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。     

生物膜法A2/O2焦化废水处理系统中好氧反应器工艺特性

以焦化厂废水处理系统气浮设备出水为水源,在中试规模上研究了生物膜法A2/O2系统中好氧反应器的工艺特性和效果.研究结果表明,系统进水COD为1 000～2 200 mg/L,NH3-N质量浓度为200~400mg/L,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3,一级好氧反应器COD容积负荷为0.40 ks/(m3·d),二级好氧反应器COD容积负荷<0.07 kg/(m3.d).NH3-N容积负荷为0.022 kg/(m3·d)时,生物膜法A2/O2系统处理出水COD和NH3-N浓度可以同时达到<污水综合排放标准>(GB 8978-1996)中的一级排放标准.     

A_1-A_2-O-M工艺处理焦化废水的实验研究

采用厌氧-缺氧-好氧-复合(A1-A2-O-M)工艺处理焦化废水,考察了外加碳源和碱源对焦化废水COD和NH4+-N脱除效果的影响。试验结果表明:外加甲醇和碳酸氢钠对焦化废水的硝化和反硝化效果影响很小;不外加碳源和碱源时,焦化废水经处理后出水的COD和NH4+-N平均质量浓度分别为125.0mg/L和1.12mg/L,分别达到《污水综合排放标准》(GB8978-1996)中的二级标准和一级标准。     

A1-A2-O-M工艺处理焦化废水的实验研究

采用厌氧-缺氧-好氧-复合.(A1-A2-O-M)工艺处理焦化废水,考察了外加碳源和碱源对焦化废水COD和NH4+-N脱除效果的影响.试验结果表明外加甲醇和碳酸氢钠对焦化废水的硝化和反硝化效果影响很小;不外加碳源和碱源时,焦化废水经处理后出水的COD和NH4+-N平均质量浓度分别为125.0 mg/L和1.12mg/L,分别达到<污水综合排放标准>(GB8978-1996)中的二级标准和一级标准.     

厌氧与缺氧/好氧交替式SBR处理印染废水

开展了厌氧与缺氧/好氧交替式SBR处理实际印染废水的小试研究。厌氧SBR处理印染废水的COD平均去除率为75%,平均出水COD为237 mg/L。缺氧/好氧交替式SBR采用分段进水和外加碳源的方式处理厌氧SBR出水,两段进水分配比为800 mL∶200 mL时,处理效果较佳,仅因反硝化碳源不足导致出水总氮未满足《纺织染整工业水污染物排放标准》(GB 4278—2012)的直接排放标准;外加葡萄糖的实际与理论投加量之比为3时,处理效果最佳,出水平均COD为79 mg/L、氨氮为0.4 mg/L、总氮为13.5 mg/L、总磷为0.14 mg/L,均满足直接排放标准。     

A/O/O生物膜反应器处理锦纶废水的影响因素

试验采用A／O／O生物膜系统对锦纶废水进行处理，考察了硝化液回流比、水力停留时间、DO和进水COD及TN浓度对系统处理效果的影响。结果表明，当进水COD和TN分别为480-525mg／L和24-26mg／L，硝化液田流比3，单个反应器HRT为3．9h，好氧池Ⅰ和Ⅱ内DO均为3．0mg／L左右时，系统COD和TN去除率分别迭95％和70％，出水氨氮低于1．5mg／L，满足GB8978-96污水综合排放一级标准。     

O1/A1/O2/A2工艺处理焦化废水试验研究

通过对短程硝化反硝化工艺的研究,开发了好氧/厌氧/好氧/缺氧(O1/A1/O2/A2)生物脱氮新工艺并用于焦化废水的处理。考察了NH4+-N、COD、TN对反应器运行效果影响。结果表明,当进水COD平均为3 012.9 mg/L,NH4+-N、TN、挥发酚、总氰平均质量浓度分别为590.5、608.4、361.8、34.5 mg/L;出水COD平均为81.7 mg/L,出水NH4+-N、TN、挥发酚、总氰的平均质量浓度分别为0.1、9.9、0.1、0.1 mg/L,出水指标达到国家污水综合排放一级标准,A/O工艺处理这种焦化废水TN偏高,而用O1/A1/O2/A2工艺可以解决这一问题,实现了TN脱除。考察了温度、DO、pH对短程硝化影响。结果表明,在DO质量浓度为1.0～1.5 mg/L、温度在30～35℃、pH 7.5～8.0,系统能够进行稳定短程硝化反硝化。     

一体化复合式生物反应器的脱氮研究

利用自制的一体式缺氧/好氧(A/O)复合式生物反应器(HBR),对高浓度氨氮废水进行了脱氮研究.结果表明,当进水COD浓度在950～1100 mg·L-1、氨氮浓度增加到150 mg·L-1时系统COD、氨氮去除率开始下降;在好氧区内检测到大量的NO-2-N积累,表明HBR的脱氮作用部分是通过短程硝化-反硝化途径实现的.且复合式生物反应器填料内部存在多种多样的微环境类型以及缺氧/好氧内循环,造成反应器缺氧、好氧区都发生了同步硝化-反硝化反应.     

同时好氧缺氧生物反应器处理垃圾压缩站废水

试验采用同时好氧缺氧反应器处理垃圾压缩站废水。试验结果表明。反应器对垃圾压缩站废水的CODcrNNH^＋4-N和TN具有较好的处理效果。试验过程中，CODDcr NH^＋4-N和TN的平均去除率分别为71．30％，87．50％和67．76％。电子计量学研究表明。同时好氧缺氧生物反应器内存在比传统短程反硝化反应消耗碳源更少的脱氮反应形式。微环境和宏观环境理论表明。反应器具备厌氧氨氧化反应发生的条件。     

滤料体积比对前置反硝化BAF处理效果的影响研究

在进水流量16.5 L/h,回流比200%,滤速2.8 m/h的工况下,考察了前置反硝化BAF工艺的处理效果。结果表明:在缺氧段与好氧段滤料体积比为1∶1、1∶2、1∶3条件下,出水COD、NH3-N和TN均能达到《城镇污水处理厂污染物排放标准》(GB 18918—2002)的一级标准;在滤料体积比为1∶4条件下,出水COD超出排放标准,而NH3-N和TN的出水效果仍满足一级排放标准。     

利用以A~2/O法为主体的工艺处理垃圾填埋场渗滤液的研究

A2/O法,是由厌氧、缺氧以及好氧三个部分组成的二级脱氮工艺,广泛运用于各类污水的处理当中。贵阳的高雁垃圾填埋场,是按照建设部标准建立起来的大型垃圾填埋场。用A2/O法进行处理其产生的渗滤液,前段设UASB反应池为厌氧段(A段),中间设A/O池为缺氧——好氧段(A/O段)。经过几年的运行后,进水的碳源降低,绕过厌氧段直接进水。采取增大回流比、增加碳源等方式来促进A/O池的硝化反应、反硝化反应的脱氮效率,达到良好的处理效果。。     

生物膜法A^2/O^2工艺处理焦化废水的实验研究

实验采用A2/O2生物膜法的工艺流程,对太原市某焦化厂的焦化废水进行处理。首先废水经过厌氧柱,经过厌氧水解酸化的预处理后,依次进入缺氧池、好氧池、沉淀池、好氧池、沉淀池,最终出水。实验表明,进水CODCr为1 200～2 200 mg/L,NH3-N为200～1 000 mg/L,系统对其的去除率比较稳定,能使出水的CODCr和NH3-N平均浓度达到《污水综合排放标准》（GB8978-1996）的二级级标准和一级标准。     

多点进水改良型复合A2/O处理低C/N污水

以低C/N比城市生活污水为研究对象,重点考查了改良A²/O工艺的脱氮除磷性能。原水按一定比例分配给厌氧池和缺氧池,以合理分配厌氧释磷和缺氧反硝化所需的碳源;在好氧池和缺氧池中分别投加填料,以稳定系统的硝化和反硝化效果,提高系统的脱氮性能;厌氧池和缺氧池出水都直接进入好氧池。在进水COD/TN平均为5.54,HRT为11 h,SRT为15 d,MLSS为3000～4000 mg·L^-1,污泥回流比为50%条件下,通过三种不同进水分配比以及三种混合液回流比的对比试验研究,得到系统最佳进水分配比5:5,对分配脱氮和除磷所需碳源更加合理;而混合液回流比为200%,过高会破坏缺氧池的溶解氧环境,过低又会导致缺氧池反硝化作用不能充分发挥。在最优工况下COD、NH₃-N、TN和TP出水水质分别为29.7、0.1、11.8和0.42 mg·L^-1,平均去除率分别达到87.8%、99.7%、72.4%和91.3%,出水优于国家GB 18918-2002一级A排放标准,并且在缺氧池中发生了明显的反硝化除磷现象。     

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.     

Optimisation of anaerobic/anoxic/oxic process to improve performance and reduce operating costs

A laboratory‐scale anaerobic/anoxic/oxic reactor system was used to treat synthetic brewery wastewater for 1 year. The objectives were to enhance denitrifying phosphorus removal, improve biological nutrient removal and reduce operating costs. Three operational strategies were tested: (1) controlling nitrate recirculation to stimulate the growth of denitrifying phosphate‐accumulating organisms; (2) adjusting the volume ratio of the anaerobic/anoxic/oxic zones to enhance anoxic P uptake; (3) bypassing a part of the influent flow into the anoxic zone to maximise anoxic P uptake and denitrification. The results showed that not only was anoxic P uptake enhanced but also energy consumption for aeration could be reduced when the anoxic effluent NO₃^?‐N concentration was controlled between 1 and 3 mg L^?1. The optimal volume ratio of the anaerobic/anoxic/aerobic zones in this system was found to be 1:1:2. The optimal bypass flow ratio was 0.32. The results indicated that the optimal strategies could improve treatment performance and reduce operational costs, but there was still a challenge to treat wastewater with low C/N ratio. Copyright © 2006 Society of Chemical Industry     

单级SBR厌氧/好氧/缺氧处理中期垃圾渗滤液深度脱氮

为了考察单级SBR处理实际中期垃圾渗滤液深度脱氮的可行性,采用单级SBR在“厌氧/好氧/缺氧”(AOA)运行方式下处理实际中期垃圾渗滤液。试验发现,厌氧/好氧/缺氧交替运行下驯化的微生物能在厌氧段消耗胞内糖原,并将水中部分溶解性有机物以聚羟基脂肪酸酯(PHAs)形式储存;在好氧段微生物消耗胞内PHAs,转化为胞内糖原,氨氧化的同时也伴随着同步硝化反硝化脱氮;好氧段氨氧化结束后贮存的碳源(PHAs和糖原)能为后置缺氧反硝化提供碳源。经长期试验研究,进水COD、NH₄⁺-N、TN浓度分别为6430～9372 mg·L^-1、1025.6～1327 mg·L^-1、1345.7～1853.9 mg·L^-1,出水COD、NH₄⁺-N、TN浓度能达到525～943 mg·L^-1、1.2～4.2 mg·L^-1、18.9～38.9 mg·L^-1。在未投加外碳源的情况下,SBR法AOA运行方式下能够实现中期垃圾渗滤液的深度脱氮,出水TN<40 mg·L^-1。其中,好氧段(DO<1 mg·L^-1)通过同步硝化反硝化去除TN占总去除量的1/3左右;缺氧后置反硝化去除的TN占总去除量的2/3左右。     

Removal of nitrogen and phosphorus using a new biofilm process-INRS (Innovative Nutrient Removal System)

Adopting various process configurations may perform biological nutrient removal (BNR) from sewage. To get a compact BNR process, biofilm reactors were chosen for nitrification and denitrification. Enhanced biological nitrogen and phosphorus removal in a new fixed biofilm reactor was investigated in operation strategies with two reaction phases: anaerobic/anoxic/aerobic process with post-anoxic/aerobic biofilm process (Run 2A) and Run 2A with exogenous carbon sources for denitrifying and removing phosphorus (Run 2B). The influent used was “J” WWTP influent that consisted of wastewater from nearby a factory district area, leachate, and sewage. Therefore, the influent contained a great deal of refractory organic compound. The mean concentrations of COD, NH ₄ ⁺ -N and T-P in the influent were about 297.0 mg/L, 64.92 mg/L and 2.63 mg/L, respectively. The C: N: P ratio of influent was 113: 25: 1 and it was not suitable for growth of microorganism compared with 100: 5: 1 of proper growth C:N:P ratio. But, at a total HRT of the system of 16 hours in Run 2, the system worked successfully obtaining removal of COD, T-N and T-P of the case of Run 2A, 80.1 %, 74.9 %, and 50.8 %, respectively, and Run 2B(c) with exogenous carbon source (Na-acetate) obtained 86.2 % T-N removal efficiency. The results of this research showed that an innovative nutrient removal system (INRS) process packed with SAC media could be applicable for treatment of nutrients from municipal wastewater.     

组合工艺处理难降解焦化废水试验研究

采用A^2／O-臭氧氧化．活性炭过滤的组合工艺对焦化废水进行处理,以解决其达标排放。进水COD1267mg／L,NH3-N113mg／L,SS150mg/L左右时．工艺对COD、氨氮、SS的去除率分剐达到93％、95％、95％,出水满足《污水综合排放标准》（GB8978-1996）一级标准。试验结果零明该工艺对焦化摩水...     

城市污水连续流A/O系统富氧条件下脱氮特征

基于添加流离填料的连续流A/O生物膜反应器,研究城市污水生物脱氮特征。系统在富氧条件（溶解氧大于1.5 mg·L^-1）下连续运行113 d,氨氮和总氮去除率均稳定在50%。系统稳定运行阶段好氧区和出水均无亚硝酸盐或硝酸盐积累现象,表现出良好的同步硝化反硝化特征。16S rDNA分析表明,实现这一现象的主要功能细菌为好氧区存在的好氧反硝化菌;FISH分析表明,不同好氧区的好氧反硝化菌的活性和相对数量不同。结果证明系统内发生的同步硝化反硝化主要由好氧反硝化作用实现,硝化反应产生的硝酸盐类物质得到去除。根据试验结果与微生物学分析,提出了在富氧水环境中通过同步硝化反硝化途径脱氮的生物膜模型。