泵 centrifugal pump离心 centrifugation force离心机 centrifugal machine离心脱水 centrifugal dewatering离心作用centrifugation离子交换 ion exchange离子交换剂 ion exchanger离子交换膜 ion exchange membrane离子交换树脂 ion exchange resin粒径 grain size砾石承托层 gravel support炼钢厂废水steel-making process wastewater炼铁 iron-smelting炼铁(高炉)废水 blastfurnace wastewater炼油厂废水 refineryprocessing waserwater淋滤 leaching淋水密度 waterdrenching density淋水面积 waterdrenching aera淋水填料 packing磷 phosphorus磷酸盐 phosphate生物流化床 Biologicalfluidized bed硫化物 sulphide硫化物沉淀法precipitation with sulphide硫酸铵 ammonium sulfate硫酸钙 Calcium sulfate硫酸铝 aluminum sulfate硫酸镁 magnesiumsulfate硫酸铁 ferric sulfate硫酸亚铁 ferroussulfate硫酸盐 sulfate硫循环 sulphur cycle铝酸钠 sodium aluminate滤层 filter layer滤池冲洗水量 filterwashing water consumption滤池配水系统 filterunderdrain system滤池运行周期 filtercycle time滤床 filter bed滤料 filtering medium滤速 filtration rate滤液 filtrate氯 chlorine氯-氨法chlorine-ammonia process氯化,加氯处理chlorination氯化物 Chlorides螺旋桨式快速搅拌机propeller-type high speedagitatorM马拉硫磷 malathion脉冲澄清池 pulsator慢滤池 slowfilter慢速渗滤系统 slow rate infiltration system (SR)煤气 coal gas煤气厂 gas work煤气发生器 coal gas generator煤气发生站 gas generation station煤气净化 coal gas purification煤炭 coal锰 manganse米门公式 Michaelis - Menten equation莫诺德公式 Monod equation密闭式循环冷却水系统closed recirculating cooling water system密集多喷嘴曝气装置compact multinozzle aerator面污染源 non-point pollution source敏感性分析 sensitivity analysis膜分离装置 membrane seperator膜选择性 membrane selectivity膜污染 membranefoulting膜中毒 membranepoisoningN难生物降解有机物nonbiodegradable organies尼龙 nylon逆流漂洗counter-current washing逆流式冷却塔counterflow cooling tower逆流再生counter-current regeneration粘胶 rayon酿酒废水 winerywastewater酿造与发酵工业废水brewery and fermentationindustrial wastewater凝聚 coagulation凝聚剂 coagulant牛奶生产废水 dairywastewater浓缩 concentration浓缩倍数 cycle ofconcentration浓缩池 thickening tank浓缩污泥 concentratedsludge农田灌溉水质标准standards for irrigationwater quality农用污泥中污染物控制标准 contaminants controlstandard for sludge farming农药 pesticide农药厂废水 pesticideplant wastewaterP排泥系统 sludge -discharge system排水量 discharge排水管 drain pipe排水口 outlet排水系统 sewer system排污 blowdown泡沫分离 foam phaseseparation配水网管 distributionsystem ,pipe system喷灌 spray irrigation喷水池 spray pond皮革 leather啤酒废水 brewerywastewater啤酒废水处理 brewery wastewater treatment漂白 bleaching平板式膜 plate membrane平板式叶轮曝气器 plate impellar aerator平衡吸附容量equilibrium adsorption capacity平流式沉砂池horizontal flow grlt removal tank平流式沉淀池horizontal flow sedimentation tank普通生物滤池biological filter,trickling filter曝气 aeration曝气沉砂池 aerationgrit chamber曝气池 aeration tank曝气栅 aeration boom曝气设备 aeration equipment曝气时间 aeration time曝气装置,曝气机aerator居民生活垃圾 HouseholdWaste庫底平整線 bottom flattingline of the site庫區填埋邊線 landfill sideline of the site庫容 Storage capacity垃圾 Waste ，Solid Waste垃圾壩 waste dam垃圾殘渣 residue垃圾槽 waste chute垃圾層 waste layer垃圾產量 Waste output垃圾堆肥場 waste compostingfield垃圾堆體 waste pile垃圾副壩 secondary waste dam垃圾揀選場 Waste SortingSite垃圾氣化 waste gasification垃圾收集車 waste collector垃圾桶 garbage ，rubbishbarrel垃圾箱 garbage container垃圾壓實系統 wastecompactor system垃圾衍生燃料 Refuse-derivedfuel (RDF)垃圾衍生燃料 waste derivedfuel垃圾轉運車 waste transfertruck垃圾轉運站 waste transferstation垃圾裝卸坡 waste loadingramp離心脫水機 centrifugaldewaterer鈉基膨潤土 sodium bentonite農業廢棄物 AgriculturalWaste濃縮池 thickening tank排放 discharge排泥閥 sludge valve排水口 Drain Outlet膨潤土 bentonite熱解 Pyrolysis溶解氧測定儀（DO計）dissolved oxygen meter（DOmeter）砂水分離機 grit-watersplitter商業垃圾 Commercial Waste上橫沖填埋場 ShanghengchongLandfill Site上清液 supernatant liquor設備選型 Type selection ofequipment滲濾液（垃圾滲濾液） leachate滲濾液處理 leachatetreatment滲濾液處理站 LeachateTreatment Station滲濾液收集及導排氣系統平面圖 Plan of LeachateCollection and Guiding andExhaust System滲濾液收集盲溝 blind drainfor leachate collection生活垃圾 Domestic waste生活垃圾焚燒污染控制標准Standard for PollutionControl on the MunicipalSolid Waste Incineration剩余污泥 excess sludge剩余污泥泵 excess sludgepump輸渣機 clinker conveyer豎向石籠 vertical stone cage雙層防滲結構 double-linersystem水位 water level提升泵站 lift pumpingstation填埋（垃圾） Landfill填埋場 Landfill site填埋場封場 seal of landfillsite填埋場總體布置圖 General Layout of Landfill Site填埋場縱斷面示意圖 Sketch Map of Landfill Site Vertical Section填埋庫區 Landfill Area填埋庫區平面布置圖 Plane Layout of Landfill Area1:1000填埋氣 Landfill gas砼 concrete圖例 legend土工合成材料粘土墊層Geosynthetics Clay Liner (GCL)土工膜 geomembrane脫水機 dewaterer脫水機房 dewatering house衛生填埋 sanitary landfill 渦流沉砂池（旋流沉砂池）vortex grit tank污泥泵房 sludge pumping room 污泥處理 sludge treatment污泥處理流程示意圖 Flow Chart of Sewage Treatment Process污泥管線 sludge pipeline污泥濃度計（MLSS計） sludge concentration meter（MLSS meter）污泥濃縮及脫水機房 Sludge Thickening & Dewatering House污泥脫水車間 sludge dewatering workshop污水泵 sewage pump污水處理 sewage treatment污水處理厂 Wastewater Treatment Plant污水處理流程示意圖 Sewage Treatment Process Sketch Map 污水管線 sewage pipeline污水水面 wastewater surface 無線傳輸 wireless transmission吸水井 suction well消毒池 disinfecting tank新聯村熊家窯 Xiongjiayao, Xinliancun序批式活性污泥法（SBR法）Sequence Batch Reactor選型 Type selection壓縮式垃圾車 waste compactors厭氧、缺氧、好氧 Anaerobic, Anoxic, Aerobic Underwater Blender厭氧堆肥 anaerobic composting厭氧發酵 methane fermentation; anaerobic fermentation厭氧流化床反應器 anaerobic fluidized bed厭氧流化床反應器 anaerobic fluidized bed氧化溝 oxidation ditch氧化溝 oxidation ditch葉輪曝氣機 impeller aerator 一級發酵（初級發酵） primary fermentation醫院垃圾 Hospital Waste營養土層 nutritious soil layer預留垃圾綜合利用生產用地Reserved Waste Comprehensive Utility and Production Land 再生 reclamation柵渣 sediment粘土層 clay layer支盲溝 blind sub-drain至垃圾填埋場 to the waste landfill site終期覆土 terminal earth covering主盲溝 main blind drain自控系統 autonomous system 自然土層 natural soil layer。

翻译硕士(MTI)考研必备：常见词汇表-W

翻译硕士（MTI）考研必备：常见词汇表－W小编网上查找中国日报常用词汇表A－Z，希望对大家词汇掌握有所帮助。

以下为汉语W开头的单词，希望大家认真记忆。

挖墙脚undermine the foundation of sth.; cut the ground from under sb's feet歪风邪气unhealthy practices and evil phenomena/外层空间outer space/外汇储备foreign exchange reserve (forex reserve)/外汇管理局Administration of Exchange Control外汇管制foreign exchange control外交庇护diplomatic asylum/外交斡旋diplomatic offices/外联网(计算机) extranet/外卖take-out外卖店take-out restaurant外贸单证员vouching clerk/外贸自营权power to engage in foreign trade/外企foreign company/外税局foreign-related tax bureau外滩(上海) The Bund外逃资本flight capital/外向型经济export-oriented economy外星人extraterrestrial being (ET)外需overseas market demand/外债foreign debt; external debt/顽固分子die-hard/万维网(计算机) World Wide Web(WWW)/汪辜会谈Wang Daohan-Koo Chen-fu Talks (Wang-Koo talks)王储，王太子Crown Prince王水aqua regia网吧Internet bar网虫netter; Internet geek网关gateway网恋online love affair网络出版online publishing网络管理员network administrator网络化networking网络经济cybereconomy网络恐怖主义cyberterrorism网络摄象机web cam网民netizen; net citizen; cyber citizen网上冲浪surf the Internet网上交易平台online trading platform网友net friend往返机票return ticket; round-trip ticket/往事如风The past has vanished (from memory) like wind.; What in past, is past.望子成龙hold high hopes for one's child/危房dilapidated building/威武之师,文明之师mighty force and civilized force/微软公司Micorsoft Corporation/微软移动构想Microsoft Vision for Mobility; Microsoft Mobility Initiatives违反合同breach of contract/围城》A Surrounded City围垦造田enclose tideland for cultivation; reclaim land from marshes唯利是图draw water to one's mill唯一致命的弱点Achilles' heel维护人权和不断改善人权状况safeguard human rights and steadily improve the human rights situation伪君子hypocrite; a wolf in sheep's clothing伪劣商品赔还法lemon law卫冕世界冠军reigning world champion卫星城satellite town/卫星导航satellilte navigation/慰安妇comfort woman/温饱工程Adequate Food and Clothing Program/温饱工程bring-warmth fill-bellies project温室气体greenhouse gases/文化产业culture industry/文化旅游culture-oriented travel/文科liberal arts文明街道model community文韬武略military expertise; military strategy纹身tattoo/稳定物价stabilize prices/稳定压倒一切Maintaining stability is of top priority问讯处information office; inquiry desk我们在国际上说话是算数的We always live up to our international commitments./乌拉圭回合Uruguay Round乌龙球own goal/污染指数pollution index/污水处理sewage treatment/ disposal/凯程2016年集训营考取北京地区翻译硕士学员30多人，成功率85%以上！屋顶花园broof garden屋漏又逢连阴雨Misfortunes never come singly. When it rains it pours./无风不起浪There are no waves without wind. There's no smoke without fire./无氟冰箱Freon-free refrigerator无公害蔬菜green vegetable/无力偿付的公司insolvent corporation/无人售票self-service ticketing无绳来电显示电话ordless telephone with caller ID无土栽培soil-less cultivation无为而治govern by doing nothing that is against nature; govern by non-interference无线应用协议W AP（wireless application protocol）无息贷款interest-free loan/无形资产intangible assets无形资产intangible assets; immaterial property/无源雷达passive radar/无源之水,无本之木water without a source, and a tree wiithout roots/无中生有make/create something out of nothing五保户household enjoying the five guarantees (childless and infirm old persons who are guarateed food, clothing, medical care, housing and burial expenses)/五讲四美三热爱the movement of five stresses, four points of beauty and three loves(The five stresses are: stress on decorum, manners, hygiene, discipline and morals. The four points of beauty are: beauty of the mind, language, behavior adn the enviornment. The three loves are: love of the motherland, socialism and the Communist Party.)/ 文联literary federation五金化工metals and chemicals武侠小说tales of roving knights; martial arts novel; kung fu novel物价局Price Bureau物流logistics; the interflow of goods and materials/物人human vegetable; vegetable物业管理estate management, property management物以类聚，人以群分Birds of a feather flock together./物质文明material progress/物质文明建设和精神文明建设一起抓pay attention to ethical as well as material progress/物种起源origin of species/凯程教育：凯程考研成立于2005年，国内首家全日制集训机构考研，一直从事高端全日制辅导，由李海洋教授、张鑫教授、卢营教授、王洋教授、杨武金教授、张释然教授、索玉柱教授、方浩教授等一批高级考研教研队伍组成，为学员全程高质量授课、答疑、测试、督导、报考指导、方法指导、联系导师、复试等全方位的考研服务。

中山大学翻译硕士MTI真题及答案

中山大学翻译硕士MTI真题及答案I. Phrase Translation1. 多边合作：multilateral cooperation2. 可持续发展：sustainable development3. 试行阶段：pilot phase4. 应急计划: contingency plan5. 污水处理: sewage treatment6. 全球变暖: global warming7. 新闻发布会: press conference; news briefing8. 市场占有率: share of market; market share9. 研发中心: RD center ( research and development center )10. 跨国犯罪: transnational crime11. 企业文化: enterprise culture ; corporate culture12. 八国峰会: G8 summit ; Group 8 Summit13. 数字鸿沟: digital divide14. 危害品贩运: drug trafficking15. 国有企业: state-owned enterprise16. brand loyalty: 品牌忠诚度17. corporate governance: 公司治理;企业管治18. corporate social responsibility: 企业社会责任19. proliferation of weapons of mass destruction: 大规模杀伤性武器扩散20. global sourcing: 全球采购21. HSBC: 汇丰银行(Hongkong and Shanghai Banking Corporation)22. carbon trading: 碳交易;碳贸易23. deforestation: 滥伐森林; 森林砍伐; 滥砍滥伐24. due diligence: 尽职调查25. code of conduct: 行为准则;行为规范26, market positioning: 市场定位27. cradle of human civilization: 人类文明发源地28. anti-dumping measures: 反倾销措施29. time to market: 上市时间; 上市时机(一个新产品从构思到实际推入市场所用的时间)30. alternative energy: 替代能源;可替代能源II. Passage translationSection A Chinese to English广交会品牌展区是鼓励和引导企业转变外贸发展方式的重要示范平台。

废水零排放英文术语

废水零排放英文术语一、Zero Liquid Discharge (ZLD)零液体排放是指将生产过程中产生的所有废水、废液全部或按需求进行回收再利用，或者通过适当的处理措施，使其最终以固体形式排出，而不会产生任何外排的废水处理方式。

这一概念在减少环境污染和提高水资源的可持续利用方面具有重要的意义。

二、Wastewater treatment废水处理是指利用物理、化学和生物方法去除废水中的各种有害物质，以达到排放标准或回收利用的目的。

废水处理的方法有很多种，包括沉淀、过滤、吸附、生物处理等。

三、Membrane technology膜技术是一种分离技术，通过膜过滤实现固液分离、气体分离、有机物和无机物的分离等。

在废水处理领域，膜技术常用于超滤、纳滤和反渗透等方面，能够高效去除废水中的杂质和有害物质。

四、Evaporation and crystallization蒸发结晶是指通过加热或真空蒸发的方式使废水中的水分以蒸汽形式逸出，而盐类和其他溶解物质则以结晶形式析出。

这一技术适用于处理高盐度的废水，能够有效回收有用物质，减少废物产生。

五、Recycling and reuse回收再利用是指将废水经过适当处理后再次用于生产过程中，以达到节约水资源的目的。

废水回收再利用可以减少新鲜水的使用量，降低生产成本，同时减少废水的排放量。

六、Solids handling and disposal固体废弃物的处理是指对废水处理过程中产生的污泥和其他固体废物进行处置的过程。

处理方法包括脱水、焚烧、填埋等，应根据废物的性质和数量选择合适的处理方式。

七、Environmental regulations and standards环境法规和标准是指为保护环境而制定的法律、行政法规、部门规章、地方法规和地方政府规章等规范性文件，以及环境质量标准和污染物排放标准等。

这些法规和标准对废水处理和排放提出了明确的要求和限制，是实现废水零排放的重要保障。

环境工程专业英语翻译Unit 10-16 (A4)

Unit 10 水污染与治理1854年英国伦敦爆发了大规模的流行性霍乱。

此事明确地证实了污水和疾病之间的关系。

当初以公共健康为目的所采取的污染控制，依然是许多地区的主要目的。

然而，水资源的保持，产鱼区的防护，以及娱乐活动用水的维持在今天也成为关注的焦点。

紧随第二次世界大战之后所产生的城市人口密度突增和工业化进程的加剧，都使得水污染问题越见明显。

致使对于水污染的关注程度在70年代中期达到了顶峰。

水污染是一个不准确的术语，它并未指出污染物的种类和来源。

而我们处理废水问题的方式往往取决于以下几个方面：污染物是否需要氧气，是否助长藻类，是否有传染性，是否有毒，或者仅仅是否好看。

水源的污染可能直接来自生活污水的排放或工厂污水排放（点源），也可能间接地由空气污染、农业排水或城市排水（非点源）所引发。

化学上所谓的纯水仅仅是水分子的集合。

无论在野外的河流或湖泊、云层或雨水中，还是在下雪期间，极地的冰帽地区，这种物质在自然界均不能找到。

然而在实验室中可以制备非常纯净的水，但是存在一定的困难。

因为水极易接受和容纳外来物质。

城市污水，也被称作生活污水，是一种复杂的混合物。

它包含水（通常超过99％）以及悬浮或溶解的有机和无机污染物。

这些污染物的浓度通常很低并且以mg/L来表示，也就是说，每升混合物含有多少毫克污染物。

重量与体积比也常用来表示在水、废水、工业废水和其它稀释溶液中的污染物浓度。

微生物任何地方只要存在适合的食物，充足的湿度和适当的温度，微生物即可大量繁殖。

而生活污水为各种各样的微生物提供了一个理想的环境。

这些微生物主要是细菌，某些病毒和原生动物。

废水中的大多数微生物是无害的，并且可借助生化过程，将有机物转化为稳定的最终产物。

但是当一些人患有可通过有毒废水传播的传染性疾病时，其排泄物所携带的致病病原体，极有可能成为污水的组成部分。

虽然在发达国家，类似于水传播的细菌性疾病，例如霍乱、伤寒和肺结核，病毒性疾病例如传染性的肝炎和原生虫引起的痢疾，已经不再是问题，但是在那些经过适当处理过的污水不能被公共利用的地区仍然存在着很大威胁。

水处理专业术语中英文翻译氧化塘生物膜法离子交换广州清都环保

水处理术语中英文翻译表广州清都环保工业循环冷却水处理设计规范Code for design of industrial recirculating cooling water treatment1、循环冷却水系统Recirculating cooling water system2、敞开式系统Open system3、密闭式系统Closed system4、药剂Chemicals5、异养菌数Count of heterotrophic bacteria6、粘泥Slime7、粘泥量Slime content8、腐蚀率Corrosion rate9、系统容积System capacity volume10、预膜Prefilming11、旁流水Side stream12、补充水量Amount of makeup water13、排污水量Amount of blowdown14、热流密度Heat load intensity建筑与市政降水工程技术规范Technical code for Groundwater Lowering Engineering in Building and Municipal1、降水工程Engineering dewatering2、降水地质条件dewatering geological condition3、降水工程勘察dewatering geological condition4、降水工程地质参数dewatering geological parameters5、降水深度ground water level after lowering6、滞水detained ground water7、降水出水量yield water during lowering.污水稳定搪设计规范1、稳定塘stabilization ponds（氧化塘）oxidation pond2、厌氧塘anaerobic pond3、兼性塘facultative pond4、好氧塘aerobic pond5、曝气塘aeration pond6、生物塘biological pond7、水生植物塘macrohydrophyte pond8、养鱼塘fish pond9、生态塘ecological pond10、深度处理塘maturationy pond工业用水软化除盐术语1、软化水softened water2、除盐水demineralized water3、高纯水high-purity water , ultra-high purity water4、除硅desilication , silica removal5、脱碱dealkalization6、酸洗acid cleaning7、石灰浆lime slurry8、石灰乳milk of lime9、树脂污染resin fouling10、树脂降解resin degradation11、离子交换剂ion exchanger12、离子交换树脂ion exchange resin13、弱碱性阴离子交换树脂weak-base anion exchange resin14、弱酸性阳离子交换树脂weak-acid cation exchange resin15、强碱性阴离子交换树脂strong-base anion exchange resin16、强酸性阳离子交换树脂strong-acid cation exchange resin17、凝胶型离子交换树脂gel-type ion exchange resin18、大孔型离子交换树脂macro-reticular type ion exchange resin 20、后处理post-treatment22、再生液置换rinse displacement23、二级钠离子交换two stage sodium ion exchange24、顺流再生co-current regeneration25、对流再生counter-current regeneration26、逆流再生up-flow regeneration27、浮动床fluidized bed28、混合离子交换器mixed bed29、空气顶压逆流再生air hold down C.C.R , air blanket C.C.R30、水顶压逆流再生water hold down C.C.R , water blanket C.C.R31、无顶压逆流再生atmospheric press bed C.C.R32、离子交换剂床层膨胀率ion exchange bed expansion33、移动床moving bed34、再生剂耗量chemical measurement35、再生剂量regeneration level36、再生剂计量chemical measurement37、超滤器ultrafiler38、微孔过滤microporous filter39、双层床stratabed , multibed40、双室床double bed41、分布再生stepwise regeneration42、工作交换容量operating capacity43、树脂捕捉器resin trapper44、电渗析器electrodialyzer45、反渗透器reverse osmosis unit46、一级除盐系统primary demineralization system47、单塔单周期移动床monobed and single cycle moving bed48、双塔连续再生移动床dual bed continuous contactor49、单床离子交换器mono-bed ion exchanger工业循环水冷却术语2、湿式冷却塔wet cooling tower3、干式冷却塔dry cooling tower4、干—湿式冷却塔dry-wet cooling tower5、自然通风冷却塔natural draft cooling tower6、机械通风冷却塔mechanical draft cooling tower7、风筒式冷却塔chimney cooling tower8、开放式冷却塔atmospheric cooling tower9、抽风式机械通风冷却塔induced draft mechanical cooling tower10、鼓风式机械通风冷却塔forced draft mechanical cooling tower11、横流式冷却塔crossflow cooling tower12、逆流式冷却塔counterflow cooling tower13、淋水填料packing14、点滴式淋水填料splash packing15、薄膜式淋水填料film packing16、点滴薄膜式淋水填料splash-film packing17、冷却塔配水系统cooling tower distribution system18、槽式配水系统troughing distribution system19、管式配水系统piping distribution system20、管—槽结合式配水系统pipe-troughing distribution system21、池式配水系统hot water distribution system22、旋转布水器rotating distributor23、溅水喷嘴spray nozzle24、冷却塔配水竖井vertical well of water distribution25、淋水面积area of water drenching26、淋水密度water drenching density27、逼近度approach28、冷却水温差cooling range29、除水器drift eliminator30、漂滴drift31、湿空气回流recirculation of wet air33、冷却池cooling pond34、深水型冷却池deep cooling pond35、浅水型冷却塔shallow cooling pond36、挡热墙skimmer wall37、潜水堰submerged weir38、蒸发损失evaporation loss39、风吹损失windage loss40、渗漏损失seepage loss41、温差异重流thermal density flow42、水面综合散热系数heat transfer coefficient室外排水术语1、排水制度sewer system2、合流制combined system3、分流制separate system4、检查井manhole5、跌水井drop manhole6、事故排水口emergency outlet7、暴雨溢流井（截留井）storm overflow well, intercepting well8、潮门tide gate9、生活污水domestic sewage, domestic wastewater10、工业废水industrial wastewater11、生产污水polluted industrial wastewater12、生产废水non-polluted industrial wastewater13、城市污水municipal sewage, municipal wastewater14、旱流污水dry weather flow15、水体自净self-purification of water bodies16、一级处理primary treatment17、二级处理secondary treatment18、生物处理biological treatment19、生活污泥法activated sludge process20、生物膜法biomem brane process21、双层沉淀池（隐化池）imhoff tank22、初次沉淀池primary sedimentation tank23、二池沉淀池secondary sedimetation tank24、生物滤池biological filter , trickling filter25、塔式生物滤池biotower26、生物转盘votating biological clisk27、生物接触氧化bio-contact oxidation28、曝气池aeration tank29、推流曝气plugflow aeration30、完全混合曝气complete-mixing aeration31、普通曝气conventional aeration32、阶段曝气step aeration33、吸附再生曝气biosorption process, contact stabilization34、高负荷曝气high-rate aeration35、延时曝气extended aeration36、氧化沟oxidation ditch37、稳定塘（氧化塘）stabilization pond, oxidation pond38、灌溉田sewage farming39、隔油池oil separator40、固定布水器fixed distributor41、活动布水器movable distributor42、空气扩散曝气diffused air aeration43、浅层曝气inka aeration44、机械表面曝气mechanical surface aeration45、混合液mixed liquor46、堰门weir gate47、原污泥raw sludge48、初沉污泥primary sludge49、二沉污泥secondary sludge50、活性污泥activated sludge51、消化污泥digested sludge52、回流污泥returned sludge53、剩余污泥excess activated sludge54、污泥气sludge gas55、污泥消化sludge digestion56、好氧消化aerobic digestion57、厌氧消化anaerobic digestion58、中温消化mesophilic digestion59、高温消化thermophilic digestion60、污泥浓缩sludge thickening61、污泥淘洗elutriation of sludge62、污泥脱水sludge dewatering63、需氧量oxygen demand64、供氧量oxygen supply65、氧转移率oxygen transfer efficiency66、充氧能力oxygenation capacity67、污泥回流比return sludge ration68、生化需氧量biochemical oxygen demand(BOD)69、化学需氧量chemical oxygen demand(COD)70、耗氧量oxygen consumption(OC或COD Mn)71、悬浮固体suspended solid(SS)通用术语1、给水工程water supply engineering2、排水工程sewerage, wastewater engineering3、给水系统water supply system4、排水系统sewerage system5、给水水源water source6、原水raw water7、地表水surface8、地下水ground water9、苦咸水（碱性水）brackish water, alkaline water10、淡水fresh water11、冷却水cooling water12、废水wastewater13、污水sewage, wastewater14、用水量water consumption15、供水量output16、污水量wastewater flow, sewage flow17、用水定额water consumption norm18、排水定额wastewater flow norm19、水质water quality20、渠道channel, conduit21、干管main22、泵房pumping house23、给水处理water treatment24、泵站pumping station25、污水处理sewage treatment, wastewater treatment26、废水处理wastewater disposal27、格栅bar screen28、曝气aeration29、沉淀sedimentation30、澄清clarification31、过滤filtration32、离子交换法ion exchange33、消毒disinfection34、氯化chlorination35、余氯residual36、游离性余氯free residual chlorine37、结合性余氯combinative residual chlorine38、污泥sludge39、污泥处理sludge treatment40、污泥处置sludge disposal41、水头损失head loss42、贮水池storage reservoir , storage tank43、过河管river crossing44、倒虹管inverted siphon45、稳定stabilization46、异重流density current室外给水术语1、直流水系统once through system2、复用水系统water reuse system3、循环水系统recirculation system4、生活用水domestic water5、生产用水process water6、消防用水fire demand7、浇洒道路用水street flushing demand, road watering8、绿化用水green belt sprinkling, green plot sprinkling9、未预见用水量unforeseen demand10、自用水量water consumption in waterworks11、管网漏失水量leakage12、平均日供水量average daily output13、最高日供水量maximum daily output14、日变化系数daily variation coefficient15、时变化系数hourly variation coefficient16、最小服务水头minimum service head给水工程中取水构筑物的术语及其涵义1、管井deep well, drilled well2、管井滤水管deep well screen3、管井沉淀管grit compartment4、大口井dug well, open well5、井群battery of wells6、渗渠infiltration gallery7、地下水取水构筑物反滤层inverted layer8、泉室spring chamber9、取水构筑物intake strcture10、取水口（取水头部）intake11、进水间intake chamber12、格网screen13、吸水井suction well给水工程中净水构筑物的术语1、净水构筑物purification structure2、投药chemical dosing3、混和mixing4、凝聚coagulation5、絮凝flocculation6、自然沉淀plain sedimentation7、凝聚沉淀coagulation sedimentation8、凝聚剂coagulant9、助凝剂coagulant aid10、药剂周转储备量current reserve11、药剂固定储备量standby reserve12、沉砂池desilting basin, grit chamber13、预沉池pre-sedimentation tank14、平流沉淀池horizontal flow sedimentation tank15、异向流斜管（或斜板）沉淀池tube (plate) settler16、同向流斜板沉淀池lamella17、机械搅拌澄清池accelerator18、水力循环澄清池circulator clarifier19、脉冲澄清池pulsator20、悬浮澄清池sludge blanket clarifier21、液面负荷surface load22、气浮池floatation tak23、气浮溶气罐dissolved air vessel24、气浮接触池contact chamber25、快滤池rapid filter26、虹吸滤池siphon filter27、无阀滤池valveless filter28、压力滤池pressure filter29、移动罩滤池movable hood backwashing filter30、滤料filtering media]31、承托层graded gravel layer32、滤速rate of filtration33、滤池配水系统filter underdrain system34、表面冲洗surface washing35、反冲洗backwash36、气水冲洗air-water washing37、滤池冲洗水量filter wash water consumption38、冲洗强度intensity of back washing39、膨胀率percentage of bed-expansion40、除铁接触氧化法contact-oxidation41、清水池clear-water reservoir42、配水管网distribution system, pipe system43、环状管网pipe network44、枝状管网branch system45、水管支墩buttress, anchorage11。

翻译专业词汇(环境)

城市热岛效应
urban heat island effect
城市污水处理
treatment of domestic sewage
大气检测系统
atmospheric monitoring system
单位国内生产总值能耗
energy consumption per unit of GDP
二氧化硫排放
sulfurdioxide emissions
翻译专业词汇环境哥本哈根气候变化大会copenhageclimateconferenee白色污染whitepollution保护自然资源conserveaturalresources濒危野生动物endangeredwildlife城市垃圾无害化处理dectaminationrefuse城市热岛效应urbanheatislandeffect城市污水处理treatmentdomesticsewage大气检测系统atmosphericmonitoringsystem单位国内生产总值能耗energyconsumptionperunitgdp二氧化硫排放sulfurdioxideemissions碳收集及储存carbstorageccs碳吸收carb防沙林sandbreak防护林shelterbelt工业废水dustrialeffluents废水处理厂wastewatertreatmentplant工业粉尘排放industrialdustdischarge国家环境保护总局stateenvironmentalprotectionadministrationsepa联合国环境与发展大会unitednationsconfereneedevelopmentunced联合国环境规划署unitednationsenvironmentprogramsunep过分开垦overplowing海水淡化seawaterdesalinization环境恶化environmentaidegradations节能减排energyconservationemissionsreduction禁猎区nohuntingareas可降解一次性塑料袋throwawaybiodegradableplasticbags可吸入颗粒物halableparticulate垃圾分类收集collectionclassifiedrefuse垃圾生物降解biodegradationrefuse垃圾填埋refuseiandfill垃圾焚化厂refuseincinerator绿化面积afforestedareas农药残留pesticideresidue汽车尾气motorvehicleexhaust尾气净化器exhaustpurifier小排量汽车smalldisplacementenginevehicles三废综合利用multipurposeusethreewasteswastega

污水处理英汉翻译资料

1) oilfield wastewater采油废水1.By samples experiment of different batches of microbiological preparations to verifying the effect of the removal rate of CODCr and petroleum hydrocarbon degradation of oilfield wastewater treatment, a method using Victory Blue B1 for detecting the quality of the microbiological preparations of oilfield wastewater treatment was proposed.通过不同批次制剂样品对采油废水的CODCr去除率和石油烃降解效果的检测实验,提出了以维多利亚蓝BI来检测油田废水微生物制剂质量的检测方法。

2.The photoelectrocatalytic degradation of oilfield wastewater containing high content of chlorine was studied in TiO_2 aqueous suspensions.以高压汞灯为光源,考察了在光催化、电氧化、光电催化及光电催化/H2O2体系中降解实际油田采油废水的效率。

3.A catalytic advanced oxidation process based on copper charging activated carbon and DO in wastewater has been studied for polishing oilfield wastewater treated by coagulation sedimentation of which COD could not meet the discharge standard.采用载铜活性炭和废水中溶解氧体系,用催化氧化法深度去除采油废水中的COD。

污水处理外文文献

Aerobic treatment of dairy wastewater with sequencing batch reactor systemsXiujin Li,Ruihong ZhangAbstract Performances of single-stage and two-stage se-quencing batch reactor(SBR)systems were investigated for treating dairy wastewater.A single-stage SBR system was tested with10,000mg/l chemical oxygen demand (COD)inﬂuent at three hydraulic retention times(HRTs) of1,2,and3days and20,000mg/l COD inﬂuent at four HRTs of1,2,3,and4days.A1-day HRT was foundsufﬁcient for treating10,000-mg/l COD wastewater,with the removal efﬁciency of80.2%COD,63.4%total solids, 66.2%volatile solids,75%total Kjeldahl nitrogen,and 38.3%total nitrogen from the liquid efﬂuent.Two-day HRT was believed sufﬁcient for treating20,000-mg/l COD dairy wastewater if complete ammonia oxidation is not desired.However,4-day HRT needs to be used for achieving complete ammonia oxidation.A two-stage sys-tem consisting of an SBR and a complete-mix bioﬁlm re-actor was capable of achieving complete ammonia oxidation and comparable carbon,solids,and nitrogen removal while using at least1/3less HRT as compared to the single SBR system.Keywords Aerobic,dairy,wastewater,sequencing batch reactor1IntroductionDairy wastewater is currently disposed of mainly through land application with little or no pretreatment in Califor-nia in the United States.Due to increasing awareness of the general public about potential adverse impact of ani-mal wastes on environmental quality and recent develop-ments in environmental regulations for gaseous-emission control and nutrient management,alternative wastewater treatment methods become attractive options for dairy producers.A sequencing batch reactor(SBR)is a biolog-ical treatment reactor that uses aerobic bacteria to degrade organic carbon and remove nitrogen present in the wastewater.If designed and operated properly,it maybecome a promising alternative for treating animal wastewater to control odors and reduce solids and nutrient contents.The SBR treats wastewater in small batches andﬁts wellwith most animal wastewater collection systems.It is atime-oriented system and operates over repeated cycles ofﬁve phases–ﬁll,react,settle,decant,and idle.The major factors that control the performance of SBRs include or-ganic loading rate,hydraulic retention time(HRT),solids retention time(SRT),dissolved oxygen(DO),and inﬂuent characteristics such as chemical oxygen demand(COD),solids content,and carbon-to-nitrogen ratio(C/N),etc. Depending on how these parameters are controlled,theSBR can be designed to have one or more of these func-tions:carbon oxidation,nitriﬁcation,and denitriﬁcation[1,2].Carbon oxidation and denitriﬁcation are carried outby heterotrophic bacteria and nitriﬁcation is by auto-trophic bacteria.The SBR has been successfully used in the treatment of municipal and industrial wastewater,wherethe high treatment performance resulted in excellent ef-ﬂuent quality[3,4].It is considered to be a suitable systemfor wastewater treatment applications in small communi-ties[5].The SBR is a relatively new technology for agri-cultural applications.Previous research on the SBR foranimal waste was primarily concentrated on swine wastewater treatment.Several researchers[6,7,8]re-ported the performance of SBR in treating swine waste-water with COD and suspended solids(SS)in the range of1,614–2,826mg/l and175–3,824mg/l,respectively.Satis-factory removal of COD and SS from the wastewater was achieved with HRTs of22–30h.Fernades et al.[9]studiedthe SBR for treating highly concentrated swine manurewith about4%total solids(TS).The inﬂuent COD,NH3-N,and total Kjeldahl nitrogen(TKN)were as high as31,175mg/l,1,265mg/l,and2,580mg/l,respectively.Their results indicated that above97%COD,99%NH3-N,and93%TKN removal efﬁciencies were achieved in theliquid efﬂuent at HRTs of6and9days and SRT of over20days.Tam et al.[10]researched SBR for treatment of wastewater from a milking center and reported that the wastewater with919–1,330mg/l COD and15–37mg/lNH3-N could be successfully treated with a HRT of20h. Bioprocess Biosyst Eng25(2002)103–109DOI10.1007/s00449-002-0286-9103Received:2October2001/Accepted:6February2002 Published online:5April2002ÓSpringer-Verlag2002X.Li(&)Department of Environmental Engineering,Beijing University of Chemical Technology,100029,Beijing,ChinaE-mail:lxiujin@Tel.:+86-010-********Fax:+86-010-********R.ZhangBiological and Agricultural Engineering Department, University of California at Davis,CA95616,USAThis research was supported in part by the California Energy Commission and the Agricultural Experiment Station of the University of California,Davis,USA.Studies on the SBR for treating dairy manure are not well documented in the literature.Previous researchﬁndings about the SBR for treatment of swine manure and other types of wastewater provide valuable references for the treatment of dairy wastewater.However,due to the dif-ferences in the characteristics of dairy wastewater from other types of wastewater,research is needed to develop design and operational guidelines for the SBR in treating dairy wastewater of various characteristics.The objectives of this study are to investigate the effects of wastewater characteristics,HRT,SRT,and organic loading rate on the performance of the SBR system in treating dairy wastewater for carbon and solids removal and nitrogen conversion,and develop design and opera-tional guidelines for the SBR system in single-and mul-tiple-stage conﬁgurations.2Materials and methods2.1Dairy manure collection and preparationDairy manure was collected on the Dairy Research Farm of the University of California at Davis.Due to runoff of urine on the feedlot,the collected manure was mainly feces and contained a relatively low content of ammonia nitro-gen.The manure was slurried with addition of water and then screened twice with two sieves with openings of4·4 and2·2mm,respectively,to remove large particles.The screened manure was transported immediately to the laboratory and stored in a freezer at–20°C until use.The TS and COD of the screened manure were30,000–40,000mg/l and35,000–50,000mg/l,respectively.When needed,the stored manure was thawed and then diluted with tap water to obtain a desired COD concentration.Due to relatively low ammonia content of the raw manure as compared to typical levels in the manure collected on dairy farms,urea was added to increase the NH3-N in the prepared manure from100–125mg/l to500–550mg/l.The prepared manure was then put into a50-l feeding tank housed in a refrigerator at4°C for daily use.The feeding tank had an agitator to mix the wastewater during the feeding of the reactors.2.2Experimental setup and operationBoth single-stage and two-stage treatment systems were tested.The single-stage SBR system consisted of an SBR and a solids-settling tank in series.The wastewater wasﬁrst fed into the SBR for treatment and the efﬂuent of the SBR, including both sludge and liquid,was then discharged into a settling tank,where liquid was separated from sludge by gravity settling and characterized as liquid efﬂuent of the system.The two-stage system consisted of an SBR(ﬁrst-stage reactor),a solids-settling tank,and a complete-mix bioﬁlm reactor(CMBR)(second-stage reactor)connected in series.The liquid efﬂuent obtained from the solids-set-tling tank was used as inﬂuent of CMBR and further treated in the CMBR for achieving complete nitriﬁcation.The two-stage SBR-CMBR system is shown in Fig.1.Each system was fed and decanted twice a day for12h in each treatment cycle.All the peristaltic pumps used for feeding and decanting were operated automatically with a digital time controller.The time sequence for different operations during each treatment cycle of the SBR was1–3minﬁll,11h and4–8min react,40min settle,1–3min decant,and10min idle.The CMBR was operated as a complete-mix reactor and had long SRT provided by the attached growth on the polyethylene pellets placed in the reactor.The plastic pellets had light density(920kg/ m3)and were keptﬂuidized with the airﬂow.Each pellet was10mm in diameter and10mm in height,with a cross inside the cylinder and longitudinalﬁns on the outside, providing a large surface area for bacterial attachment. Theﬁlling volume of the pellets in total occupied ap-proximately18%of liquid volume(3l)in the reactor.The SBR and CMBR reactors were made from trans-parent acrylic and had a total volume of6l each,with51cm height and12cm diameter.During testing,the liquid vol-ume of each reactor was3l.Each reactor was aerated using pressurized air at a controlledﬂow rate.In order to mini-mize the water evaporation in the reactor,the air was hu-midiﬁed by traveling through water contained in a15-l jar prior to entering the reactor.The air was evenly distributed into the wastewater through four air stone diffusers in-stalled near the bottom of the reactor.All the reactors were initially seeded with the activated sludge obtained from the UC Davis Wastewater Treatment Plant and allowed to ac-climate for about2months before formal experiments were started.It normally took about4weeks for each SBR re-actor to reach a steady state when a new operating condi-tion was introduced.The steady state was deﬁned to be a state when the weekly variations of efﬂuent COD,TS,NH3-N,and pH were less than5%.These parameters were monitored twice a week.The CMBR had been fully accli-mated with dilute dairy wastewater for about6months and had nitriﬁcation bacteria well established before being connected with the SBR.The mixed liquor suspended solids (MLSS)in the CMBR was about10,000mg/l,which was calculated from both suspended growth and attached growth solids.In order to determine the ammonia emission from SBR due to aeration,ammonia in the exiting air of SBR was collected by absorbing it in0.3N boric acid solution for 24h under each testing condition.2.3Experimental plan and system performance evaluation The experiment was carried out in two phases.Theﬁrst phase was for studying the effects of inﬂuent characteris-tics,HRT,and corresponding SRT and loading rate on the performance of the single-stage SBR system.The second phase was to evaluate the performance of a two-stage SBR-CMBR system.The two systems were then compared in terms of carbon and solids removal and nitrogen conver-sion efﬁciencies.With the single-stage SBR system,three HRTs(1,2and 3days)were tested for wastewater of10,000mg/l COD and four HRTs(1,2,3and4days)for wastewater of20,000mg/l COD.For the wastewater of10,000mg/l COD, the corresponding loading rate and SRT for the three HRTs were10,5,and3.3g COD/l/day and8,12,andBioprocess Biosyst Eng25(2002) 10415days,respectively.For the wastewater of 20,000mg/l COD,the corresponding loading rate and SRT for the four HRTs were 20,10,6.7,and 5g COD/l/day and 1.5,3,4,and 6days,respectively.With the two-stage SBR system,2days was used ﬁrst as the system HRT,with 1day for the ﬁrst-stage and 1day for the second-stage for both in ﬂu-ents,and then 2.5days was used with 2days for the ﬁrst stage and 0.5days for the second stage.An air ﬂow rate of 4l/min was applied for all runs,which was able to main-tain dissolved oxygen (DO)in the SBR and CMBR above 3mg/l.The performance of the treatment systems was evalu-ated in terms of carbon and solids removal and nitrogen conversion ef ﬁciencies.The parameters analyzed included TS,volatile solids (VS),COD,SCOD (soluble COD),TKN,NH 3-N,NO 2-N,and NO 3-N.Two kinds of removal/con-version ef ﬁciencies were used to interpret the results for carbon and solids removal and nitrogen oxidation.One ef ﬁciency,E t ,is based on the removal from total ef ﬂuent (including both sludge and liquid ef ﬂuent generated),re-ﬂecting the removal ef ﬁciency through biological process alone.The other ef ﬁciency,E l ,was based on the removal from liquid ef ﬂuent,i.e.,supernatant,representing the removal ef ﬁciency through both biological process and sludge separation.For the single-stage SBR system,the total ef ﬂuent was the ef ﬂuent from the SBR and the liquid ef ﬂuent was the supernatant decanted from the solids settling tank.For the two-stage SBR-CMBR system,the total ef ﬂuent was the combination of sludge from the settling tank and the ﬁnal ef ﬂuent from CMBR,and the liquid ef ﬂuent was the liquid ef ﬂuent of CMBR.Most of previous research only reports removal ef ﬁciency from liquid ef ﬂuent (E l ).Actually,E l does not re ﬂect the real capability of a system for removing various constituents from wastewater,because part of these constituents are contained in the sludge that is separated from the liquid ef ﬂuent and discharged as a separate sludge stream.Therefore,E t needs to be used in order to assess the real capability of a system for removing various constituents from wastewater.2.4Sampling and analytical methodsAfter each reactor reached steady state under testing conditions,samples were taken from the in ﬂuent,mixed liquor,total ef ﬂuent,and liquid ef ﬂuent of the reactor three times a week (every other day)for analyses of COD,SCOD,TS,VS,NH 3-N,NO 2-N,NO 3-N,and TKN.The re-moval ef ﬁciencies,E l and E t ,were calculated based on the data from in ﬂuent,liquid ef ﬂuent,and total ef ﬂuent of the systems.The separation of sludge and liquid in the total ef ﬂuent of the SBR was performed by settling the ef ﬂuent in a 1-l graduated cylinder for 2h and then decanting the liquid fraction above the sludge-liquid interface line.The COD,SCOD,TS,VS,and TKN were measured according to APHA standard methods [11].The COD measured in this study was COD Cr .The pH was measured with an Accumet pH meter (Fisher Scienti ﬁc,Pittsburgh,Pa.).The NH 3-N was measured with a gas-sensing elec-trode and the pH meter.The DO in the reactors wasmonitored on a daily basis with a DO meter (YSI Mode158,Fisher Scienti ﬁc,Pittsburgh,Pa.).The NO 2-N was analyzed with the HACH method,using a DR/2000spectropho-tometer [12].The NO 3-N was measured with a diffusion –conductivity analyzer [13].3Results and discussion3.1Performance of the single-stage SBR system3.1.1Removal of carbon and solidsThe performance data of the SBR for 10,000mg/l COD in ﬂuent COD of 10,000are shown in Table 1.With the increase of HRT from 1to 3days,the COD,SCOD,TS,and VS in the liquid ef ﬂuent became lower,yielding better ef ﬂuent quality due to increased biological conversion and improved sludge settleability,as indicated by the increased removal ef ﬁciencies (E l and E t ).However,there wasnoboratory setup for a two-stage SBR-CMBR system for dairy wastewater treatmentX.Li,R.Zhang:Aerobic treatment of dairy wastewater with sequencing batch reactor systems105signi ﬁcant difference in terms of carbon and solids rem-ovals and liquid ef ﬂuent quality for the three HRTs.For example,the increase of COD and TS removal ef ﬁciency E l was 5.1%and 0.3%,and E t was 5.7%and 2.0%,respec-tively,when HRT increased from 1to 3days.Therefore,1-day HRT was believed to be suf ﬁcient for treating the dairy wastewater with 10,000mg/l COD for its satisfactory removal ef ﬁciency and relatively short HRT.At 1-day HRT,the removal ef ﬁciency from the liquid ef ﬂuent (E l )was 80.2%for COD,63.4%for TS,and 66.2%for VS.These removals were due to both biological conversion in the SBR and sludge separation in the solids-settling tank.The removal due to biological conversion alone in the SBR,as measured by E t ,was 45.0%for COD,21.4%for TS,and 34.2%for VS.E t was signi ﬁcantly greater than E l ,sug-gesting that the sludge separation after SBR treatment is necessary for achieving signi ﬁcant carbon and solids re-moval from the dairy wastewater.It was found that aerobic treatment greatly enhanced the ﬂocculation and settlea-bility of the solids in the wastewater.Good settleability of sludge was important for achieving high carbon and solids removal ef ﬁciency.The performance data of the SBR for 20,000mg/l COD in ﬂuent are shown in Table 2.The 1-day HRT was tested ﬁrst.It was found that it was impossible to control the SRT at a desired level due to fast solids buildup in the reactor and poor solids settleability.When the HRT was increased to 2days,there was signi ﬁcant improvement in the ef ﬂuent quality and increase of removal ef ﬁciencies.However,when the HRT was further increased to 3days,the changes in the ef ﬂuent quality,COD,and solids removals were not signif-icant.Therefore,2-day HRT was considered enough for COD and solids removal for 20,000mg/l COD in ﬂuent due to its relatively short retention time and high removal ef ﬁ-ciency.At 2-day HRT,the removal ef ﬁciency E l of COD,SCOD,TS,and VS was 85.7%,67.1%,71.0%,and 70.6%,respectively,and E t was 35.9%,67.1%,22.8%,and 25.6%,respectively.The 4-day HRT was tested for achieving com-plete ammonia conversion.Since ammonia was not com-pletely converted at 2-day and 3-day HRT,longer HRT was needed when complete nitri ﬁcation was desired.This will be further discussed in the following nitrogen removal section.The sludge separated from the ef ﬂuent of the SBR contained 4.1–5.9%TS.The lower in ﬂuent COD(10,000mg/l)resulted in better sludge settleability than the higher in ﬂuent COD (20,000mg/l).The sludge volume as the fraction of total ef ﬂuent volume was 5–6%and 13–16%for the lower and higher levels of in ﬂuent COD,respectively.The sludge was composed of not-degraded solids in the wastewater and newly formed bacterial cells.It can be further processed into organic soil amendment through dewatering and composting.Table 1.Ef ﬂuent quality and treatment ef ﬁciencies of SBR for 10,000mg/l COD in ﬂuentParametersIn ﬂuent (mg/l)1-day HRT 2-day HRT3-day HRT Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)COD 10,0001,9806,50080.245.01,5805,13084.248.71,4704,93085.350.7SCOD 2,9141,4571,45750.050.01,4511,45150.250.21,4281,42851.051.0TS 6,6562,4365,23263.421.42,4765,07962.823.72,4165,09863.723.4VS 5,1081,7243,36166.234.21,5323,24970.036.41,4003,16772.638.0TKN 7801953657553.218535476.354.616533878.856.7TN 78048160738.322.248059838.523.447459639.223.6NH 3-N 51012012076.576.510510579.479.4707086.386.3NO 3-N 0375545NO 2-N 024*******pH8.16.86.76.7Table 2.Ef ﬂuent quality and treatment ef ﬁciencies of SBR for 20,000mg/l COD in ﬂuentPara-meters In ﬂuent (mg/l)1-day HRT 2-day HRT 3-day HRT 4-day HRTLiquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)Liquid ef ﬂuent Total ef ﬂuent E l (%)E t (%)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)(mg/l)COD 20,0004,30013,92078.530.42,87012,82085.735.92,66012,32086.738.4167010,90091.743.3SCOD 6,6603,1973,19752.052.02,1902,19067.167.12,0052,00569.969.912151,21581.881.8TS 12,4424,36710,11564.918.73,6129,60571.022.83,4989,58071.923.033509,19573.124.3VS 10,1043,1427,92268.921.62,9727,51770.625.62,8097,33672.227.424607,05375.729.5TKN 1,14054089952.621.118063884.244.017060085.147.48550092.552.3TN 1,14057393349.718.248491857.519.548891857.219.538888863.020.5NH 3-N 54031031042.642.6828284.884.8808085.285.200100100NO 3-N 020*********NO 2-N 01314013010pH8.08.77.97.87.6Bioprocess Biosyst Eng 25(2002)1063.1.2Nitrogen conversionWith the inﬂuent of10,000mg/l COD and1-to3-day HRT,22.2–23.6%of total nitrogen(TN)was lost in the treatment process as indicated by the E t.The losses of TN for the three HRTs were not signiﬁcantly different.The ammonia collection results showed that the amount of NH3-N volatilized accounted for only2–3%of TN,indi-cating that the ammonia loss through volatilization was small under these operating conditions.The rest of TN loss (approximately20%)might be due to the emission of other nitrogenous gases,such as nitrous oxides(NO and NO2)formed in the nitriﬁcation process,and nitrogen gas (N2)formed in the denitriﬁcation process.The TKN removal was53.2–56.7%from the total efﬂuent and75–78.8%from the liquid efﬂuent,respectively.The TKN removal mainly resulted from ammonia oxidation.With the inﬂuent of20,000mg/l COD and1-to4-day HRTs,the loss of TN was18.2–20.5%.For the1-day HRT, the ammonia collection results showed that ammonia volatilization accounted for16%of TN,indicating that most of TN loss was due to ammonia volatilization.This occurred with the low nitriﬁcation rate in the SBR.But ammonia volatilization was insigniﬁcant at2-to4-day HRTs,at which the SBR had high nitriﬁcation activities. These results might imply that ammonia volatilization could be related to nitriﬁcation activity.Little nitriﬁcation occurrence at1-day HRT was due to the short SRT of 1.5days.This agrees with theﬁndings of Prakasam and Loehr[14],who stated that2-day SRT was the minimum for nitriﬁcation of poultry wastes.Therefore,HRT was increased to2days and3days,and corresponding SRT were3days and4days.It was found that nitriﬁcation was able to sustain in the SBR at both HRTs.At2-day and3-day HRT,the TN and TKN removals were19.5%and44.0–47.4%from the total efﬂuent,and57.5–57.2%and84.2–85.1%from the liquid efﬂuent,respectively.Signiﬁcant NH3-N was removed,as indicated by removal efﬁciency of 84.8%for2-day HRT and85.2%for3-day HRT,although there was still80–82mg/l residual NH3-N present in the efﬂuent.It can be seen that there was no signiﬁcant dif-ference between two HRTs in terms of TN,TKN,and NH3-N removal.Therefore,if complete ammonia oxidation is not required,2-day HRT would be considered efﬁcient for treating20,000mg/l COD inﬂuent in terms of both nitrogen removal discussed here and COD and solids removal as mentioned in Sect.3.1.1.Certain amounts of residual ammonia were present in the efﬂuent from20,000mg/l COD inﬂuent at2-day and 3-day HRT.This indicates that the nitriﬁcation process might have been inhibited in both operation conditions. Nitriﬁcation inhibition might be due to possible inhibitions of nitriﬁcation bacteria by free ammonia(FA)and free nitrous acids(FNA)and suppression of nitriﬁcation bac-teria by more competitive heterotrophic bacteria[15].NH3 was undesirable because of its odor and toxicity to aquatic lives;thus,it needed to be removed from the wastewater. Shammas[16]studied the interaction of temperature,pH, and biomass on the nitriﬁcation process and concluded that high nitriﬁcation efﬁciency can only be obtained with either very long detention time or a combination of highsolids concentration and elevated temperature.Therefore,HRT was further increased to4days in order to obtain complete ammonia conversion.It was found that4-dayHRT,corresponding6-day SRT,was enough for complete ammonia conversion,as indicated by zero ammonia pre-sent in the efﬂuent(see Table2).Therefore,it could be concluded that if complete ammonia conversion is desired,4-day HRT would be needed for treating20,000mg/l COD wastewater with540mg/l NH3-N.A track study was conducted in order to further un-derstand the nitriﬁcation process in the SBR.The varia-tions of NH3-N,NO2-N,and NO3-N in the SBR during a12-h operating cycle in treating the wastewater of10,000mg/l COD at2-day HRT are shown in Fig.2.Am-monia oxidation mostly occurred in theﬁrst5h,as indi-cated by the increase of NO2-N and decrease of NH3-N.Since a large amount of ammonia was oxidized in the earlystage of one cycle with high nitriﬁcation,the amount of ammonia volatilization may be decreased in contrast tothe condition when nitriﬁcation is small as mentionedabove.The relationship between ammonia volatilizationand nitriﬁcation activity needs to be further investigated infuture study.The pH could be another factor related to ammonia volatilization.Since higher medium pH in-creased the gas fraction of total ammonia dissolved in the medium,ammonia volatilization could have been highwhen there was little nitriﬁcation and pH maintained rel-atively high(approximately8.0),but small when there wasgood nitriﬁcation and the pH was decreased(Fig.2).TheNO2-N increased to the peak value about5h later after feeding and then started to decrease,while NO3-N startedto increase slightly.Generally speaking,the variations ofNH3-N,NO2-N,NO3-N,and pH in the SBR during the operating cycle depends on the bioconversion dynamics inthe reactor,initial ammonia concentration,and alkalinityin the wastewater.3.2Performance of the two-stage SBR-CMBR systemAs stated above,a4-day HRT is needed for achieving complete oxidation of ammonia in the dairy wastewaterin107the single-stage SBR.It appears that increasing HRT to achieve complete nitri ﬁcation is not cost effective.This led us to explore a two-stage treatment system.Research showed that nitrifying in a separate second-stage aeration system would increase nitri ﬁcation rate,due to the more suitable environment provided by a two-stage system than a single-stage system [17].In aerobic treatment,carbon oxidation is carried out by heterotrophic bacteria,while nitri ﬁcation is carried out by autotrophic bacteria.The two groups of bacteria are signi ﬁcantly different in physiology,substrate requirement,metabolic characteristics,and growth kinetics.In a single-stage system,both carbon oxidation and nitri ﬁcation proceed in one reactor.This forces two groups of bacteria to coexist within the same physical and chemical environment,which is not optimal for either autotrophic or heterotrophic bacteria and makes it dif ﬁcult to achieve optimum carbon and ammonia ually,longer HRT is applied in a single-stage system to balance the slow-growing autotrophic bacteria responsible for nitri ﬁcation and fast-growing he-terotrophic bacteria for carbon oxidation.But this is not economical,as mentioned above.A two-stage system could separate carbon oxidation and the nitri ﬁcation process and make each process proceed in a separate re-actor.The ﬁrst-stage reactor is intended mainly for carbon oxidation and enhancement of solids settleability,and the second-stage reactor for providing suitable conditions fornitri ﬁcation.Since carbon could be oxidized quickly by fast-growing heterotrophic bacteria,the ﬁrst-stage reactorcould use a relatively shorter HRT.After the ﬁrst-stage SBR treatment,the solids settleability is improved as well,the sludge generated is separated and the liquid ef ﬂuent is used as in ﬂuent for the second-stage reactor.Sludge sep-aration would signi ﬁcantly increase the system removal ef ﬁciency and reduce concentrations of constituents such as COD,TS,and NH 3-N in the in ﬂuent,making it possible to use a shorter HRT,while maintaining a longer SRT for nitri ﬁcation in the second-stage reactor.With the opti-mization of environmental conditions and substratecharacteristics for heterotrophic and autotrophic bacteria in separate stages as mentioned above,the overall per-formance of the two-stage system can be improved and overall HRT reduced,as indicated from the performance data presented below.The two-stage system consisted of one SBR as the ﬁrst stage and one CMBR as the second stage.The CMBR was selected to be the second-stage reactor,because the at-tached bacteria growth supported by the polyethylene pellets were believed to be favorable for nitri ﬁcation bac-teria by providing a long SRT.The CMBR was used to treat the liquid ef ﬂuent from the SBR.Both SBR and CMBR were ﬁrst operated at 1-day HRT,with the system HRT being 2days for treating 10,000mg COD/l and 20,000mg COD/l in ﬂuent,respectively.The 1-day HRT in the CMBR was determined to be the appropriate level,based on preliminary test results.The performance data of the two-stage system are shown in Tables 3and 4.It can be seen that the liquid ef ﬂuent quality and removal ef ﬁciencies of carbon,solids,and nitrogen from the two-stage system at 2-day HRT were comparable to those from the single-stage SBR at 3-day HRT for both in ﬂuents.This suggests that,based on the HRT,the two-stage system would require 1/3less reactor volume than the single-stage system and therefore appears to have more favorable economics.In addition,the two-stage system allows complete ammonia oxidation in the wastewater as indicated by zero NH 3-N present in the two-stage system ef ﬂuent at 2-day HRT as compared to 70mg/l NH 3-N in the one-stage ef ﬂuent at 3-day HRT.Because with the in ﬂuent of 20,000mg/l COD ammonia volatilization was high in the ﬁrst-stage SBR at 1-day HRT,Table 3.Performance of two-stage SBR-CMBR system for 10,000mg/l COD in ﬂuent In ﬂuent (mg/l)Stage I:SBR(1-day HRT)Stage II:CMBR (1-day HRT)E l (%)E t (%)Liquid ef ﬂuent Liquid ef ﬂuent (mg/l)(mg/l)COD 10,0001,9801,37486.351.1SCOD 2,9141,4571,01465.265.2TS 6,6562,4362,07668.824.8VS 5,1081,7241,47271.239.1TKN 7801956092.358.0TN 78048143544.224.7NH 3-N 510120 2.599.599.5NO 3-N 037195NO 2-N 0249180pH 8.16.87.9Table 4.Performance of the two-stage SBR-CMBR system for 20,000mg/l COD in ﬂuentIn ﬂuent (mg/l)stage I:SBR (1-day HRT)stage II:CMBR (1-day HRT)E l (%)E t (%)stage I:SBR (2-day HRT)stage II:CMBR (0.5-day HRT)E l (%)E t (%)Liquid ef ﬂuent Liquid ef ﬂuent Liquid ef ﬂuent Liquid ef ﬂuent (mg/l)(mg/l)(mg/l)(mg/l)COD 20,0004,3002,67686.637.028********.543.8SCOD 6,6603,1972,02069.769.7219089086.686.6TS 12,4424,3673,43272.421.83612267078.526.4VS 10,1043,1422,15278.727.029********.532.5TKN 1,14054018084.246.11804096.556.2TN 1,14057350455.823.248443062.321.5NH 3-N 540310 3.099.499.4820100100NO 3-N 020*********NO 2-N 0131341400pH 8.08.77.87.97.4Bioprocess Biosyst Eng 25(2002)108。

污水处理的英文文献翻译(1)

Nutrient removal in an A2O-MBR reactor with sludgereductionABSTRACTIn the present study, an advanced sewage treatment process has been developed by incorporating excess sludge reduction and phosphorous recovery in an A2O-MBR process. The A2O-MBR reactor was operated at a flux of 77 LMH over a period of 270 days. The designed flux was increased stepwise over a period of two weeks. The reactor was operated at two different MLSS range. Thermo chemical digestion of sludge was carried out at a fixed pH (11)and temperature (75℃) for 25% COD solubilisation. The released pbospborous was recovered by precipitation process and the organics was sent back to anoxic tank. The sludge digestion did not have any impact on COD and TP removal efficiency of the reactor. During the 270 days of reactor operation, the MBR maintained relatively constant transmembrane pressure. The results based on the study indicated that the proposed process configuration has potential to reduce the excess sludge production as well as it didn't detonated the treated water quality.Keywords: A2O reactor; MBR; Nutrient removal; TMP1. IntroductionExcess sludge reduction and nutrients removal are the two important problems associated with wastewater treatment plant. MBR process has been known as a process with relatively high decay rate and less sludge production due to much longer sludge age in the reactor (Wenet al., 2004). Sludge production in MBR is reduced by 28-68%, depending on the sludge age used (Xia et al.,2008). However, minimizing the sludge production by increasing sludge age is limited due to the potential adverse effect of high MLSS concentrations on membrane (Yoon et al., 2004). This problem can be solved by introducing sludge disintegration technique in MBR (Young et al., 2007). Sludge disintegration techniques have been reported to enhance the biodegradability of excess sludge (Vlyssides and Karlis, 2004). In overall, the basis for sludge reduction processes is effective combination of the methods for sludge disintegration and biodegradation of treated sludge. Advances in sludge disintegration techniques offer a few promising options including ultrasound (Guo et al., 2008), pulse power (Choi et al.,2006), ozone (Weemaes et al., 2000), thermal (Kim et al., 2003), alkaline (Li et al., 2008) acid (Kim et al., 2003) and thermo chemical(Vlyssides and Karlis, 2004). Among the various disintegration techniques, thermo chemical was reported to be simple and cost effective (Weemaes and Verstraete, 1998). In thermal-chemical hydrolysis, alkali sodium hydroxide was found to be the most effective agent in inducing cell lysis (Rocker et al., 1999). Conventionally, the nutrient removal was carried out in an A2O process. It has advantage of achieving, nutrient removal along with organic compound oxidation in a single sludge configuration using linked reactors in series (Tchobanoglous et al., 2003). The phosphoroes removal happens by subjecting phosphorous accumulating organisms (PAO) bacteria under aerobic and anaerobic conditions (Akin and Ugurlu, 2004). These operating procedures enhance predominance PAO, which are able to uptake phosphorous in excess. During the sludge pretreatment processes the bound phosphorous was solubilised and it increases the phosphorousconcentration in the effluent stream (Nishimura, 2001).So, it is necessary to remove the solubilised phosphorus before it enters into main stream. Besides, there is a growing demand for the sustainable phosphorous resources in the industrialized world. In many developed countries, researches are currently underway to recover the phosphoroes bound in the sludge's of enhanced biological phosphorus removal system (EBPR). The released phosphorous can be recovered in usable products using calcium salts precipitation method. Keeping this fact in mind, in the present study, a new advanced wastewater treatment process is developed by integrating three processes, which are: (a) thermo chemical pretreatment in MBR for excess sludge reduction (b) A2O process for biological nutrient removal (c) P recovery through calcium salt precipitation. The experimental data obtained were then used to evaluate the performance of this integrated system.2. Methods2.1. WastewaterThe synthetic domestic wastewater was used as the experimental influent. It was basically composed of a mixed carbon source, macro nutrients (N and P), an alkalinity control (NaHCO3) and a microelement solution. The composition contained (/L) 210 mg glucose, 200 mg NH4C1, 220 mg NaHCO3, 22一34 mg KH2PO4, microelement solution (0.19 mg MnCl2 4H20, 0.0018 mg ZnCl22H2O,0.022 mg CuCl22H2O, 5.6 mg MgSO47H2O, 0.88 mg FeCl36H2O,1.3 mg CaCl2·2H2O). The synthetic wastewater was prepared three times a week with concentrations of 210±1.5 mg/L chemical oxygen demand (COD), 40±1 mg/L total nitrogen (TN) and 5.5 mg/L total phosphorus (TP).2.2. A2O-MBRThe working volume of the A2O-MBR was 83.4 L. A baffle was placed inside the reactor to divide it into anaerobic (8.4 L) anoxic (25 L) and aerobic basin (50 L). The synthetic wastewater was feed into the reactor at a flow rate of 8.4 L/h (Q) using a feed pump. A liquid level sensor, planted in aerobic basin of A2O-MBR controlled the flow of influent. The HRT of anaerobic, anoxic and aerobic basins were 1, 3 and 6 h, respectively. In order to facilitate nutrient removal, the reactor was provided with two internal recycle (1R). IRl (Q= 1)connects anoxic and anaerobic and IR 2 (Q=3) was between aerobic and anoxic. Anaerobic and anoxic basins were provided with low speed mixer to keep the mixed liquid suspended solids (MLSS) in suspension. In the aerobic zone, diffusers were used to generate air bubbles for oxidation of organics and ammonia. Dissolved oxygen (DO) concentration in the aerobic basin was maintained at 3.5 mg/1 and was monitored continuously through online DO meter. The solid liquid separation happens inaerobic basin with the help of five flat sheet membranes having a pore size of 0.23 pm. The area of each membrane was 0.1 m2. They were connected together by a common tube. A peristaltic pumpwas connected in the common tube to generate suction pressure. In the common tube provision was made to accommodate pressure gauge to measure transmembrane pressure (TMP) during suction. The suction pump was operated in sequence of timing, which consists of 10 min switch on, and 2 min switch off.2.3. Thermo chemical digestion of sludgeMixed liquor from aerobic basin of MBR was withdrawn at the ratio of 1.5% of Q/day and subjected to thermo chemical digestion. Thermo chemical digestion was carried out at a fixed pH of 11(NaOH) and temperature of 75℃for 3 h. After thermo chemical digestion the supernatant and sludge were separated. The thermo-chemicallydigested sludge was amenable to further anaerobic bio-degradation (Vlyssides and Karlis, 2004), so it was sent to theanaerobic basin of the MBR2.4. Phosphorus recoveryLime was used as a precipitant to recover the phosphorous in the supernatant. After the recovery of precipitant the content was sent back to anoxic tank as a carbon source and alkalinity supelement for denitrification.2.5. Chemical analysisCOD, MLSS, TP, TN of the raw and treated wastewater were analyzed following methods detailed in (APHA, 2003). The influent and effluent ammonia concentration was measured using an ion-selective electrode (Thereto Orion, Model: 95一12). Nitrate in the sample was analyzed using cadmium reduction method (APHA, 2003).3. Results and discussionFig. 1 presents data of MLSS and yield observed during the operational period of the reactor. One of the advantages of MBR reactor was it can be operated in high MLSS concentration. The reactor was seeded with EBPR sludge from the Kiheung, sewage treatment plant, Korea. The reactor was startup with the MLSS concentration of 5700 mg/L. It starts to increase steadily with increase in period of reactor operation and reached a value of 8100 mg/L on day 38. From then onwards, MLSS concentration was maintained in the range of 7500 mg/L by withdrawing excess sludge produced and called run I. The observed yields (Yobs) for experiments without sludge digestion (run I) and with sludge digestion were calculated and given in Fig. 1. The Yobs for run I was found to be 0.12 gMLSS/g COD. It was comparatively lower than a value of 0.4 gMLSS/g CODreported for the conventional activated sludge processes (Tchoba-noglous et al., 2003). The difference in observed yield of these two systems is attributed to their working MLSS concentration. At high MLSS concentration the yield observed was found to be low (Visva-nathan et al., 2000). As a result of that MBR generated less sludge.The presently used MLSS ranges (7.5一10.5 g/L) are selected on the basis of the recommendation by Rosenberger et al. (2002). In their study, they reported that the general trend of MLSS increase on fouling in municipal applications seems to result in no impact at medium MLSS concentrations (7一12 g/L).It is evident from the data that the COD removal efficiency of A2O system remains unaffected before and after the introduction of sludge digestion practices. A test analysis showed that the differences between the period without sludge digestion (run I) and with sludge digestion (run II and III) are not statistically significant.However, it has been reported that, in wastewater treatment processes including disintegration-induced sludge degradation, the effluent water quality is slightly detonated due to the release of nondegradable substances such as soluble microbial products (Ya-sui and Shibata, 1994; Salcai et al., 1997; Yoon et al., 2004). During the study period, COD concentration in the aerobic basin of MBR was in the range of 18-38 mg/L and corresponding organic concentration in the effluent was varied from 4 to 12 mg/L. From this data it can be concluded that the membrane separation played an important role in providing the excellent and stable effluent quality.Phosphorus is the primary nutrient responsible for algal bloom and it is necessary to reduce the concentration of phosphorus in treated wastewater to prevent the algal bloom. Fortunately its growth can be inhibited at the levels of TP well below 1 mg/L (Mer-vat and Logan, 1996).Fig. 2 depicts TP removal efficiency of the A2O-MBR system during the period of study. It is clearly evident from the figure that the TP removal efficiency of A/O system was remains unaffected after the introduction of sludge reduction. In the present study, the solubilised phosphorous was recovered in the form of calcium phosphate before it enters into main stream. So, the possibility of phosphorus increase in the effluent due to sludge reduction practices has been eliminated. The influent TP concentration was in the range of 5.5 mg/L. During thefirst four weeks of operation the TP removal efficiency of the system was not efficient as the TP concentration in the effluent exceeds over 2.5 mg/L. The lower TP removal efficiency during the initial period was due to the slow growing nature of PAO organisms and other operational factors such as anaerobic condition and internal recycling. After the initial period, the TP removal efficiency in the effluent starts to increase with increase in period of operation. TP removal in A2O process is mainly through PAO organisms. These organisms are slow growing in nature and susceptible to various physicochemical factors (Carlos et al., 2008). During the study period TP removal efficiency of the system remains unaffected and was in the range of 74-82%.。

污水处理英语词汇

污水处理英语词汇AA/A/O法anaerobic-anoxic-oxic process(厌氧-缺氧-好氧法)A-A-O生物脱氮除磷工艺A-A-O biological nitrogen and phosphorus removal processA-O脱氮工艺 A-O nitrogen removal processA-O除磷工艺 A-O phosphorus removal processAB法 Adsorption Biodegradation process(吸附生物降解法)总a放射线 Total a radioactivity氨氮 ammonia-nitrogen氨基酸 amino acid氨化反应 Nitragen铵盐 ammonium saltA/O法(厌氧-好氧法) anaerobic-oxic process奥贝尔(Orbal)型氧化沟Orbal oxidation ditchB巴登福脱氮除磷工艺Ｂardenpho nitrogen and phosphorus removal process白水(漂洗废水) white water(bleaching water)板框压滤 plate pressure filtration离心机 centrifugalmachine半渗透膜semi-permeable membrane棒状杆菌属corynebacterium薄膜式淋水填料 filmpacking饱和常数(Ks) saturationconstant暴雨公式 storm flowformula暴雨径流 storm runoff溢流井 overflow well苯 benzene苯胺 aniline总B放射性 Total Bradioactivity泵型叶轮暴气器 paddleimpeller aerator泵站 pumping stationBMTS型一体化氧化沟BMTS intrachannel clarifieroxidation ditch闭路循环 closed loop表面冲洗 surfacewashing表面负荷 surface load表面过滤 surfacefiltration表面活性剂 surfactant表面活性物质 surfaceactive additive agent表面曝气 surfaceaeration表面曝气器 surfaceaerator表面淹灌 surface floodirrigation表面冲洗装置 surfacewashing facility丙烯酸 acrylic acid丙烯腈 acrylonitrile病毒 virus病原菌(致病菌) pathogen病原微生物 pathogenmicroorganismBOD-污泥负荷BOD-sludge load补充水 make-up water布朗运动 BrownianmovementC财务评价 financialevaluation配水系统 distributionsystem侧渠型一体化氧化沟integrated oxidation ditchwith side ditch产氢气乙酸菌Rydrogenes and acetic aidgenes产甲烷细菌methanogenes产率系数 yield coefficient常规给水处理工艺conventional water treatment processes敞开式循环冷却水系统opened recirculating cooling water system超高纯水ultra-high-purify water超过滤 ultrafiltration超过滤膜法ultrafiltration membrane process沉淀 precipitation, sedimentation沉淀池 sedimentation tank沉砂池 grit chamber城市废水 municipal wastewater城市废水处理 municipal wastewater treatment澄清 clalification可持续发展 sustainable development充满度 degree of fullness重现期 exceedion interval, period of recurrence抽风式机械通风冷却塔induced draft mechanicalcooling tower臭氧发生器 ozonegenerator臭氧法 ozonationprocess臭氧消毒 ozonedisinfection初次(级)沉淀池 primaryclarifier, primarysedimentation tank除水器 drift eliminator除铁除锰 iron andmanganese removal除盐水(脱盐水) desaltedwater,demineralized water除渣 desilication,silica removal除藻 algal removal除氟 algal fluorine穿透曲线 penetrationcurve活性污泥法 activatedsludge process生物脱氮工艺biological nitrogen removalprocess船型一体化氧化沟 BoatType in intrachannelclarifier oxidation ditch纯(富)氧曝气法pure-oxygen aeration process磁凝聚 magneticcoagulation磁盘法 magnetic diskprocess磁过滤法 magneticfierration process萃取 extraction萃取剂 extractantD达西定律 Darcy’s law大肠菌群Coliform-group bacteria大气泡曝气装置 largebubble aerator代谢 metabolism带式过滤 belt pressfiltration]单级传统消化池single-stage conventionaldigester单螺旋式曝气装置single spiral aerator氮 nitrogen氮循环 nitrogen cycle蛋白质 protein倒虹管 inverted siphon低放射性废物 low-levelradio active waste制浆废水 kraft millwastewater敌百虫 dipterex敌敌畏 dichlorvos涤纶纤维 polyester fiber地表漫流系统 overland flow system(OF)地表水 surface water地面（表）水环境质量标准 environmental quality standard for surface water地下滤场 underground filtration field地下渗漏 underground percolation地下渗滤系统subsurface infiltration system地下水 groundwater人工湿地系统artificial(constructed) wetland再生水回流地下水质标准water quality standard for recharging parified wastewaterwater into groundwater aquifer地下水位 underground water level淀粉生产废水 starch producing wastewater点滴-薄膜式淋水填料splash-film packing点滴式淋水填料 splash packing点污染源 pointpollufion source电动电位electromotance potential电镀废水electroplating wastewater电极 electrode电解法 electrolyticalprocess电流密度 eletronicdensity电渗析 electrodialysis电渗析器electrodialyzer电晕放电 brushdischarge动态年成本 dynamicannual cost动植物油 oil and grease对硫磷 parathion多层床 multibed多环芳烃 polycyclichydracarban多氯联苯polychlorinatedbiphenyls(PCBs)E二次(级)沉淀池secondary clarifier,secondary sedimentation tank二级处理 secondarytratamentF乏燃料spent fuel反冲洗black washing反渗透（逆渗透）reverse osmosis反渗透法reverseosmosis process反渗透膜reverseosmosis membrane反硝化，脱氮denitrification防止腐蚀corrosionprevention纺丝spining纺织废水textilewastewater放射性半衰期radioactive half-life放射性废水处理radioactive wastewatertreatment放射性排出物radioactive effluent非点源污染（面源污染）non-point source pollution非离子氨non-ionicammonia废水处理wastewatertreatment废水中和neutralization ofwastewaters分离separation分流制separate system分流排水系统separated sewer system酚phenol焚烧incineration风吹损失windage loss风筒式冷却塔chimmey cooling tower封闭循环系统closed recirculation system氟化物fluoride辐射流沉淀池radial flow sedimentation tank浮盖式消化池floating-cover digester气浮flotation福斯特利帕除磷工艺Phostrip phosphorus removal process福列德克斯脱氮除磷工艺Phoredox nitrogen and phosphorus removal process腐蚀corrosion富营养化eutrophication富营养化湖泊、水库eutrophic lake,eutrophic reservoirGr射线 gamma rays甘蔗废水 sugarcanewastewater干化 drying干化床 drying bed冷却塔 cooling tower钢铁工业废水 iron andsteel mill wastewater高纯水 ultrapure water高放废物 high-levelradio active wastes高分子电解质polymolecular electrolye高分子絮凝剂polymolecular floc高负荷活性污泥法high-loading activatedsludge method高负荷生物滤池 highloading biological filter高炉煤气洗涤水wastewater produced fromscrubbing blast furnace topgas高锰酸盐指数 potassiumpermanganate index高速消化池 high-ratedigester高梯度磁分离器(HGMS)high grade magnegic separator高浊度水 high turbiditywater格栅 bar screen隔板反应池 bafflereaction tank隔板式混合槽 bafflemixer隔油池 oil separator镉 cadmium铬 chromium给水泵站 water pumpingstation给水处理 watertreatment给水网管系统 watersupply system工业水处理与循环系统industrial water treatmentand recirculation system工业废水 industrialwastewater汞 mercury鼓风曝气 blast aeration鼓风式机械通风冷却塔forced draft mechanicalcooling tower固定螺旋式曝气装置fixed spiral aerator景观、娱乐水体landscape and recreationwaterbody管道接口 conduit joint给水配水系统 watersupply piping distributionsystem网管平差 balancing netwok罐头生产废水 Cannery wastewater硅藻土 cilicious marH海水淡化demineralization of sea water含酚废水 phenol contained wastewater含水量 moisture content含盐量 saline capacity含油废水 oily wastewater旱流污水量(DWF)dry-weather flow好氧生物处理 aerobic biological treatment好氧塘 aerobic pond好氧稳定 aerobic stabilization合成洗涤剂 synthetic detergent合成纤维 syntheticfiber合成纤维废水 synthetic fiber wastewater合成橡胶 synthetic rubber合流城市废水 combined municipal wastewater合流制排水系统combined sewer system水体功能分类 waterbodyfunction classification核能工厂 nuclear powerstation核燃料循环 nuclear fuelcycle核素 nuclide冶金工业废水metallurgical industrywastewater黑液 black liquor黑液除硅sillica-elimination fromblack liquid虹吸滤池 siphon filter化学处理 chemicaltreatment化学工业 chemicalindustry化学吸附 chemicaladsorption化学纤维 chemical fiber化学需氧量 chemicaloxygen demand (COD)环状管网系统 grid pipenetwork system缓蚀 corrosioninhibition缓蚀剂 corrosioninhibitor磺化煤 sulfonated coal挥发酚 volatile phenol回流比 recycle ratio回流污泥率 returnsludge ratio汇水面积 catchment area,collection area混合 mixing混合床 miced bed混合液挥发性悬浮固体mixed liquor volatilesuspended solids(MLVSS)混合液悬浮固体 mixedliquor suspendedsolids(MLSS)混凝 coagulation混凝沉淀coagulation-sedimentation混凝剂 coagulant浑浊度 tubidity活化产物 activationproducts硅酸钠 sodium silicate活性剂 activator活性染料 active dye活性炭 activated carbon活性炭的再生re-generation of activatedcarbon活性炭吸附 activecarbon adsorption活性污泥 activated sludge活性污泥法 activated sludge process活性污泥负荷 activated sludge loading活性污泥驯化acclimation of activated sludgeJ机械反应池 mechanical reactor机械剪切曝气装置mechanical shearing aerator机械搅拌 mechanical mixing机械搅拌澄清池accelerator机械曝气 mechanical aeration机械通风冷却塔mechanical draft cooling tower机械脱水 mechanical dewatering极化现象 polarization级配 granular composition集水池 collection well集中处理(合并处理)joint treatment计算机 computer计算机辅助设计computer aid design加速过滤器accelo-filter加压气化pressure-gasification甲基对硫磷 parathionmethyl甲醛 formaldehyde甲烷 methane甲烷发酵 methanefermentation甲烷气体 methane gas间歇式活性污泥系统sequencing batch reactoractivated sludge system(SBR)蒹性塘 facultative pond检查井 manhole减压薄膜蒸发法decreasing pressure andthin-film evaporationprocess碱法制浆 soda pulpingprocess浆粕 pulp降雨历时 duration ofrainfall降雨量,降水precipitation浇洒道路用水 streetflushing water焦化废水 cokingwastewater交替工作式氧化沟alternative operatingoxidation ditch交替运行的生物滤池alternative operatingtrickling filter胶体 colloid阶段曝气 step aeration接触池 contact chamber接触氧化法 contactoxidation process结垢 scale节水 water saving锦纶纤维 polyamidefiber腈纶纤维 acrylic fiber精制塘(深度处理塘)polishing pond经济效益 economicbenefit径流系数 runoffcoefficent静态年成本 staticannuity cost景观娱乐用水水质标准water quality standard forlandscape and recreation area酒精工业 alcoholdistilery就地处理系统(小型处理)on-site treatment systems(small scale facilities)聚丙烯酰胺polyacrylamide聚丙烯酰胺水解体polyacrylamide hydrolysis product聚合 polymerize聚合度 polymerizing degree聚合氯化铝polyaluminum chloride均衡池(塘) equalizalion tank(basin,lagoon)K卡罗塞式氧化沟Corrousel oxidation ditchK型叶轮曝气机 K type impeller aerator凯式氮 kjeldahl nitrogen空气驱动式生物转盘aero biological disks孔隙率 porosity快滤池 rapid filter快速渗滤系统 rapid infiltration system(RI)矿井 shaft(mine)矿区 mining area矿区环境 mining area environment矿山废水 minery wasterwater矿山酸性废水 acid minewastewater扩散板 diffusion plate扩散管 diffusion tube扩散盘(罩) diffusiondisc(cover)L乐果 dimethoate冷凝 condensation冷凝水 condensate water冷却 cooling冷却池 cooling pond冷却塔 cooling tower冷却塔配水系统 coolingtower distribution system冷却循环水 circulatedcooling water冷轧 cold steel-rolling离心泵 centrifugal pump离心 centrifugationforce离心机 centrifugalmachine离心脱水 centrifugaldewatering离心作用centrifugation离子交换 ion exchange离子交换剂 ionexchanger离子交换膜 ion exchangemembrane离子交换树脂 ionexchange resin粒径 grain size砾石承托层 gravelsupport炼钢厂废水steel-making processwastewater炼铁 iron-smelting炼铁(高炉)废水 blastfurnace wastewater炼油厂废水 refineryprocessing waserwater淋滤 leaching淋水密度 waterdrenching density淋水面积 waterdrenching aera淋水填料 packing磷 phosphorus磷酸盐 phosphate生物流化床 Biologicalfluidized bed硫化物 sulphide硫化物沉淀法precipitation with sulphide硫酸铵 ammonium sulfate硫酸钙 Calcium sulfate硫酸铝 aluminum sulfate硫酸镁 magnesiumsulfate硫酸铁 ferric sulfate硫酸亚铁 ferroussulfate硫酸盐 sulfate硫循环 sulphur cycle铝酸钠 sodium aluminate滤层 filter layer滤池冲洗水量 filter washing water consumption滤池配水系统 filter underdrain system滤池运行周期 filter cycle time滤床 filter bed滤料 filtering medium滤速 filtration rate滤液 filtrate氯 chlorine氯-氨法chlorine-ammonia process氯化,加氯处理chlorination氯化物 Chlorides螺旋桨式快速搅拌机propeller-type high speed agitatorM马拉硫磷 malathion脉冲澄清池 pulsator慢滤池 slowfilter慢速渗滤系统 slow rateinfiltration system (SR)煤气 coal gas煤气厂 gas work煤气发生器 coal gasgenerator煤气发生站 gasgeneration station煤气净化 coal gaspurification煤炭 coal锰 manganse米门公式 Michaelis -Menten equation莫诺德公式 Monodequation密闭式循环冷却水系统closed recirculating coolingwater system密集多喷嘴曝气装置compact multinozzle aerator面污染源 non-pointpollution source敏感性分析 sensitivityanalysis膜分离装置 membraneseperator膜选择性 membraneselectivity膜污染 membranefoulting膜中毒 membranepoisoningN难生物降解有机物nonbiodegradable organies尼龙 nylon逆流漂洗counter-current washing逆流式冷却塔counterflow cooling tower逆流再生counter-current regeneration粘胶 rayon酿酒废水 winerywastewater酿造与发酵工业废水brewery and fermentationindustrial wastewater凝聚 coagulation凝聚剂 coagulant牛奶生产废水 dairywastewater浓缩 concentration浓缩倍数 cycle ofconcentration浓缩池 thickening tank浓缩污泥 concentratedsludge农田灌溉水质标准standards for irrigation water quality农用污泥中污染物控制标准 contaminants control standard for sludge farming农药 pesticide农药厂废水 pesticide plant wastewaterP排泥系统 sludge - discharge system排水量 discharge排水管 drain pipe排水口 outlet排水系统 sewer system排污 blowdown泡沫分离 foam phase separation配水网管 distribution system ,pipe system喷灌 spray irrigation喷水池 spray pond皮革 leather啤酒废水 brewery wastewater啤酒废水处理 brewery wastewater treatment漂白 bleaching平板式膜 plate membrane平板式叶轮曝气器 plateimpellar aerator平衡吸附容量equilibrium adsorptioncapacity平流式沉砂池horizontal flow grlt removaltank平流式沉淀池horizontal flowsedimentation tank普通生物滤池biological filter,tricklingfilter曝气 aeration曝气沉砂池 aerationgrit chamber曝气池 aeration tank曝气栅 aeration boom曝气设备 aerationequipment曝气时间 aeration time曝气装置,曝气机aerator居民生活垃圾 HouseholdWaste庫底平整線 bottomflatting line of the site庫區填埋邊線 landfillside line of the site庫容 Storage capacity垃圾 Waste ，Solid Waste垃圾壩 waste dam垃圾殘渣 residue垃圾槽 waste chute垃圾層 waste layer垃圾產量 Waste output垃圾堆肥場 wastecomposting field垃圾堆體 waste pile垃圾副壩 secondarywaste dam垃圾揀選場 WasteSorting Site垃圾氣化 wastegasification垃圾收集車 wastecollector垃圾桶 garbage ，rubbish barrel垃圾箱 garbagecontainer垃圾壓實系統 wastecompactor system垃圾衍生燃料Refuse-derived fuel (RDF)垃圾衍生燃料 wastederived fuel垃圾轉運車 wastetransfer truck垃圾轉運站 wastetransfer station垃圾裝卸坡 wasteloading ramp離心脫水機 centrifugal dewaterer鈉基膨潤土 sodium bentonite農業廢棄物Agricultural Waste濃縮池 thickening tank排放 discharge排泥閥 sludge valve排水口 Drain Outlet膨潤土 bentonite熱解 Pyrolysis溶解氧測定儀（DO計）dissolved oxygen meter（DO meter）砂水分離機 grit-water splitter商業垃圾 Commercial Waste上橫沖填埋場Shanghengchong Landfill Site上清液 supernatant liquor設備選型 Type selection of equipment滲濾液（垃圾滲濾液）leachate滲濾液處理 leachate treatment滲濾液處理站 Leachate Treatment Station滲濾液收集及導排氣系統平面圖 Plan of LeachateCollection and Guiding andExhaust System滲濾液收集盲溝 blinddrain for leachatecollection生活垃圾 Domestic waste生活垃圾焚燒污染控制標准 Standard for PollutionControl on the MunicipalSolid Waste Incineration剩余污泥 excess sludge剩余污泥泵 excesssludge pump輸渣機 clinker conveyer豎向石籠 vertical stonecage雙層防滲結構double-liner system水位 water level提升泵站 lift pumpingstation填埋（垃圾） Landfill填埋場 Landfill site填埋場封場 seal oflandfill site填埋場總體布置圖General Layout of LandfillSite填埋場縱斷面示意圖Sketch Map of Landfill SiteVertical Section填埋庫區 Landfill Area填埋庫區平面布置圖Plane Layout of Landfill Area1:1000填埋氣 Landfill gas砼 concrete圖例 legend土工合成材料粘土墊層Geosynthetics Clay Liner(GCL)土工膜 geomembrane脫水機 dewaterer脫水機房 dewateringhouse衛生填埋 sanitarylandfill渦流沉砂池（旋流沉砂池）vortex grit tank污泥泵房 sludge pumpingroom污泥處理 sludgetreatment污泥處理流程示意圖Flow Chart of SewageTreatment Process污泥管線 sludgepipeline污泥濃度計（MLSS計）sludge concentration meter（MLSS meter）污泥濃縮及脫水機房Sludge Thickening &Dewatering House污泥脫水車間 sludgedewatering workshop污水泵 sewage pump污水處理 sewage treatment污水處理厂 Wastewater Treatment Plant污水處理流程示意圖Sewage Treatment Process Sketch Map污水管線 sewage pipeline污水水面 wastewater surface無線傳輸 wireless transmission吸水井 suction well消毒池 disinfecting tank新聯村熊家窯Xiongjiayao, Xinliancun序批式活性污泥法（SBR 法） Sequence Batch Reactor選型 Type selection壓縮式垃圾車 waste compactors厭氧、缺氧、好氧Anaerobic, Anoxic, Aerobic Underwater Blender厭氧堆肥 anaerobic composting厭氧發酵 methane fermentation; anaerobic fermentation厭氧流化床反應器anaerobic fluidized bed厭氧流化床反應器anaerobic fluidized bed氧化溝 oxidation ditch氧化溝 oxidation ditch葉輪曝氣機 impeller aerator一級發酵（初級發酵）primary fermentation醫院垃圾 Hospital Waste營養土層 nutritioussoil layer預留垃圾綜合利用生產用地 Reserved Waste Comprehensive Utility and Production Land再生 reclamation柵渣 sediment粘土層 clay layer支盲溝 blind sub-drain至垃圾填埋場 to the waste landfill site終期覆土 terminal earth covering主盲溝 main blind drain自控系統 autonomous system自然土層 natural soil layer。

《污水处理技术》术语英语词汇大全

污水处理技术术语专有名词病毒细菌Campylobacteria Jejuni 弯曲菌Coliform-group bacteria 大肠菌群Corynebacterium 棒状杆菌属Cryptosporidium 隐孢子虫Escherichia Coli 大肠杆菌Dipterex 敌百虫Giardia 贾第鞭毛虫Legionella 军团菌Methanogenes 产甲烷细菌Norovirus 诺罗病毒Pathogen 病原菌(致病菌)Rydrogenes and acetic aid genes 产氢气乙酸菌自建字库A/A/O法anaerobic-anoxic-oxic process (厌氧-缺氧-好氧法)A-A-O生物脱氮除磷工艺A-A-O biological nitrogen and phosphorus removal process Activated sludge process 活性污泥法Adsorption 吸附Aeration 曝气Aerobinen bakteeri 需氧微生物A-O脱氮工艺A-O nitrogen removal processA-O除磷工艺A-O phosphorus removal processAB法Adsorption Biodegradation process (吸附生物降解法)ammonia-nitrogen 氨氮ammonium salt 铵盐amino acid 氨基酸Anaerobinen bakteeri 厌氧微生物A/O法(厌氧-好氧法)anaerobic-oxic processBackwater 回用水Biofilm 生物膜法Biological aerated 生物曝气BOD (Biochemical oxygen demand) 生物需氧量Campylobacteria Jejuni 弯曲菌Carrousel Oxidation ditch 卡鲁塞尔氧化沟（荷兰DHV1967研制）CAST回圈式活性污泥法(Cyclic Activated Sludge Technology，简称CAST) Cesspool 污水池COD（chemical oxygen demand）化学需氧量Colloid 胶体Corrosion腐蚀Cryptosporidium 隐孢子虫Giardia 贾第鞭毛虫Escherichia Coli 大肠杆菌Eutrophication 富营养化Flocculation 絮凝Flotation 悬浮法= flotaatioHBR （high compound biological reactor）高效复合生物反应器Hydrogen sulfide 硫化氢= rikkivetykaasuICEAS间歇循环延时曝气系统(Intermittent Cycle Extended Aeration System)Ion Exchange 离子交换Legionella 军团菌Microbiology 微生物Nitragen氨化反应Norovirus 诺罗病毒Nutrients 营养物Orbal oxidation ditch奥贝尔(Orbal)型氧化沟ozone generator臭氧发生器ozonation process臭氧法ozone disinfection臭氧消毒Pathogen病原菌(致病菌)pathogen microorganism病原微生物primary treatment, 一级处理SBR序列间歇式活性污泥法（Sequencing Batch Reactor Activated Sludge Process）secondary treatment 二级处理Sedimentation tank 沉淀池Sewage 污水Sewage treatment 污水处理sewage treatment rate 污水处理率Suspended solids 悬浮物Tertiary treatment 三级处理Total a radioactivity总a放射线Unitank好氧生物污水处理法Wastewater 污水B巴登福脱氮除磷工艺Ｂardenpho nitrogen and phosphorus removal process白水(漂洗废水)white water(bleaching water)板框压滤plate pressure filtration离心机centrifugal machine半渗透膜semi-permeable membrane棒状杆菌属corynebacterium薄膜式淋水填料film packing饱和常数(Ks)saturation constant暴雨公式storm flow formula暴雨径流storm runoff溢流井overflow well苯benzene苯胺aniline总B放射性Total B radioactivity泵型叶轮暴气器paddle impeller aerator泵站pumping stationBMTS型一体化氧化沟BMTS intrachannel clarifier oxidation ditch 闭路循环closed loop表面冲洗surface washing表面负荷surface load表面过滤surface filtration表面活性剂surfactant表面活性物质surface active additive agent表面曝气surface aeration表面曝气器surface aerator表面淹灌surface flood irrigation表面冲洗装置surface washing facility丙烯酸acrylic acid丙烯腈acrylonitrile病毒virus病原菌(致病菌) pathogen病原微生物pathogen microorganismBOD-污泥负荷BOD-sludge load补充水make-up water布朗运动Brownian movementBOD (Biochemical oxygen demand) 生物需氧量Campylobacteria Jejuni 弯曲菌Carrousel Oxidation ditch 卡鲁塞尔氧化沟（荷兰DHV1967研制）Cast活性污泥法之一Cintinuous Loop Reator,简称CLR连续环式反应池COD（chemicaloxygendemand）化学需氧量C财务评价financial evaluation配水系统distribution system侧渠型一体化氧化沟integrated oxidation ditch with side ditch产氢气乙酸菌Rydrogenes and acetic aid genes产甲烷细菌methanogenes产率系数yield coefficient常规给水处理工艺conventional water treatment processes敞开式循环冷却水系统opened recirculating cooling water system 超高纯水ultra-high-purify water超过滤ultrafiltration超过滤膜法ultrafiltration membrane process沉淀precipitation, sedimentation沉淀池sedimentation tank沉砂池grit chamber城市废水municipal wastewater城市废水处理municipal wastewater treatment澄清clalification可持续发展sustainable development充满度degree of fullness重现期exceedion interval, period of recurrence抽风式机械通风冷却塔induced draft mechanical cooling tower臭氧发生器ozone generator臭氧法ozonation process臭氧消毒ozone disinfection初次(级)沉淀池primary clarifier, primary sedimentation tank除水器drift eliminator除铁除锰iron and manganese removal除盐水(脱盐水)desalted water,demineralized water除渣desilication, silica removal除藻algal removal除氟algal fluorine穿透曲线penetration curve活性污泥法activated sludge process生物脱氮工艺biological nitrogen removal process船型一体化氧化沟Boat Type in intrachannel clarifier oxidation ditch 纯(富)氧曝气法pure-oxygen aeration process磁凝聚magnetic coagulation磁盘法magnetic disk process磁过滤法magnetic fierration process萃取extraction萃取剂extractantD达西定律Darcy’s law大肠菌群Coliform-group bacteria大气泡曝气装置large bubble aerator代谢metabolism带式过滤belt press filtration]单级传统消化池single-stage conventional digester单螺旋式曝气装置single spiral aerator氮nitrogen氮循环nitrogen cycle蛋白质protein倒虹管inverted siphon低放射性废物low-level radio active waste制浆废水kraft mill wastewater敌百虫dipterex敌敌畏dichlorvos涤纶纤维polyester fiber地表漫流系统overland flow system(OF)地表水surface water地面（表）水环境质量标准environmental quality standard for surface water 地下滤场underground filtration field地下渗漏underground percolation地下渗滤系统subsurface infiltration system地下水groundwater人工湿地系统artificial(constructed) wetland再生水回流地下水质标准water quality standard for recharging parified wastewater water into groundwater aquifer地下水位underground water level淀粉生产废水starch producing wastewater点滴-薄膜式淋水填料splash-film packing点滴式淋水填料splash packing点污染源point pollufion source电动电位electromotance potential电镀废水electroplating wastewater电极electrode电解法electrolytical process电流密度eletronic density电渗析electrodialysis电渗析器electrodialyzer电晕放电brush discharge动态年成本dynamic annual cost动植物油oil and grease对硫磷parathion多层床multibed多环芳烃polycyclic hydracarban多氯联苯polychlorinated biphenyls(PCBs)Dat－Ita 活性污泥法之一Decant 排水E二次(级)沉淀池secondary clarifier, secondary sedimentation tank二级处理secondary tratamentEceas 活性污泥法之一Escherichia Coli 大肠杆菌F乏燃料spent fuel反冲洗black washing反渗透（逆渗透）reverse osmosis反渗透法reverse osmosis process反渗透膜reverse osmosis membrane反硝化，脱氮denitrification防止腐蚀corrosion prevention纺丝spining纺织废水textile wastewater放射性半衰期radioactive half-life放射性废水处理radioactive wastewater treatment放射性排出物radioactive effluent非点源污染（面源污染）non-point source pollution非离子氨non-ionic ammonia废水处理wastewater treatment废水中和neutralization of wastewaters分离separation分流制separate system分流排水系统separated sewer system酚phenol焚烧incineration风吹损失windage loss风筒式冷却塔chimmey cooling tower封闭循环系统closed recirculation system氟化物fluoride辐射流沉淀池radial flow sedimentation tank浮盖式消化池floating-cover digester气浮flotation福斯特利帕除磷工艺Phostrip phosphorus removal process福列德克斯脱氮除磷工艺Phoredox nitrogen and phosphorus removal process 腐蚀corrosion富营养化eutrophication富营养化湖泊、水库eutrophic lake,eutrophic reservoirFlocculant 絮凝Gr射线 gamma rays甘蔗废水 sugarcane wastewater干化 drying干化床 drying bed冷却塔 cooling tower钢铁工业废水 iron and steel mill wastewater高纯水 ultrapure water高放废物 high-level radio active wastes高分子电解质 polymolecular electrolye高分子絮凝剂 polymolecular floc高负荷活性污泥法 high-loading activated sludge method高负荷生物滤池 high loading biological filter高炉煤气洗涤水 wastewater produced from scrubbing blast furnace top gas 高锰酸盐指数 potassium permanganate index高速消化池 high-rate digester高梯度磁分离器(HGMS) high grade magnegic separator高浊度水 high turbidity water格栅 bar screen隔板反应池 baffle reaction tank隔板式混合槽 baffle mixer隔油池 oil separator镉cadmium铬chromium给水泵站 water pumping station给水处理 water treatment给水网管系统 water supply system工业水处理与循环系统industrial water treatment and recirculation system 工业废水 industrial wastewater汞 mercury鼓风曝气 blast aeration鼓风式机械通风冷却塔 forced draft mechanical cooling tower固定螺旋式曝气装置 fixed spiral aerator景观、娱乐水体landscape and recreation waterbody管道接口 conduit joint给水配水系统 water supply piping distribution system 网管平差 balancing netwok罐头生产废水 Cannery wastewater硅藻土 cilicious marH海水淡化 demineralization of sea water含酚废水 phenol contained wastewater含水量moisture content含盐量saline capacity含油废水 oily wastewater旱流污水量(DWF) dry-weather flow好氧生物处理 aerobic biological treatment好氧塘aerobic pond好氧稳定 aerobic stabilization合成洗涤剂 synthetic detergent合成纤维 synthetic fiber合成纤维废水 synthetic fiber wastewater合成橡胶 synthetic rubber合流城市废水 combined municipal wastewater合流制排水系统 combined sewer system水体功能分类 waterbody function classification核能工厂 nuclear power station核燃料循环 nuclear fuel cycle核素nuclide冶金工业废水 metallurgical industry wastewater黑液 black liquor黑液除硅 sillica-elimination from black liquid虹吸滤池 siphon filter化学处理 chemical treatment化学工业 chemical industry化学吸附 chemical adsorption化学纤维 chemical fiber化学需氧量 chemical oxygen demand (COD)环状管网系统 grid pipe network system缓蚀 corrosion inhibition缓蚀剂corrosion inhibitor磺化煤sulfonated coal挥发酚volatile phenol回流比recycle ratio回流污泥率 return sludge ratio汇水面积 catchment area, collection area混合 mixing混合床 miced bed混合液挥发性悬浮固体 mixed liquor volatile suspended solids(MLVSS)混合液悬浮固体 mixed liquor suspended solids(MLSS)混凝 coagulation混凝沉淀 coagulation-sedimentation混凝剂 coagulant浑浊度 tubidity活化产物 activation products硅酸钠 sodium silicate活性剂 activator活性染料 active dye活性炭 activated carbon活性炭的再生 re-generation of activated carbon活性炭吸附 active carbon adsorption活性污泥activated sludge活性污泥法 activated sludge process活性污泥负荷 activated sludge loading活性污泥驯化 acclimation of activated sludgeIdle 闲置Legionella 军团杆菌Oxidation ditch 氧化沟, 又名连续循环曝气池（Continuous loop reactor）Ritilä 格栅？SBR(Sequencing Batch Reactor Activated Sludge Process) 序列间歇式活性污泥法Settle 沉淀Unitank活性污泥法之一污水处理技术知识目前，国内外城市污水处理厂处理工艺大都采用一级处理和二级处理。

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河流污水处理的相关论述1 前言随着工业化和城市化的发展，水环境污染、水资源紧缺日益严重，水污染控制、水环境保护已刻不容缓。

我国现在新建城市或城区采用雨污分流制，但老城市或老城区大多仍然是雨污合流的排水体制。

许多合流污水是直接排放到水体。

而将旧合流制改为分流制，受现状条件限制大许多。

老城区建成年代较长，地下管线基本成型，地面建筑拥挤，路面狭窄，旧合流制改分流制难度较大。

合流污水的一大特点是旱季和雨季的水质、水量变化大，雨季污水ＢＯＤ浓度低，不利于生化处理。

国家提出2010 的我国城市污水处理率要求达到4０%，因此研究有效的合流污水处理方法对加快城市污水处理步伐具有重要的意义。

本文针对合流污水处理的有关情况，谈一些个人看法。

2污水处理工艺要求我国目前不少城市，新城区与老城区并存, 合流制与分流制并存。

因此，新建或扩建的污水处理厂,在满足城市总体规划和排水规划需要的同时, 还应能达到如下要求:1. 具备接纳旧城区合流污水的能力，具有较强的适应冲击负荷的能力。

污水处理厂污水来源包括两部分，一是新城区分流污水，二是老城区合流污水。

与合流污水相比,分流污水水质、水量变化幅度小得多，对污水处理厂调节缓冲的要求小得多。

对于合流污水，降雨前期因雨水冲刷街区,合流污水较脏, 但水量相对较小, 降雨后期水量较大，但污水中有机物浓度相对较小。

因此, 降雨前期合流污水,可考虑与分流污水一起经预处理后进入污水处理构筑物。

降雨后期合流污水，除一部分与分流污水一起经污水预处理构筑物进入污水处理构筑物外, 另一部分可考虑通过雨污溢流构筑物进入雨污溢流沉定池后排入附近水体。

为了对进入污水处理构筑物的合流污水高峰流量、水质波动进行缓冲调节，污水处理构筑物前端可设缓冲调节池以均衡水质、储存水量。

2. 具有可靠的BOD、COD、ＳS 去除功能及氮磷去除功能, 保证最终出水水质稳定。

通常情况下, 城市污水中难降解有机物较少，BOD、ＣOD 去除比较容易实现,而氮磷去除则较复杂。

我国现行的污水排放标准对污水处理厂出水氮磷指标有严格的要求，故城市污水处理都必须达到氮磷的有效去除。

在现行城市污水脱氮除磷工艺中，Ａ２／０采用较为广泛。

针对Ａ2/0工艺存在的问题目前出现了许多改进工艺，每种工艺又都存在各自的特点和局限。

由于合流污水引起的水质、水量波动较大，对污水厂各处理单元产生冲击，为了适应受纳水体的要求, 为使BOD、CＯD 等指标进一步降低,进一步去除污水中的细菌及氮、磷等植物性营养物质，在污水厂与受纳水体之间可设氧化塘。

３.具有灵活多变的运行方式，可根据收集的污水量、进水水质以及季节变化调整运行方式。

常规A2/０工艺,很难做到灵活方便地调整运行方式。

但A2／0工艺从构成原理上讲, 是在曝气段前加厌氧段和缺氧段。

这一原理用于氧化沟技术, 便可形成各种适应不同水质、水量、季节变化的运行方式。

污水厂可根据实际情况设两个以上的氧化沟，每个沟设一定数量的水力推进器，池底均匀分布微孔爆气器。

通过调整氧化沟污水进水管阀门、曝气器的开及关的区域、内回流比大小、污泥回流比大小及水力推进器运行个数，便可形成串联、并联等若干种运行方式。

每种运行方式具有各自区域大小不同的厌氧段、缺氮段、曝气段。

当旱季污水量小则采用串联运行方式，雨季污水量大，则采用并联运行方式。

夏季温度高,硝化反应速度快, 则采用具有较小曝气区域、较小硝化段的运行方式，相应反硝化区域增加、功能加强, 冬季情况则正好相反。

如进水碳源浓度较低,则采取串联的、使后续反硝化段的碳源能得到补充的运行方式。

３工艺流程选择和特点说明根据污水合流制与分流制并存的特点及处理后污水排放水体的要求: 来自新城区的分流污水，经格栅处理后进入后续污水处理构筑物; 来自老城区的合流污水平时直接进入污水处理系统。

降雨时，前期的较脏、水量较小的合流污水, 与分流污水一起经格栅后进入后续污水处理构筑物。

降雨后期的合流污水水量较大主要含泥砂，一部分经雨污溢流构筑物，在沉淀池作短暂停留, 去除部分泥砂后直接排放水体，另一部分则与分流污水一起经格栅后进入后续处理构筑物。

格栅用以去除污水中的大块悬浮物、漂浮物等污物, 以消除大块污物对后续处理系统的不良影响。

曝气沉砂池用以去除较大砂粒及其他无机污染物颗粒, 以提高污泥活性有机组分含量、减轻对管道设备的磨损、减轻后续沉淀池负荷、改善系统运行条件。

初沉池主要用以去除SS，在初沉池中，根据进水水质情况,可适时外加碳源和氨氮，以保证有足够量和适当比例的C、N、P来源，为后续生化反应正常运行创造条件。

缓冲池主要作用是在合流污水高峰流量时均衡水质、储存水量。

氧化沟是一种简易、高效、经济的城市污水处理工艺近几十年发展迅速。

在流态上, 它既是完全混合式, 又具有推流式特征。

由于沟渠溶解氧浓度的递减变化规律, 通过适当安排进水口、出水口、回流污泥入口位置，氧化沟可形成一个倒置Ａ2/０工艺。

根据硝化、反硝化、生物除磷及好氧活性污泥微生物的代谢特在缺氧段, 主要功能是脱氮，回流污泥中反硝化菌以原水中有机物为碳源，以来自好氧段的硝化液中的硝酸盐为电子受体, 将硝态氮NＯ-3-N 还原为气态氮N2。

在厌氧段，主要功能是释磷，回流污泥中聚磷菌分解释放体内聚磷酸盐,同时摄入污水中的有机物,以PＨB 及糖原等形式储存于细胞内。

对于缺氧段与厌氧段的过渡过区域,既非严格的厌氧状态，而溶解氧浓度又低于缺氧段, 脱氮与释磷过程都将存在，但都不易取得竞争优势。

在好氧段, 功能有三: 1、好氧活性污泥中微生物，使污水中有机物得到降解、去除，好氧微生物本身得以增殖, 活性污泥得以增长;２、在亚硝化菌和硝化菌作用下, 将污水中氨氮ＮH+4-N 氧化成硝态氮,主要为NＯ-3-N；3、聚磷菌体内PHB 氧化产生大量能量一部分用于从污水中过量吸收磷酸盐, 并以聚磷的形式贮存于体内，一部分供给细菌合成和维持生命。

与A2/0工艺相比,前置缺氧段不仅可优先从污水中获得碳源, 强化反硝化过程。

同时,因先经历反硝化过程，消除了硝酸盐的大量存在对聚磷菌厌氧释磷过程的不利影响。

通过对曝气器的控制, 沟渠内可形成区域大小适宜的缺氧段、厌氧段、曝气段, 在去除BOD的同时进行生物脱氮除磷, 能取得较好的氮磷去除效果。

特别是能够通过对曝气区域大小和进出水管阀门的控制，形成灵活多变的运行方式，适应污水水量、水质、季节性的变化, 具有广阔的发展应用前景。

当水质波动幅度不大时，通过前述的预处理、生物处理后的污水，一般能排放水体，但由于各种不确定偶发因素的影响, 这样考虑处理水排放存在不小风险。

当水质、水量大幅波动时这种情况更为突出。

由于水污染、生态破坏的严峻形势，城市污水处理厂必须从技术上严格把关，从工艺上确保处理水安全排放水体。

若在生物处理工艺之后设置熟化塘,不仅可在污水处理厂和受纳水体之间起缓冲作用, 还能通过藻类-动物性浮游生物－鱼类等食物链和生态系统，使BＯD、CＯD指标、细菌及氮磷等植物性营养物浓度进一步降低, 具有良好稳定的处理效果。

特别是在熟化塘系统中, 通过塘内生态系中多条食物链的物质迁移、转化和能量逐级传递、转化, 在去除污染的同时, 以水产资源形式达到物质、能量的回收，将污水处理与利用相结合, 实现污水资源化。

4 结语1. 合流制污水水质、水量波动幅度大, 技术工艺必须满足缓和冲击负荷的要求，设置缓冲池均衡水质、储存水量比较适宜。

２. 通过多个氧化沟构成若干个串、并联运行方式，在适应进水水质、水量、季节性变化方面能够发挥重要作用。

３. 通过安排适当的进出水口位置、回流污泥入口位置，氧化沟可形式一个倒置A２/0 工艺, 在去除ＢOD 的同时，能取得较好的氮磷去除效果４. 熟化塘的应用，为处理水安全排放水体，能够提供可靠的技术保证。

熟化塘投资省、运行费用低、管理维护方面、污水处理与利用相结合, 在防治水污染、保护水环境及生态环境综合治理方面具有明显优势。

如果美化熟化塘表观, 设置喷泉等设施,形成供人们休闲、游乐的人工景点, 协调城市建设中土地资源的合理配置,那么熟化塘占地面积较大这一不足就不会成为突出的问题。

ﻩCoｍｂined sewａge treａｔmｅｎt relａted ｄiscussiｏn1 ＰｒeｆaceWiｔh the inｄuｓｔriaｌizatiｏｎandｕrbanizａtion dｅvelopment, wateｒpollutｉon,worsｅnｉｎg ｗater ｓｈｏrｔage, wａteｒpolｌutiｏｎcｏntrｏl, enviｒｏnmｅnｔａl protｅctiｏn h ａs uｒｇentｎeeｄof wateｒ.Ｃhina iｓnow adoptｉng ａnew citｙor urban ｓtorｍwaｔｅr sewagｅdiｖerｓioｎｓyｓtｅm，ｂｕt the old city ｏr ｔｈeｏldｃityｉs stilｌmosｔｌy combined sewage ｓtｏrmwater draiｎａge systeｍ，a numｂeｒof combineｄsewage ｉs diｒeｃtly ｄischarged into ｔｈe water body. The confｌuｅｎｃe of tｈe ｏｌd systｅm tｏa triagｅsystem, the staｔus quｏcｏnｄｉtionｓ, aｎd maｎy of thｅoｌd ｃitｙｂuiｌt during the loｎg, ｕnｄergrouｎｄpｉpeline ｂａｓic ｓｈａpe, tｈe grounｄｃｏnｓtruｃtion crowded，naｒrｏｗroaｄs, tｈe old Comｂinｅd triａｇe systeｍmore ｄiｆfiｃuｌt ｔo cｈangｅ．Cｏｍbined ｓewaｇe ｉｓa major featurｅoｆｔｈe water qualｉtｙof ｔhe dry ａｎｄｗｅt seasonｓ，water ｃhａngｅs，lｏw BＯD ｅffluent cｏｎcenｔｒaｔｉoｎｄuring t ｈｅrａiny ｓｅasｏn iｓnｏｔcoｎdｕcivｅtｏbiochemical trea ｔment．Couｎtrｉeｓ, 2010 Chiｎa＇s urban sewage trｅaｔｍe ｎt rａtｅoｆ40 ｐercent reｑuirｅd, and thｅrｅfore the sｔｕｄｙof theｃoｎvergeｎce of eｆｆective mｅthｏｄs oｆseｗａｇe treａtment, seｗaｇe ｔreatｍent to accｅlerate the ｐａce ｏf ｔｈe ciｔyｉｓoｆgrｅat signifｉｃanｃｅ.In ｔhｉs papｅr，ｔhe coｎveｒgence of tｈｅsewage tｒｅaｔmenｔｓituaｔion，s ｏme perｓonal vieｗs.2 Requirｅments of tｈe ｓｅwage treａtmｅnt ｐｒocessMａny ciｔｉes inＣhiｎa，ｔｈe nｅw cｉty ｗith tｈｅcoexisteｎcｅof tｈｅoｌd city，Cｏmｂiｎed with thｅｓｔｒｅamｉｎg sysｔｅm cｏ-ｅxiｓt. Tｈerefｏrｅ, ｎew oｒeｘpa ｎded ｓｅwagｅtrｅａｔmｅnt pｌａnｔto meet ｔhｅoveｒall ｕrban pｌaｎniｎg ａnd draiｎａgｅｐlanｎinｇreqｕｉrｅｍents ｓｈould be able tｏmeet the folloｗiｎg requｉremｅnt ｓ：(1) Ｈave to accept mergｉｎg the oｌd citｙｓewａge ｃａpａbilitｉｅs, a strｏｎｇａbiｌｉtyｔo adａpt tｏthｅｉｍｐac ｔｌoad. Sｏuｒce of tｈｅsewａge tｒeａtmenｔplaｎt efflue ｎt is coｍpoｓed ｏｆtｗo partｓ: Fｉrst, the nｅw uｒban s ｅｗagｅdｉveｒsiｏn; Sｅｃｏnd,merｇiｎｇthe old city ｓew ａge. Cｏmpaｒｅd witｈtｈe ｃombiｎｅd sewage,ｓewaｇeｄiveｒsｉon of wａｔer qualｉty, ｗateｒ, a muｃh smaller ｒａnge oｆsewage treatｍeｎt plants rｅquirｅmｕch less adｊustmeｎｔｂuffer. Ｔhｅcｏnｆｌｕeｎｃｅｏｆseｗａgｅand rain red ｒain due tｏpre-ｒinse blｏcks, merginｇmore dｉｒty water,ｂut wａter is ｒｅlaｔiveｌy smａｌｌ；raiｎwater，the laｒgｅr the latｔeｒ,ｂut the concentration oｆorgaｎic compｏunds iｎｗaｔeｒis relatively ｓmａll.Theｒｅfore，ｐre-conｆｌuencｅraｉn waｔer,couldｂe coｎｓiderｅd tｏgether wiｔh the diｖerｓioｎof ｓｅwａｇe by prｅ-treated sewagｅｉnto thｅｓtr ｕctｕrｅ. Comｂiｎed sｅwagｅｌaｔｅrａinｆaｌl，ｗｉthｔｈe ｅxcｅptｉoｎof paｒt oｆthｅｓeｗage, togeｔher witｈtheｄiversion oｆｓeｗａgｅｂy pre－treatment ｓtructurｅs inｔｏthe seｗagｅtｒeatｍent structureｓ，anｄｔhe otｈer parｔｔo considｅr ｔhｅａｄoptiｏn of sｔormwaｔer poｌlution entering the storm sewage ｏｖｅrｆlｏｗｓtruｃｔｕreｓSｈen ｏveｒfloｗpool seｔiｎtｏthe nｅarby ｗaｔer bodyａfter．Iｎorder ｔo eｎter the ｓｔructurｅof thｅcｏmbiｎｅd sewaｇeｅffｌuent peak flow，water ｑualiｔy buｆｆer fｌuctuａtｉoｎs ｃonditiｏｎing, ｓｅｗage trｅａtment strucｔｕres regulatｉnｇｔｈe ｆｒont －ｅndｂuffer poｏl can be inｓｔａllｅd in order to bａlance ｗater ｑｕality, stoｒagｅｏf water．(2) ReliablｅBOD, ＣOD, SS rｅmoｖａl ofｎiｔrｏgｅｎaｎd phosphoｒｕs removal function aｎd features ｔo ｅnｓure the stabiliｔｙｏf the finaｌeffluｅｎt qualiｔy. Under normaｌci ｒcumstaｎces,urban sewage ｉn leｓs refrａctoryｏrgａｎｉｃmattｅr，BOD, COD ｒemoval iｓeasiｅr tｏachｉeve, ratｈer ｔhan ｔhｅcomplexity of nｉｔｒｏgen and phosphorus reｍｏv ａｌ．Ｔhe curｒｅntｅfｆｌuent sｔａndards foｒsewagｅtreatment plant effｌｕｅnt nitroｇen and ｐhｏsphoｒus indicators have strｉct rｅｑuirｅｍｅnｔs, iｔmuｓｔｂe of ｕｒbaｎseｗaｇe treatmｅnt tｏａchievｅthe ｅｆfectｉve ｒemoval ｏf nitｒo ｇen ａｎｄphosｐhorｕs.Uｎdｅr ｔhe exｉｓtinｇurban s ｅwage niｔrogen and phｏspｈorus ｒｅmoval prｏｃｅss, A2 / 0usｅd ｍoreｗｉｄely. For thｅA2／0 ｐroceｓs ｐroｂlems, tｈe prｅsent situatｉoｎof a number of ｉmprovementｓin tｅｃhnologｙ，tｅcｈnｏloｇy also ｅxiｓｔｓfor eaｃh of thｅcha ｒacｔerisｔicｓand lｉmitations of each. Ａs ａresuｌt of merｇing the water qualiｔｙcaused by sｅwage, ｗaｔer, volatile，waｓt ｅwater tｒeaｔment pｌaｎt on tｈｅimpaｃt ｏf the pｒocｅssing uｎｉts，ｉn orｄer to adapｔtｏthe ｒeceiving waｔer ｒeｑuiremenｔs,iｎorｄeｒｔｏＢＯD，COD ａｎd othｅｒinｄicatoｒs of a furｔheｒｄrop low，ｆurｔhｅｒremoｖal of ｓe ｗaｇe ｂacteriａａnd ｎitroｇｅｎ, pｈoｓphorus and other plａnt nuｔｒｉｅnｔs ｉn ｔhｅwａsｔｅwater ｔrｅaｔmｅｎt plant and rｅｃeｉving wａtｅr can be estａｂｌiｓｈed betwｅenｔhe oxidａtioｎpｏｎd.(3) Wｉtｈfｌeｘible ｏperatｉｏn moｄe, ａcｃordｉnｇto the qｕantity of sｅｗａge cｏlleｃｔioｎ, wａter qｕaｌｉty and seａsoｎal variation of ｔｈe adjustmｅnt oｐｅration. Conｖeｎtional Ａ２/ 0 proｃess,it is dｉfficuｌt ｔoｄo adｊust ｔhe flexible opeｒaｔiｏｎｍode. Howｅveｒ,A2 ／0 proｃess fｒｏm ｔhｅprinｃｉpｌe cｏｎstｉtutes ａsensｅ,ｂｅｆorｅｔhe pａragrａph in ｔhe ａerａｔion aｎd anoｘｉc pｌus anaerｏbic ｐaｒａｇraph. Tｈis principle foｒｔｈｅoxidation ｄitch techｎｏｌｏgy can be adaｐted to the formation of a vａrieｔy oｆdｉfｆｅrent waｔer quａlity, qｕaｎtiｔy，ｓeａsｏnal chaｎgeｓiｎtｈｅoperating ｍｏde.Wastｅwater ｔrｅatｍentｐlan ｔcan be estａblished aｃcording tｏtｈe aｃtual sｉtｕatiｏn ｏf the oxidatiｏn ditch mｏｒｅthaｎｔwo,ｅach fｏr a ceｒtain ａｍoｕｎt of diｔch wａｔeｒpropeｌler,bottom uniform micｒoporｏus ｇaｓexplosｉon deｖice．3 Seleｃｔion aｎd charaｃtｅrisｔｉcs of thａt procesｓOxidation dｉtch is a sｉmpｌe，efficiｅnt anｄeconomｉｃaｌmunicipaｌwastｅwateｒｔreatment technoｌogy, ｈas deｖeloped rａpｉｄlｙiｎrecenｔdｅcades．In the ｆlo ｗｐaｔtern, iｔｉs ｃｏmpletely mixed，bｕt also hａs push-flow chａracteriｓtics. As ａresulｔoｆthe ｄｅcｒｅaｓｉｎｇconｃentraｔｉon oｆdiｓsoｌved oxygen ditｃheｓc ｈangｅs anｄaｐｐｒoｐｒiate aｒｒaｎｇemｅnts throughｔhe iｎｌeｔ, ouｔleｔ, backｔｏtｈe eｎｔrance oｆthe locａtion o ｆthｅsludge, oｘidａtion diｔｃh can be invertｅd to fｏrｍa A２/ 0procesｓ:Combined sewaｇe systｅm iｎａccordaｎｃe wｉth the ｃhａrａcteriｓｔics of ｂoｔh a triage sｙstem, aｎd trｅateｄwater dischａrge requireｍenｔs．Grilｌe to remove tｈe effｌｕeｎｔｓｕｓpｅnｄeｄsolids iｎtｈｅlargｅ，ｆloatｉng deｂｒis sucｈas dirt, ｔorｅmove ｌargeｐｉeｃes of dirt on tｈe foｌｌow-uｐto thｅaｄｖｅrsｅefｆｅｃｔs of ｔｒeａtｍｅｎt ｓｙstems.Aeｒated ｇriｔchａmbeｒto remove lａrge saｎd partｉclｅs aｎd oｔher i ｎｏrｇａniｃｐｏllutantｓiｎｏrｄｅr tｏimpｒｏveＡcｔｉveｏｒｇaｎic ｃoｍpoｎent coｎtent ｉn tｈe sluｄge,rｅducinｇｗｅaｒand tｅar on the pluｍbing, the follow－ｕｐｓediｍeｎtaｔｉon ｔａnks tｏreｄｕce loａd and impｒoｖe the ｓystem opeｒating conｄitioｎs．Primarｙsedimeｎtatioｎtaｎk for reｍｏvaｌoｆthe main ＳS, Shen pool in thｅbｅgiｎｎing, ａcｃordｉng to thｅiｎfluent wａｔer quality can be a tｉmelｙad ｄｉtion to cａrbｏn aｎd niｔrｏgen in ordｅｒtｏenｓurｅaｄequａte and proper proportionｏf C，N, P souｒcｅs,iｎｏrde ｒto follow-uｐｂiolｏgical aｎd cｈemicaｌresｐｏnｓｅto c ｒeate the condｉtionｓfor normal oｐｅｒａtioｎ. Ｔhe main rolｅｏf a bｕffer pooｌof seｗage ｉn tｈe cｏmbiｎed baｌａn ｃｅｏfｔhｅwａｔｅｒqｕality peａk floｗ, storａｇeｏｆｗaｔer.Aｎd A2 /0 proceｓs, tｈe pre-hyｐoxic ｐａragraph prioｒit ｙnoｔｏnｌy to obtainｃaｒｂｏn from the wasｔｅｗater，and strengtｈen tｈe prｏcess of deｎitrificａtion．At t ｈｅsａme tiｍe,by ｆirsｔgoｉng ｔｈrｏugh tｈe process of ｄenitriｆicaｔｉon, niｔraｔe eliｍinated thｅeｘiｓtence of a lａrgｅnumber of PAＯｓａnaerｏbic pｈｏｓｐhorｕs ｒｅlease tｈe adｖerｓｅeｆｆecｔs of thｅprｏｃesｓ.Ciｔy ｏf divｅrsion fｒom new sewａge trｅatmｅnt bｙthe graｔinｇiｎto thｅsewage treatmｅnt follow-ｕp ｓtrｕctures; ｆｒｏmｔhe mｅｒging ｏf ｔhe old city sewage, usually ｄirectly into ｔhe sｅｗage treａtmｅnt system．Rainfａlｌ，tｈe prｅ－than dirt，water, ｔhｅｍerging ｏｆｓmalleｒsewage, ｔog ｅther witｈthe diｖｅrsｉｏn of ｓewａge into ｔhe folｌｏw-up by tｈe grａｔiｎg structurｅs sｅwage treatｍeｎｔ；theｍerging ｏf the lａte rainsｔｈe sewage ｗatｅr,ｌarｇely with siｌt, some thｒough sｔorｍwaｔer ｐoｌｌution oｖerflow struｃturｅｓ,iｎｔhe ｓedimentaｔｉoｎtank for aｓｈoｒt sｔay, aftｅr ｔhe removal of ｓome sedｉmｅnt，direｃt dischaｒｇe of ｗateｒbｏdies, the oｔher part，toｇeｔherｗｉtｈthe diversion ｏf sewagｅinto the follow-up by the grａｔinｇstructｕres ｔo dea ｌwitｈ.In accorｄanｃe with ｎitrificatioｎ, dｅnitrifiｃatiｏn, bioｌｏgical phospｈｏruｓｒemｏval aｃtivated sludｇe ａnd aerobic metabolｉｓm ofｍicｒｏoｒgａnisms ｉn the anoxic paragraｐh,ｔhe mａｉn funcｔioｎｉs to denitrｉfication, sｌｕｄge reｔｕrn toｄeniｔrifyｉnｇbacｔeriａas ａcarbon sｏｕrｃe of oｒganic matter in rａw waｔｅr, frｏｍthe ａerｏbic paragｒａph ｎiｔrifｉcatiｏn of nitrate soｌｕｔion forｔhｅelectｒonａｃcｅptor, tｈe nitrate （NO－３－Ｎ) back into gａｓeｏｕs ｎitrogen (N2)．Ａnaerｏbic pａragraph，ｔhｅmain funcｔioｎis to ａdｄress thｅphosphｏｒuｓ, ｔｈe rｅturn slｕdge in the ｄｅcompositｉｏｎoｆｐhoｓpｈａｔe accｕmuｌatinｇbactｅr ｉａin vivo relｅａｓe ｏｆpｏlyphoｓphaｔe, ｗhilｅintaｋe of orｇanic matter in wａｓtewaｔer to the ｆorm of PHB and gly ｃogen ｓtored in the cellｓ.Ｈypoxｉc anaeｒoｂiｃpａｒagraph for parａgraph ａnd tｈe transｉtｉon overｔhe rｅｇion, n ｅiｔheｒstrictly anaerｏbic stａｔe,And tｈｅconｃentratiｏn of ｄｉｓｓolｖed oxygeｎａbove anｄbelｏｗthe anoｘic, denitrificatｉｏn and pｈospｈｏｒus releasｅproｃeｓｓwill eｘisｔ, bｕｔaｒｅnot ｅasｙto ga ｉn ａcｏｍpetitivｅｅdge. In aerobiｃ,fuｎctions There are threｅ: ｆｉrst,Ａeroｂicａcｔivａｔed sｌudgｅmicro-ｏrｇａnisms, so that hａs beｅｎtｈｅdｅgraｄaｔionｏf organi ｃｍatｔｅr ｉn wastewateｒ, ｒeｍoved tｈemselveｓto ｔhe pｒｏlｉferation of aeｒｏbic micro-ｏrganismｓ,acｔivａted ｓlud ｇe tｏｇrowth; Sｅcond, Niｔrosａｔｉoｎnｉtrifｉｃａtion bacteria anｄfuｎｇi Ｕｎder thｅeffeｃt of ａmmonia nitｒｏgen in tｈe waｓtewａtｅr (NH +4- Ｎ) oｘｉdizｅｄｔo nｉｔra ｔe（ｍaｉｎly NO-3-Ｎ）；III PAＯs PHＢiｎvivo oxidatｉｏnoｆa laｒgｅａｍoｕnt oｆenergy, pａrｔof thｅseｗａｇe ｆｒom excessive ａｂsｏrｐtioｎof phosphｏruｓsａｌtｓ，and the fｏrｍof polｙ－Pｓtored ｉn tｈe bｏdy,ｐart ｏf thｅsup ｐly and maintｅnaｎcｅof bａcｔeriaｌsynthesis4 CｏｎclusionBy Ａeｒatorｃoｎｔrol ditchｅs can be sｕｉtable for thｅｆormａtion of ｔhe size of the hypoｘiｃregioｎｐaraｇraph, parａｇｒaph anaeｒｏｂic,aerａtｉon paragraph, at thｅsame time iｎtｈe BOD rｅmoval oｆbiｏlｏgiｃal nitroｇen anｄphｏｓphorus rｅmoval to obtaiｎa bettｅr reｍovaｌoｆnitrogenａｎｄｐhosphｏｒuｓeｆｆect．In partｉｃulaｒｔo Ａeratｉon through the pipes ｉntｏand ｏut ｏｆthe region and thｅｓize ofｔhe ｃoｎtroｌvaｌve to forｍ a flｅｘiblｅｏpｅratｉon moｄe，to adapｔｔo waｔｅｒ, sｅwａge, ｗater quａｌｉｔｙ, ｓeasｏnal ｃｈanges, there ａrｅｂroａｄprosｐectｓfｏr developmentｏｆapplications．。

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