水解酸化-UASB-SBR工艺处理改性淀粉废水研究

以 3种高浓度改性淀粉废水 (氧化淀粉、酯化淀粉和醚化淀粉 )为研究对象 ,采用水解酸化 上向流厌氧生物法(UASB) 活性污泥法 (SBR)组合工艺 ,从设计、调试、运行和技术分析来研究该工艺的可行性。研究结果表明 :该工艺处理改性淀粉废水是可行的 ,对不同种类的改性淀粉废水具有较强的适应性。     

UASB+SBR工艺处理啤酒废水的研究

江苏某啤酒厂在工艺改造的过程中,采用UASB+SBR工艺进行啤酒废水处理,经工程实际运行表明,处理后的废水达到了国家一级排放标准,同时可以实现工业废弃物的资源化再生利用.     

山东某淀粉厂污水处理改造工程

介绍了采用UASB SBR工艺处理淀粉废水的工程实例 ,UASB反应器采用中温消化 ,水力停留时间 32h ,有机负荷 7～ 8kg m3 ·d ,CODCr去除率大于 90 %。SBR池周期为 12h ,滗水率 5 0 %。在进水平均CODCr=10 0 0 0mg L时 ,处理后出水CODCr<15 0mg L ,可达标排放     

UASB+SBR工艺在屠宰废水处理中的实例研究

本论文阐述了利用UASB SBR工艺处理屠宰废水的工程取得到了良好的效果的工程事实.在全面分析整个工艺过程的基础上,通过与常规的好氧处理相比较,在同样达标排放的前提下,采用该工艺的工程初期投资和运行成本都较低,并且可以做到回收生物能和处理废物的资源化.     

上流式厌氧污泥床——生物接触氧化工艺处理白酒有机废水工程实例

结合工程实例,阐述了上流式厌氧污泥床（UASB）-生物接触氧化工艺处理白酒有机废水的可行性,分析总结了设计、调试和工程实际运行的情况.     

UASB-SBR处理工艺试验研究

介绍了升流式厌氧污泥床反应器 (UASB) -序批式活性污泥法 (SBR)处理淀粉废水的工艺 ,详细叙述了该类废水的特点、试验系统组成、UASB的启动到污泥颗粒化的过程 ,以及处理效果。试验结果表明该处理系统具有耐冲击负荷 ,处理效果稳定 ,运行管理简单 ,运行成本低等特点。废水经颗粒化UASB稳定处理后 ,出水COD可降到 5 0 0mg/L以下 ,然后经SBR稳定处理后 ,出水COD可降到 10 0mg/L以下     

UASB+生物膜/活性污泥联合工艺处理果冻生产废水

通过UASB+生物膜/活性污泥联合工艺在果冻生产废水处理中的应用工程实例,介绍了工程的设计参数与工艺调试过程。竣工验收监测结果表明,该工艺处理果冻废水可获得良好的效果,出水主要指标均满足排放标准的水质指标要求。     

皂素生产废水处理方法比较研究

皂素生产废水为难处理高浓度酸性含硫有机废水,目前常用处理工艺为UASB+SBR,但该工艺运行效果较差。文章对UASB+SBR改进工艺进行了比较研究,结果表明:在UASB中加入适量铁屑和颗粒活性炭解除了SO42-的二次抑制,COD去除率比对照组UASB高2%～3%,出水水质COD一直稳定在1300mg/L左右,去除率在95%以上,出水无异味。UASB中污泥增长速率约为0.0686d-1,是仅加活性炭污泥增长速率(0.0197d-1)的3.48倍,可见加入铁屑后污泥增长速率改变明显。该改进UASB+SBR工艺的COD去除率高于对照组,出水COD维持在200mg/L以下,略带浅黄色(20倍左右),低于GB8978-1996《污水综合排放标准》原料药料二级排放标准值(300mg/L),SBR污泥增长速率为0.3083d-1,略高于对照组。     

糟液废水处理工程综合效益实例分析

采用以调温上流式厌氧污泥床反应器（UASB） 序批式活性污泥法（SBR）为主体的联合生物处理工艺处理酿酒行业产生的糟液废水。该工艺可减少大量CODcr,BOD5超标的糟液废水的直接排放，还可产生大量沼气供综合利用，工艺技术先进，工程的综合效益较高。     

UASB——生物接触氧化工艺处理啤酒废水

以沈阳某啤酒企业为例,采用UASB＋接触氧化工艺处理啤酒废水。通过污水处理站的启动调试与运行证明,UASB＋生物接触氧化工艺处理啤酒行业高负荷有机废水工艺稳定可靠,各项指标都可达到《啤酒工业水污染排放标准》（GB19821-2005）的排放要求。     

Advanced landfill leachate treatment using a two-stage UASB-SBR system at low temperature

A two-stage upflow anaerobic sludge blanket(UASB) and sequencing batch reactor(SBR) system was introduced to treat landfill leachate for advanced removal of COD and nitrogen at low temperature.In order to improve the total nitrogen(TN) removal efficiency and to reduce the COD requirement for denitrification,the raw leachate with recycled SBR nitrification supernatant was pumped into the first-stage UASB(UASB1) to achieve simultaneous denitrification and methanogenesis.The results showed that UASB1 played an important role in COD removal and UASB2 and SBR further enhanced the nutrient removal efficiency.When the organic loading rates of UASB1,UASB2 and SBR were 11.95,1.63 and 1.29 kg COD/(m3·day),respectively,the total COD removal efficiency of the whole system reached 96.7%.The SBR acted as the real undertaker for NH4+-N removal due to aerobic nitrification.The system obtained about 99.7% of NH4+-N removal efficiency at relatively low temperature(14.9-10.9°C).More than 98.3% TN was removed through complete denitrification in UASB1 and SBR.In addition,temperature had a significant effiect on the rates of nitrification and denitrification rather than the removal of TN and NH4+-N once the complete nitrification and denitrification were achieved.     

厌氧—好氧处理高得率浆APMP废水的研究

设计了生物处理高得率浆碱性过氧化氢机械浆 (APMP)废水厌氧 (UASB)—好氧 (SBR)组合技术 ,结果表明该技术可使 APMP废水 COD去除率达 90 .3 %。并用计算机处理实验结果 ,建立了厌氧—好氧关联方程及 SBR降解 APMP废水的动力学关系式。     

皂素废水处理工程的设计与调试运行

介绍了内电解UASB厌氧好氧深度处理组合工艺处理皂素生产废水的工程实例,废水处理后出水水质达到《污水综合排放标准》(GB89781996)一级排放标准。结合工程实际,对整个系统的调试运行进行了介绍。     

高盐度采油废水生物处理影响因素

采用UASB+SBR法处理某海洋油田产生的采油废水。针对该废水难降解和高盐度的特性,探讨总盐度、Cl-浓度、处理负荷、曝气时间等因素对生物处理过程的影响,为工程设计及实际应用提供科学依据。     

Nitrogen removal via nitrite from municipal landfill leachate

A system consisting of a two-stage up-flow anaerobic sludge blanket (UASB), an anoxic/aerobic (A/O) reactor and a sequencing batch reactor (SBR), was used to treat landfill leachate. During operation, denitrification and methanogenesis took place simultaneously in the first stage UASB, and the e uent chemical oxygen demand (COD) was further removed in the second stage UASB. Then the denitrification of nitrite and nitrate in the returned sludge by using the residual COD was accomplished in the A/O reactor, and ammonia was removed via nitrite in it. Last but not least, the residual ammonia was removed in SBR as well as nitrite and nitrate which were produced by nitrification. The results over 120 d (60 d for phase I and 60 d for phase II) were as follows: when the total nitrogen (TN) concentration of influent leachate was about 2500 mg/L and the ammonia nitrogen concentration was about 2000 mg/L, the shortcut nitrification with 85%–90% nitrite accumulation was achieved stably in the A/O reactor. The TN and ammonia nitrogen removal e ciencies of the system were 98% and 97%, respectively. The residual ammonia, nitrite and nitrate produced during nitrification in the A/O reactor could be washed out almost completely in SBR. The TN and ammonia nitrogen concentrations of final e uent were about 39 mg/L and 12 mg/L, respectively.