溶气气浮/水解酸化/接触氧化工艺处理亚麻生产废水

根据克山亚麻纺织厂废水处理工程的实际情况,将印染废水和纺织综合废水分别进行预处理,然后采用溶气气浮／水解酸化／接触氧化工艺进行处理。工程设计规模为3000m^3／d,三个多月的调试运行结果表明,该工艺运行稳定,耐冲击负荷能力强。当进水平均COD为930mg／L、BOD5为516mg／L、SS为500mg／L时,出水COD≤58mg／L、BOD5≤19mg／L、SS≤51mg／L,达到了《污水综合排放标准》（GB 8978-1996）的一级标准。     

无机—有机复合膨润土用于焦化废水的深度处理

对辽宁省黑山钙基膨润土进行有机—无机复合改性,开发了一种高效、廉价的吸附剂,并将其用于焦化废水的深度处理,考察了膨润土粒径、反应温度、吸附剂投量、反应时间、pH等因素的影响。结果表明,经5g/L的Al2（SO4）3及0．02mol／L的十六烷基三甲基溴化铵（CTMAB）复合改性的膨润土,能同时去除焦化废水二级生化出水中残留的氨氮和COD,在投量为40g/L、反应时间为30min、反应温度为25℃、pH值为9的条件下,对氨氮和COD的去除率可分别达75％和47％,处理出水的氨氮和COD可分别降至25mg／L和150mg／L以下,为焦化废水的再生回用创造了条件。     

厌氧/好氧/生物滤池工艺处理牛仔服漂洗废水

采用厌氧折流板反应池／改良接触氧化池／生物滤池工艺处理牛仔服漂洗废水,运行结果表明,厌氧折流板反应池和接触氧化池的容积负荷分别达到1．05kgCOD／（m^3·d）和0．52kgCOD／（m^3·d）。当进水COD、BOD5、SS、色度和硫化物的浓度分别为667．5mg／L、220．3mg／L、396．2mg／L、580倍和38．4mg／L时,出水相应指标的浓度分别为46．8mg／L、8．1mg／L、42．2mg／L、30倍和0．2mg／L,可实现牛仔服漂洗废水长期稳定达标排放。     

水解酸化/好氧工艺处理高盐油田采出废水研究

采用水解酸化／好氧工艺对山东胜利油田某联合处理站经过“隔油-混凝-过滤”处理的高盐（12000mg／L）出水进行深度处理。结果表明：采用水解酸化／好氧工艺处理采出废水是可行的,当进水COD为110～130mg／L、HRT为7．5h、容积负荷为0．423kgCOD／（m^3·d）时,出水COD能够达到小于80mg／L的排放要求。反应器的启动采用炼油厂污泥与城市污水厂污泥为混合接种源,进水采用采出废水、生活污水和炼油厂废水的混合废水,并逐日增加混合废水中采出废水的比例,反应体系达到稳定运行所需时间较短,启动期约为20d。GC／MS分析结果表明,油田采出废水经处理后,大分子有机物的降解显著;水解酸化工艺可以降解含有苯环的有机物。     

除油/生物处理/混凝沉淀工艺处理焦化废水

采用除油／生物处理／混凝沉淀工艺处理焦化废水，经过近一年的实际运行表明，该工艺在进水COD浓度为1500～7000mg／L、NH3-N浓度为300～3000mg／L的条件下，对COD去除率〉95％、出水NH3-N稳定在10mg／L以下（去除率〉98％），出水水质达到《污水综合排放标准》（GB8978-1996）的一级标准。     

UASB—TF工艺处理食品工业废水

对食品（豆制品、乳制品、啤酒）加工过程中产生的中,低浓度有机废水可采用UASB-TF工艺进行处理,当进水COD浓度为1000-3000mg/L时,出水COD浓度可降至50-90mg/L,此工艺对季节性生产废水的处理也非常适合。     

生物流化床深度处理油田废水

采用隔油-混凝（气浮）-过滤的传统工艺处理油田废水，出水水质往往不能达到国家二级排放标准。在传统工艺的基础上，增设了三相生物流化床深度处理该废水，以使其达标排放。为提高生物深度处理的效果，分别采用了漂浮填料、悬浮填料、专性菌等多种强化处理措施，结果表明：流化床出水含油量为3．5～4．9mg／L，系统出水COD〈20mg／L，出水水质可满足国家一级排放标准的要求。     

燃奥里油电厂的含钒废水处理工艺

湛江中粤能源有限公司燃奥里油电厂采用硫酸亚铁还原／石灰中和法处理含钒、铬、铅废水，采用吹脱法处理高浓度氨氮废水，出水钒〈1mg／L，出水氨氮〈45mg／L，各项水质指标均能达到《污水综合排放标准》（GB8978-1996）的二级标准，但处理费用较高，其中药剂费为26．97元／m^3，蒸汽费、电费、水费合计为13．99元／m^3。     

三维电极-混凝法处理酵母生产废水的试验研究

采用三维电极-混凝法处理广东某酵母厂经厌氧、好氧、缺氧处理后的酵母生产废水，结果表明，采用石墨电极，在电压为9V、极板间距为4cm、电解时间为3h的条件下，废水经三维电极法处理后出水COD可降至400mg／L左右；继续采用混凝法对上清液进行处理，在聚合氯化铝投量为1～2g／L时，出水COD可降至300mg／L以下，色度可降至14倍，出水水质可达到《污水综合排放标准》（GB8978-1996）的二级标准。     

人工湿地/反渗透组合工艺处理钢铁废水的中试研究

钢铁企业的废水排放量较大，经处理达标后的外排废水中仍含有较多的溶解性总固体、铁和锰，且电导率较高。采用人工湿地与反渗透的组合工艺对某大型钢铁企业的外排废水进行处理，中试结果表明：湿地植物生长良好，人工湿地内的锰砂填料强化了湿地的除铁除锰能力，使铁、锰从1．59、0．53mg／L分别降低至0．03、0．06mg／L；在回收率为75％的条件下反渗透系统运行稳定，脱盐率达到了98％，产水水质达到了《城市污水再生利用工业用水水质》（GB／T19923-2005）及企业生产用水水质的要求。为降低处理成本，可将反渗透出水与人工湿地预处理出水混配后再回用。     

养殖废水处理工程

采用厌氧反应器（UASB）＋好氧接触生物反应器（OC）组合工艺处理养猪场高浓度有机废水,结果表明：工艺运行稳定,出水COD,BOD5,氨氮和SS的值分别为135 mg/L,28 mg/L,12 mg/L和100 mg/L,出水各项指标均达到GB8978-1996污水综合排放标准二级排放标准。     

水解酸化-膜生物反应器处理印染废水的试验研究

研究了水解酸化与膜生物反应器组合工艺对印染废水的处理效能。当进水CODCr为3500～4500mg/L、NH4+-N为55～60mg/L、色度为600倍时,经UASB-MBR系统处理后出水CODCr为120～150mg/L、NH4+-N为4～8mg/L、色度小于50倍,出水水质达到《纺织染整工业水污染物排放标准》的一级标准要求。试验结果表明,UASB-MBR系统运行良好,用于印染废水处理是可行的。     

UASB/MBR组合工艺处理抗生素废水的研究

采用UASB/MBR组合工艺处理抗生素废水,考察了其处理效果及影响因素.结果表明,当UASB的水力停留时间(HRT)为13 h、MBR的HRT为7.5 h时,系统对COD的去除效果最好,在进水COD为1 000～9 000 mg/L的条件下,出水COD可降至199 mg/L,对COD的总去除率可达80%以上.     

混凝沉降硅藻土吸附处理印染废水的研究

本研究利用混凝沉降硅藻土吸附处理印染废水,使处理后的废水达到国家行业一级排放标准。研究结果表明：每处理100mLCOD为211．74mg／L的废水需加入浓度为10％的聚合氯化铝0．5mL,搅拌20min,进行混凝沉降,处理后的废水COD为155．08mg／L。每处理100mLCOD为155．08mg／L的废水需加入2．0g硅藻土,搅拌20min,处理后的废水COD为60mg／L,色度为10,达到国家一级排放标准。此法相对于其他处理方法具有工艺简单、沉降速度快、吸附处理效果好等优点,具有广阔的应用前景。     

Treatment of phenol and cresols in upflow anaerobic sludge blanket (UASB) process: a review

Upflow anaerobic sludge blanket (UASB) process has been successfully applied in the treatment of municipal and industrial wastewaters. Several researchers have investigated the suitability of the process for the treatment of phenols and phenolic wastewaters. The anaerobic treatment of phenols is still at an investigative stage. With increasing recognition of the UASB process, feasibility studies on the treatment of wastewater containing phenol and cresols (o-, m- and p- isomers) in UASB have been reviewed. It is reported that phenol concentration up to a range of 500-750 mg/L is generally not inhibitory to the UASB process. Phenol concentrations greater than 500 mg/L can be effectively treated with acclimatization of inocula, recirculation of the treated effluent and/or supplementing with co-substrates such as glucose, VFA and dilute molasses. The degradability of phenol is more than p-cresol, which in turn is more than m- and o-cresol.     

混凝气浮/UASB/一体化氧化沟处理淀粉生产废水

采用混凝气浮/UASB/一体化氧化沟工艺处理玉米淀粉生产废水,介绍了工程设计、调试和实际运行情况.实践表明,该工艺处理效果稳定可靠(出水COD平均值为65.5 mg/L,BOD5平均值为19.1 mg/L,SS平均值为53.7 mg/L),高效节能.     

Removal of carbon and nutrients from domestic wastewater using a low investment, integrated treatment concept

An integrated chemical-physical-biological treatment concept for the low-cost treatment of domestic wastewater is proposed. Domestic wastewater was subjected to a chemically enhanced primary treatment (CEPT), followed by treatment in an upflow anaerobic sludge blanket (UASB) reactor. In addition, a regenerable zeolite was used to remove NH4+, either after CEPT pretreatment or after biological treatment in the UASB reactor. The CEPT pretreatment consisted of the addition of a coagulant (FeCl3) and an anionic organic flocculant and removed on average 73% of the total chemical oxygen demand (COD(t)), 85% of the total suspended solids, and 80% of PO4(3-) present in the wastewater. The UASB system, which consequently received a low COD(t) input of approximately 140 mg/L, was operated using a volumetric loading rate of 0.4 g COD(t)/L. d (hydraulic retention time [HRT]=10 h) and 0.7 g COD(t)/L. d (HRT=5 h). For these conditions, the system removed about 55% of the COD(t) in its influent, thus producing an effluent with a low COD(t) of approximately 50 mg/L. The zeolite, when applied in batch mode before the UASB reactor, removed approximately 45% of the NH4+, whereas its application as a post-treatment cartridge resulted in almost 100% NH4+ removal. The simple design and relatively low operating costs, due to low costs of added chemicals and low energy input (estimated at Euro 0.07-0.1 per m3 wastewater treated), combined with excellent treatment performance, means that this system can be used as a novel domestic wastewater treatment system for developing countries. Therefore, the system is called a Low Investment Sewage Treatment (LIST) system.     

UASB/水解酸化/曝气生物滤池处理高浓度聚酯废水

介绍了UASB／水解酸化／曝气生物滤池工艺在聚酯废水处理中的应用，并进行了工艺参数的选择和运行效果的分析。结果证明，当进水COD、BOD5浓度分别为（1—1．2）×10^4mg／L和3450—4200mg／L时，处理出水COD≤150mg／L，BOD5≤30mg／L，能够达到《污水综合排放标准》（GB8978--1996）的二级排放标准。     

乳酸链球菌素生产废水处理工艺分析

某生物制药企业排放的生产废水中含乳酸链球菌素等大量抗生素和有机物,其COD、BOD_5和Cl~-均较高.该企业采用UV/TiO_2/Fenton-水解酸化-UASB-A/O工艺进行处理.经过两年多的稳定运行,出水COD为92 mg/L、BOD_5为20 mg/L、NH_3-N为12 mg/L,完全满足<污水综合排放标准>(GB 8978-1996)的一级标准.此外,甲烷产气量达到300 m~3/d,可为热交换器提供能源.     

Effect of process configuration and substrate complexity on the performance of anaerobic processes

The roles of substrate complexity (molecular size of the substrate) and process configuration in anaerobic wastewater treatment were investigated to determine optimal methanogenic technology parameters. Five substrates (glucose, propionate, butyrate, ethanol, and lactate) plus a mixed waste (60% carbohydrate, 34% protein, and 6% lipids) were studied under five reactor configurations: batch-fed single-stage continuous stirred tank reactor (CSTR), continuously fed single-stage CSTR, two-phase CSTR, two-stage CSTR, and single-stage upflow anaerobic sludge blanket (UASB). The substrate feed concentration was 20,000 mg/L as COD. The solids retention time (SRT) and hydraulic retention time (HRT) in the CSTR reactors were 20 d, while HRT in the UASB was 2 d. All reactors were operated for at least 60 d (equal to 3SRT). Substrate complexity was observed to be less significant under two-phase, two-stage and UASB reactor configurations. Two-phase CSTR, two-stage CSTR, and single-stage UASB configurations yielded the lowest effluent chemical oxygen demands (130-550, 60-700, and 50-250 mg/L, respectively). The highest effluent chemical oxygen demands were detected when feeding glucose, propionate, and lactate to continuously fed single-stage CSTRs (10, 400, 9900, and 4700 mg/L COD, respectively) and to batch-fed single-stage CSTRs (11, 200, 2500, and 2700 mg/L COD, respectively). Ironically, the one stage CSTR--most commonly utilized in the field--was the worst possible reactor configuration.