AAO法处理焦化废水中氨氮及COD的实验研究

采用厌氧-缺氧-好氧工艺处理焦化废水,在稳定运行阶段,考察了系统及其各反应段对COD及氨氮的降解情况。结果表明,系统对COD及氨氮的去除率分别为86.7%,97.2%,最终出水COD浓度低于150 mg/L,氨氮浓度低于15 mg/L,达到国家废水排放标准。系统运行稳定时,各段对COD及氨氮的降解能力不同:COD去除率由大到小为缺氧池、好氧池和厌氧池;氨氮去除率由大到小为好氧池、缺氧池和厌氧池,初步探讨了AAO各段运行机理。     

AAO法处理焦化废水中氨氮及COD的实验研究

采用厌氧-缺氧-好氧工艺处理焦化废水,在稳定运行阶段,考察了系统及其各反应段对COD及氨氮的降解情况。结果表明,系统对COD及氨氮的去除率分别为86.7%,97.2%,最终出水COD浓度低于150 mg/L,氨氮浓度低于15 mg/L,达到国家废水排放标准。系统运行稳定时,各段对COD及氨氮的降解能力不同:COD去除率由大到小为缺氧池、好氧池和厌氧池;氨氮去除率由大到小为好氧池、缺氧池和厌氧池,初步探讨了AAO各段运行机理。     

黑臭水体治理智能水质净化设备设计及运行分析

采用模块化碳纤维作为装置主体设计黑臭水体智能水质净化设备。该设备包括进水、处理、曝气、排泥和远程管理等系统。设备进水来自于某河道应急水质处理站细格栅出水,分析其COD、氨氮、总氮和总磷浓度,结果表明:设备出水总氮浓度为20～35 mg/L,去除率约为10%;该设备对COD、氨氮和总磷具有较好的去除效果,出水COD、氨氮和总磷浓度分别低于50 mg/L、1.5 mg/L和2 mg/L,去除率分别为50%～80%、95%～99%和60%～90%。本设备对黑臭水体治理具有较好的应用效果。     

纯氧曝气与BAF联用处理含盐炼油污水

联合应用纯氧曝气与BAF工艺处理污染严重的天津石化含盐炼油污水,取得较好的处理效果。对于盐质量浓度<3 000 mg/L的污水,经该工艺处理后COD、石油类、S2-、NH3-N去除率均超过95%,出水COD平均为52mg/L;当进水盐质量浓度突然升至6 000 mg/L以上时装置运行恶化,出水COD升高到70 mg/L以上。经调整优化运行参数,装置的耐盐能力明显提高。进水盐质量浓度在4 230～6 150 mg/L时装置运行稳定,出水COD、石油类、S2-、NH3-N等均达到GB 8978—1996的一级标准要求,污水处理成本仅为6.03元/m3。     

高盐榨菜废水处理工程实例

采用化学除磷-水解酸化-厌氧接触-CASS工艺处理高盐榨菜废水。工程运行结果表明,进水盐度为0.8%～1.2%(以NaCl计),COD为1 300～2 200 mg/L,氨氮质量浓度90～150 mg/L,总磷质量浓度30～40 mg/L时。处理后出水COD为49～84 mg/L,氨氮质量浓度5～11 mg/L,总磷质量浓度0.3～0.4 mg/L,可达到污水综合排放标准(GB 8978-1996)一级标准。     

橡胶填料在厌氧-好氧一体式生物反应器处理高浓度有机废水中的作用

采用厌氧-好氧一体式折流板生物反应器,在好氧室添加废旧橡胶作为微生物附着生长填料的情况下,进行了该反应器处理马铃薯淀粉废水中COD和NH3-N的去除试验.试验结果表明:在温度为25～35 ℃,pH值为5.0～8.5时,出水COD浓度低于200mg/L,反应器COD总去除率最高达到98%,出水氨氮浓度在10mg/L左右,氨氮去除率达到74.7%.     

间歇循环延时曝气活性污泥法处理城市污水的试验

对间歇循环延时曝气(ICEAS)工艺处理模拟城市污水进行了研究,结果表明,在运行周期为4.5h,污泥负荷在0.07~0.09kg[BOD5]/(kg[MLSS]·d)的条件下,出水COD的质量浓度为15.2~42.2mg/L,COD去除率达80%~88%;BOD5的质量浓度为5.12～16.9mg/L,去除率可达85%～93%;氨氮的质量浓度为4.5～7.5mg/L,去除率为60%～70%,磷的去除率为60%～75%。说明ICEAS工艺处理南方地区城市污水是可行的。     

乙烯生产过程产生污水的深度脱氮研究

采用A/O工艺处理乙烯生产过程中产生的含氮污水。中试试验结果表明:总水力停留时间为24 h,处理能力比工业装置提高1.6倍。连续运行期:进水COD浓度190~300 mg/L、有机氮浓度10~70 mg/L、氨氮浓度14~25 mg/L、总氮浓度26~76 mg/L之间,经过处理后的出水COD浓度低于50 mg/L,氨氮浓度低于1 mg/L,有机氮浓度低于5 mg/L,总氮浓度低于10 mg/L。两种菌体组合后可以相互促进,进而提高脱氮效率。系统脱除总氮效果稳定,总氮和COD去除率分别可达80%和90%以上。     

水解酸化-A/O工艺处理污泥电渗透脱除水

针对经电渗透技术对污泥进行深度脱水后产生的脱除水,采用水解酸化-A/O工艺对其进行处理,考察了系统的启动方法及在启动期间的运行情况,结果表明在启动30 d后,出水COD为250 mg/L,氨氮质量浓度为10 mg/L以下,去除率分别在80%和90%以上;研究了好氧池HRT和DO对污水处理效果的影响,当HRT为48 h,DO质量浓度为2~3 mg/L时,达到较好处理效果;对最佳条件下系统的稳定运行进行了长期观察。结果表明,出水COD平均为120.76 mg/L,氨氮平均质量浓度为9.27 mg/L。     

鱼糜加工废水处理工艺研究

分析了鱼糜加工废水具有水温低、悬浮物多、油脂多、COD、氨氮及TP高等特点,介绍了现场取样和试验分析的方法,提出了废水处理工艺流程和设计参数。实际运行结果表明,1)采用两级物化处理工艺去除酸性蛋白质、碱性蛋白质及悬浮物后,COD去除率为60%,TP去除率为95%,SS去除率为80%;2)采用"水解酸化池+UASB+A/O池"的主体工艺,污水处理站总出水COD为85 mg/L,出水BOD为15 mg/L,出水氨氮质量浓度为10 mg/L,出水TP质量浓度为0.3 mg/L;3)该工艺系统运行稳定,处理后出水水质达到污水综合排放标准(GB 8978-1996)表4的一级排放标准。     

生物膜法A~2/O~2焦化废水处理系统缺氧反应器工艺特性

以焦化厂废水处理系统气浮设备出水为试验废水水源,在中试规模上研究了生物膜法A2/O2(厌氧/缺氧/好氧/好氧)系统中缺氧反应器的工艺特性和效果。缺氧反应器为以陶粒作填料的上流式滤池。研究结果表明,缺氧反硝化对去除焦化废水中COD有重要作用。反硝化菌可利用一些好氧微生物和厌氧微生物都难以降解的焦化废水中的有机物作碳源,反硝化反应器可去除进水中40%的COD。缺氧反硝化反应器进水碳氮质量比在5以上就可基本满足焦化废水反硝化对碳源的需求。稳定运行状况下的NO3--N容积负荷不大于0.24 kg/(m3.d)。缺氧反应器的水力停留时间不小于24 h。系统进水COD、NH3-N的质量浓度分别在1 000～2 200、200～400 mg/L范围内,对系统进水不进行稀释的条件下,水解酸化反应器HRT为20 h,缺氧反应器HRT为24 h,一级好氧反应器和二级好氧反应器HRT均为48 h,二级好氧反应器硝化液回流比为3时,生物膜法A2/O2系统处理出水的COD和NH3-N可以同时达到《污水综合排放标准》(GB8978-1996)中的一级排放标准。     

连续流状态下好氧颗粒污泥培养及其脱氮除磷性能研究

在上流式污泥床好氧颗粒污泥反应器中,以厌氧颗粒污泥为接种泥．采用人工配制的模拟废水为进水的条件下,成功培养出具有同步脱氮除磷的好氧颗粒污泥。颗粒污泥粒径在0．5~2mm,颗粒污泥沉淀速度在29～58m／h。MLSS为3077---4103mg／L。当COD的进水容积负荷为4．8kg／（m3·d）时,去除率高达96％以上。氨氮进水在160mg／L时,去除率达97％以上,出水氨氮在5mg／L以下。对总磷的去除率在22％-37％。主要是因为亚硝态氮浓度、COD／TN比和TN／TP比等对聚磷菌除磷有影响。     

Fluorescence in situ hybridization and INT-dehydrogenase activity test to assess the effect of DO concentration in aerobic biofilm reactor

To assess the effect of DO concentration in aerobic biofilm reactor, we investigated the bacterial communities and their activity utilizing the combination of two methods, fluorescence in situ hybridization (FISH) and INTdehydrogenase activity test. D-1, D-2, D-3 and D-4 reactor with different DO concentrations (1, 3, 5 and 7 mg/L, respectively) were set up in the thermostat and acclimated. The optimal DO concentration with stable nitrification efficiency in aerobic biofilm reactor was above 5.0 mg/L. FISH method showed us that higher DO concentration led to the increase of ammonia-oxidizing bacteria and nitrite-oxidizing bacteria ratios and the decrease of heterotrophs ratio. The INT-DHA activities of each reactor were 203, 153, 36 and 45 mgO₂^*/g VSS/day, respectively. The INT-DHA activities in D-1 and D-2 reactors were higher than those of D-3 and D-4 reactors, which indicates that filamentous microorganisms affected the INT-DHA activity. In the case of D-3 and D-4 reactors, as nitrification efficiency increased, INT-DHA activity also increased. In the relationship between the attached biomass and nitrification efficiency, only active biomass influenced the nitrification efficiency.     

生物膜法A^2／O^2焦化废水处理系统缺氧反应器工艺特性

以焦化厂废水处理系统气浮设备出水为试验废水水源,在中试规模上研究了生物膜法A^2／O^2（厌氧／缺氧／好氧／好氧）系统中缺氧反应器的工艺特性和效果。缺氧反应器为以陶粒作填料的上流式滤池。,研究结果表明,缺氧反硝化对去除焦化废水中COD有重要作用,．反硝化菌可利用一些好氧微生物和厌氧微生物都难以降解的焦化废水中的有机物作碳源,反硝化反应器可去除进水中40％的COD。缺氧反硝化反应器进水碳氮质量比在5以上就可基本满足焦化废水反硝化对碳源的需求．．稳定运行状况下的NO3^- -N客积负荷不大于0．24kg／（m^3·d）．缺氧反应器的水力停留时间不小于24h。系统进水COD、NH3-N的质量浓度分别在1000～2200、200～400mg／L范围内,对系统进水不进行稀释的条件下．水解酸化反应器HRT为20h．缺氧反应器HRT为24h．一级好氧反应器和二级好氧反应器HRT均为48h．二级好氧反应器硝化液回流比为3时．生物膜法A^2／O^2系统处理出水的COD和NH3-N可以同时达到《污水综合排放标准》（GB8978—1996）中的一级排放标准。     

Comparison of COD, nitrogen and phosphorus removal between anaerobic/anoxic/aerobic and anoxic/aerobic fixed biofilm reactor using SAC (Synthetic Activated Ceramic) media

In order to remove nitrogen and phosphorus simultaneously and to develop a compact process for retrofitting a conventional activated sludge system, a new fixed-biofilm reactor was designed and tested employing an operation strategy with three and two reaction phases : anaerobic/anoxic/aerobic (Run-1) and anoxic/aerobic (Run-2). Four kinds of HRT (4, 6, 8 and 10 h) were varied to investigate the effect of nitrification and denitrification in each reactor. The results of the experiments are summarized as follows. All removal rates of COD, T-N and T-P in the water treated in Run-1 were higher than those of Run-2. The average values of COD, T-N and T-P in the treated water were reduced to 5.0 mg/L, 5.6 mg/L and 3.1 mg/L in case of Run-1. The COD and T-N removal efficiencies of Run-1 were higher than that of Run-2, but the difference between Run 1 and Run 2 was almost negligible. More than 60 % T-P removal efficiency could be achieved when the HRT was above 8 hour, but the efficiency was sharply decreased to 36% as the HRT was decreased to 4 hour in case of Run-1. Although the removal efficiency of T-P in Run-2 decreased by 56 % compared with that of Run-1, the fixed biofilm reactor using SAC media reduced the volume of reactor, and high-level COD and T-N removal from domestic wastewater was performed ; stable effluent quality was thereby achieved. The performance of Run 2 with no anaerobic reactor was mostly similar to that of Run 1 with an anaerobic reactor, except for T-P removal. Hence, according to these results, anoxic and aerobic processes using SAC media could be possible for removing organics and nutrients from municipal wastewater, in case phosphorus removal is not considered for municipal wastewater with low concentration of phosphorus.     

The characteristics of microbial ecosystem response with the changes of hydrolic retention time on an aerobic fixed-biofilm biological nutrient removal system

The influence of an aerobic fixed-biofilm activity, microbial ecosystem and mass transfer with respect to HRT variation in a BNR (biological nutrient removal) system has been investigated in this study. The process used in this study was an anoxic (1)/aerobic (1)/anoxic (2)/aerobic (2) system. The study was demonstrated by several kinds of techniques such as INT-dehydrogenase activity (DHA), INT (2-(p-iodophenyl)-3-(p-nitrophenyl)-5-phenyl tetra-zolium chloride), DAPI (4’,6’-diamidino-2-phenylindole hydrochloride), and microelectrode. The study used by synthetic wastewater and HRT variation demonstrated that the DHA activity, density and heterotrophs/autotrophs ratio increased, as the HRT decreased from 8 hr to 4 hr. In comparing two aerobic reactors in fixed-biofilm process, the first aerobic reactor of the higher C/N ratio showed higher heterotrophs/autotrophs ratio and microbial activity than the second aerobic reactor. It was therefore concluded that the heterotrophs/autotrophs ratio and microbial activity were a greater influence on the first aerobic reactor, as organic loading rate was increased by HRT variation.     

Integrated anaerobic/aerobic biodegradation in an internal airlift loop reactor for phenol wastewater treatment

Anaerobic and aerobic biodegradation were integrated in an internal airlift loop reactor (IALR) by adding porous microbial carriers. In this bioreactor, aerobic activated sludge was suspended in the liquid bulk, while the anaerobic microbes were attached within the core of carriers. The integrated IALR was applied to the treatment of synthetic phenol wastewater. After 50 days’ acclimation according to co-substance strategy, the influent COD decreased from 3,700 mg/L to 400 mg/L (phenol removal rate was over 99%) with the residence time of 24 h. High performance could be achieved under the operation condition of superficial gas flow rate higher than 0.07 cm/s, temperature beyond 15°C and the microbial carrier volume fraction larger than 5%. Integration of anaerobic/aerobic biodegradation in IALR enhanced the synergetic effects between aerobic and anaerobic degradation; therefore, it has great potential in the treatment of phenol wastewater and other wastewater containing hard biodegradable organics.     

厌氧-好氧生物处理工艺用于去除水中杀虫剂(英文)

The biodegradability of wastewater containing priority pollutant pesticideVydine or triadimenol(C14H18CLN3O2) in different bio-reactor configurations was investigated.Two laboratory scale biological reactors were employed:one reactor under aerobic condition and the other under anaerobic condition.The aerobic reactor was operated at an ambient temperature(22±2) °C,while the anaerobic reactor was run in the lower mesophilic range(30±2) °C.The effect of pesticide concentration,hydraulic retention time(HRT) ,and co-substrate on the treatment process was explored,using glucose as a supplemental carbon substrate.More than 96%pesticide was removed after an acclimation period of approximately 172 d(aerobic) and 230 d(anaerobic) .The aerobic reactor achieved complete Vydine utilization at feed concentrations up to 25 mg·L-1 .On the other hand,the anaerobic reactor was able to degrade 25 mg·L-1 of Vydine.Moreover,glucose was consumed first throughout the experiment in a sequential utilization pattern.The combination of anaerobic and aerobic biological processes yielded higher biomass concentration and lower retention time than individual units.The biomass in the combined reactors was first acclimated with the corresponding pesticide.Then,the target pesticide,at a concentration of 25 mg·L-1,was sequentially treated in a semi batch mode in the reactors.HRT studies showed that 24 h HRT of aerobic and 12 h HRT of anaerobic were the optimum combination for the treatment of simulated wastewater containing Vydine,which produced Vydine effluent at concentration below 0.1 mg·L-1 .The optimum ratio of substrate(Vydine) to co-substrate(glucose) was 1︰100.     

Advanced treatment of textile dyeing wastewater through the combination of moving bed biofilm reactors and ozonation

A four-stage lab-scale treatment system [anaerobic moving bed biofilm reactor (MBBR)-aerobic MBBR-ozonation-aerobic MBBR in series] was investigated to treat textile dyeing wastewater. The MBBRs were operated in a continuous horizontal flow mode. To determine the optimum operating conditions, the effect of hydraulic retention time (HRT) and ozonation time on pollutant removal were analysed by continuous and batch experiments. The optimum operating conditions were found to be 14 h HRT for both anaerobic and no. 1 aerobic MBBRs, 14 min ozonation time and 10 h HRT for no. 2 aerobic MBBR. The average influent concentrations of chemical oxygen demand (COD), suspended solids (SS), ammonia and colour were 824 mg/L, 691 mg/L, 40 mg/L and 165°, respectively. Under these conditions, the average effluent concentrations of COD, SS, ammonia and colour were 47 mg/L, 15.2 mg/L, 5.9 mg/L and 6.1°, respectively, corresponding to total removal efficiencies of 94.3%, 97.8%, 85.3% and 96.3%, respectively. The final effluent could meet the reuse requirements of textile industry. The anaerobic MBBR process improved the biodegradability of the raw wastewater, while the two aerobic MBBRs played an important role in removing COD and ammonia. The ozonation process enhanced the biodegradability of no. 1 aerobic MBBR effluent, and finally, deep treatment was completed in no. 2 aerobic MBBR. The combined process showed a promising potential for treatment of high-strength dyeing wastewater.     

SBR法处理吗啉废水的工艺研究

文章研究了吗啉废水的SBR生化处理工艺。通过调整进水COD、TN浓度及运行周期长度、好氧段、缺氧段时间等因素,研究上述因素对序批式活性污泥法（SBR）处理吗啉废水的效果的影响。实验结果表明,进水COD为2 466 mg/L、TN=435 mg/L,运行周期为84 h,其中缺氧段为48 h,好氧段34 h,静置2 h时COD和TN的去除率分别可以达到90%和75%,系统运行稳定,SBR工艺可行。