气浮-混凝沉淀工艺处理含重金属含油废水

采用"预处理气浮除油+混凝沉淀深度处理重金属"组合工艺处理某企业超声清洗工序产生废水,该废水具有酸性强、含油量高,并含有金属铜离子的水质特征。当进水COD、BOD_5、石油类、总铜平均浓度分别为450 mg/L、135 mg/L、100 mg/L、25 mg/L时,该工艺对COD、BOD_5、石油类、总铜的去除率分别达到86.7%、92.6%、97%、98%,出水水质满足《城市污水再生利用·城市杂用水水质》(GB/T18920-2002)标准后厂区内回用。     

钼铼生产废水处理工程实例

钼铼生产废水具有高氨氮、含油和重金属的特点,采用"气浮-芬顿法-沉淀-脱氨-电絮凝"工艺处理钼铼生产废水,原水氨氮20~40g/L,COD 500~1 000 mg/L,出水氨氮<10 mg/L,COD<100mg/L,重金属<0.5mg/L,达到GB 8978-1996一级排放标准。本工程具有处理效果好和运行稳定的优势,具有较好的社会与环境效益。     

黄金矿山含氰废水深度处理工艺研究及应用

黄金矿山含氰废水污染物种类多，处理难度大，采用“MVR—氯碱深度破氰—反渗透”联合工艺对浮选废水、混合废水2种废水进行中试试验，并进行了工业应用。结果表明：采用该工艺可实现废水中铜、铅、砷、汞等的达标去除，总氰化合物降至0.1 mg/L左右，COD降至40 mg/L以下，氨氮降至2 mg/L以下；直接处理成本较低，仅为57.90元/m³。项目的成功实施，形成了一套完整的黄金矿山含氰废水处理工艺，且成本低，推广应用前景广阔。     

“絮凝沉淀-电氧化-电气浮”联合工艺处理含Mn~(2+)采选综合废水试验研究

湖南某矿山采选综合废水中含有Zn~(2+)、Mn~(2+)等重金属离子,其中Mn~(2+)含量达15.34 mg/L、Zn~(2+)含量达5.24 mg/L、COD含量181 mg/L,废水经"絮凝沉淀-电氧化-电气浮"联合工艺处理后,出水水质达到国家《污水综合排放标准》(GB8978-1996)一级排放标准。新工艺具有除锰效果好、含锰渣不反溶、操作简便、易控制等优点,在矿山废水治理与回用领域具有良好的应用前景。     

涂铁污泥吸附处理中低浓度氨氮废水

未经处理或处理不完全的含氮污染物的任意排放给环境造成极大的危害,而采用传统方法处理中低浓度氨氮废水效率不高.文中以某污水处理厂的剩余活性污泥为基质,其表面经一定浓度的氯化铁溶液改性2 h后用作吸附剂处理中低浓度氨氮废水.实验结果表明:室温时经0.15 mol/L的氯化铁溶液改性的涂铁污泥用量5 g/L,pH值为9,反应40 min即可达到氨氮去除率95%以上,且该吸附反应符合拟二级速率方程.将此工艺条件用于处理氨氮浓度为102.68 mg/L、COD为362 mg/L的实际工业废水,处理后滤液中氨氮浓度9.2 mg/L、COD 83 mg/L,达到《污水综合排放标准(GB8978-1996)》一级标准(NH4+浓度<15 mg/L和COD<100 mg/L).     

三段生物制剂-石灰法深度处理酸性重金属废水

采用生物制剂与石灰三段法深度处理株洲冶炼集团股份有限公司酸性重金属废水,工业试验运行过程中对总废水及处理后出水中各重金属浓度进行监测,并对渣样进行分析。结果表明：重金属浓度分别由锌84.63-583.39 mg/L,铅1.11-20.43 mg/L,镉2.38-19.18 mg/L,铜0.35-6.51 mg/L,砷0.71-1.19 mg/L,汞0.001 2-0.063 mg/L脱除至锌0.12-0.83 mg/L,铅0.18-0.46 mg/L,镉0.008-0.046 mg/L,铜0.12-0.19 mg/L,砷0.005-0.009 mg/L,汞0.000 12-0.002 2 mg/L,处理后出水各重金属含量均远低于《铅、锌工业污染物排放标准GB 25466-2010》。整套工艺只需控制一段水解pH值为9.0,无需硫酸、NaOH再次调节二段及三段水解pH值。配合渣中锌的质量分数达到了29.5%,可以作为锌冶炼企业的原料回收其中的重金属。     

造纸废水处理工艺研究

采用高速上流式厌氧污泥床反应器(HUASB)联合供气式低压射流(FAS-Jet)曝气氧化沟工艺处理造纸废水,对整个工艺及调试运行过程进行了详细介绍.实际运行结果表明,该工艺设计合理,运行稳定可靠,总排放口出水COD≤90 mg/L、SS≤30 mg/L、BOD5≤20mg/L,出水水质可达到<造纸工业水污染排放标准>(GB3544-2008)的要求.且该工艺基本达到封闭运行,实现了系统的零排放.     

基于高炉渣的重金属废水净化材料的研制

在炉渣基固化/稳定化重金属土壤的基础上，以高炉渣为主要材料，通过掺入不同比例的激发剂和石灰石粉，研制了炉渣基重金属废水净化材料.试验原废水中Cd2+、Cr3+、Pb2+和Zn2+的浓度分别为10 mg/L、10 mg/L、20 mg/L和50 mg/L，以重金属去除率为评价指标.结果表明，在高炉渣、激发剂和石灰石粉的质量比为55:10:35，材料总添加量为6 g/L时，废水中Cd2+、Cr3+、Pb2+和Zn2+的去除率分别达到99.60 %、99.50 %、99.70 %和97.76 %，达到了国家排放标准.      

云南某冶炼厂含铊废水深度处理工业试验研究

针对云南某铅锌冶炼厂废水水质情况,采用"生物制剂+稳定剂协同除铊"工艺对其进行深度处理工业试验,处理规模为120 m~3/h,进水Tl浓度(0.09～0.15) mg/L,处理后出水Tl0.005 mg/L,各项重金属指标均达到《铅、锌工业污染物排放标准》 GB25466-2010中的排放限值,为实际应用提供了依据和关键工艺参数。     

高效催化电解法处理酸性重金属废水工艺的研究

文章通过自行开发的高效催化电解一体化装置处理酸性重金属废水,研究结果表明:产出净化水中锌浓度0.55～1.44 mg/L,铅浓度0.11～0.46 mg/L,镉浓度0.019～0.049 mg/L,COD浓度31.89～59.12 mg/L,均低于国家《铅、锌工业污染物排放标准》(GB 25466-2010)。净化水中的氯离子含量低于锌浸出工艺回用要求150 mg/L,酸性重金属废水经处理后可实现在有色处理工艺中最大限度的回用。该工艺简单,无需加入石灰等混凝剂,产生的泥渣量少,且泥渣中锌含量超过了18%,可通过回收泥渣中的锌,创造更高的经济效益。     

含氨氮有机物和重金属离子的废水处理试验与设计

通过对某科技园含高氨氮、有机物、重金属离子废水的现场试验,确定了该类型工业废水处理工艺流程。采用两段吹脱NH3-N;两级重金属絮凝沉淀回收金属Co^2＋、Ni^2＋;缺氧、好氧组合生化、生物滤池、沸石过滤器处理工艺。处理后出水COD、NH3-N浓度分别小于100和15mg／L;重金属Co^2＋、Ni^2＋离子浓度均小于1mg／L。     

Influence of COD:N:P Ratio on Nitrogen and Phosphorus Removal in Fixed-Bed Filter

This study examined the effects of COD:N:P ratio on nitrogen and phosphorus removal in a single upflow fixed-bed filter provided with anaerobic, anoxic, and aerobic conditions through effluent and sludge recirculation and diffused air aeration. A high-strength wastewater mainly made of peptone, ammonium chloride, monopotassium phosphate, and sodium bicarbonate with varying COD, N, and P concentrations (COD: 2,500–6,000, N: 25–100, and P: 20–50 mg/L) was used as a substrate feed. Sodium acetate provided about 1,500 mg/L of the wastewater COD while the remainder was provided by glucose and peptone. A series of orthogonal tests using three factors, namely, COD, N, and P concentrations, at three different concentration levels were carried out. The experimental results obtained revealed that phosphorus removal efficiency was affected more by its own concentration than that of COD and N concentrations; while nitrogen removal efficiency was unaffected by different phosphorus concentrations. At a COD:N:P ratio of 300:5:1, both nitrogen and phosphorus were effectively removed using the filter, with removal efficiencies at 87 and 76%, respectively, under volumetric loadings of 0.1?kg?N/m3?d and 0.02?kg?P/m3?d.     

铜矿山含铜酸性废水微电解处理方法的研究

研究了采用铁碳微电解方法回收铜矿山含铜酸性废水中铜离子的可行性,并与铁屑法进行对比。研究表明,铁碳微电解法效果不同于铁屑法,具有去除效果好、反应速度快、所需时间短和节省铁屑用量的优点。反应时间比铁屑法节省三分之二以上,去除效率高20％左右。采用铁碳微电解法处理后,在处理时间30min,铁碳质量比为1：1和铁碳总量为2g条件下,实际铜矿山含铜酸性废水经一次处理后铜离子去除率达到95．6％,实际废水中铜离子浓度从98．6mg／L下降到4．3mg／L。铁碳微电解法是一种处理矿山含铜酸性废水及回收其铜资源的实用有效方法,具有很好的推广应用价值。     

焦粉吸附深度处理焦化废水试验

 以高级氧化技术处理后的焦化废水为研究对象,用焦化厂干熄焦焦粉作为吸附剂,对焦粉吸附深度处理焦化废水高级氧化出水的方法进行了研究,考察影响吸附的因素如焦粉粒径、投加量、废水pH值、吸附时间等对焦化废水COD去除率和色度的影响。试验结果表明,当焦粉粒径为0.16 mm、1 L水中投加焦粉80 g、废水pH值为4、焦粉吸附时间为2 h,最终出水的COD去除率为37.4%,色度由进水的48倍降到23倍,工艺出水水质稳定,水质可以达到《辽宁省地方排放标准》(DB 21/1627—2008)的要求,为焦化废水的达标排放提供了一条技术可行、经济合理的新途径。     

废弃等离子屏湿法冶金提银废水处理工艺研究

对等离子屏湿法冶金提银废水分别采用"中和+氧化+絮凝"、蒸发法、"中和+絮凝+蒸发法"进行处理。结果表明,"中和+絮凝+蒸发"方案对该废水中的重金属和COD等污染物均有较好的处理效果,还能通过回收硝酸和出售中和渣,实现废水处理和回收成本价值基本平衡,且冷凝水回用到生产工艺中对生产指标无影响。     

同轴电絮凝处理铅锌冶炼污酸废水的试验研究

通过采用同轴电絮凝处理技术对铅锌冶炼污酸废水进行处理的试验研究,探索同轴电絮凝反应器对污酸废水处理的适应性,得到了对污酸废水中重金属离子、氟化物等污染物的去除效率及絮凝剂选用、处理电流调整等技术参数,为实际生产中污酸废水治理方案的选择提供依据.     

2,4,6 Tri-Chlorophenol Containing Wastewater Treatment Using a Hybrid-Loop Bioreactor System

A hybrid-loop bioreactor system consisting of a packed column biofilm and an aerated tank bioreactor with an effluent recycle was used for biological treatment of 2,4,6 tri-chlorophenol (TCP) containing synthetic wastewater. The effects of sludge age (solids retention time) on chemical oxygen demand (COD), TCP, and toxicity removal performance of the system were investigated for sludge ages between 5 and 30?days, while the feed COD (2600±100?mg?L?1), TCP (370±10?mg?L?1), and the hydraulic residence time (25?h) were constant. Percent TCP, COD, and toxicity removals increased with increasing sludge age resulting in nearly complete COD, TCP, and toxicity removal at sludge ages above 20?days. Biomass concentrations in the packed column and in the aeration tank increased with increasing sludge age resulting in low reactor TCP concentrations, and therefore, high TCP, COD, and toxicity removals. More than 95% of COD, TCP, and toxicity removal took place in the packed column reactor. Volumetric rates of TCP and COD removal increased due to increasing biomass and decreasing effluent TCP and COD concentrations with increasing sludge age. The specific rate of TCP removal was maximum (120?mg?TCP?gX?1?day?1) at a sludge age of 20?days. TCP inhibition was eliminated by operation of the system at sludge age above 20?days to obtain nearly complete COD, TCP, and toxicity removal.     

Removal of Methyl Isobutyl Ketone From Contaminated Air by Trickle-Bed Air Biofilter

A laboratory-scale trickle-bed air biofilter was evaluated for the removal of methyl isobutyl ketone (MIBK) from a waste gas stream. Six-millimeter (6?mm) Celite pellets (R-635) were used as the biological attachment medium. Effects of MIBK volumetric loading rates on removal efficiency, biofilter reacclimation, biomass growth, and removal kinetics were studied under three different operating conditions, namely, backwashing and two intermittent periods (off chemical—no MIBK input; and off flow-no flow input). Backwashing of the biofilter once a week with full-medium fluidization removed the excess biomass and attained stable long-term performance with over 99% removal efficiency for loading rates less than 3.26?kg chemical oxygen demand (COD)/m3?day. The two intermittent periods could also sustain high removal efficiency for loading rates up to 1.09?kg?COD/m3?day without any backwashing. The recovery time increased with an increase in loading rates. Furthermore, the intermittent operations required a longer time to recover than backwashing. The pseudo-first-order removal rate constant decreased with an increase in volumetric loading rate. The removal kinetics showed an apparent dependency on the experimental operating conditions.     

Use of Sequencing Batch Reactor for Biological Denitrification of High Nitrate-Containing Water

The efficiency of a sequencing batch reactor in denitrification of drinking water with relatively high nitrate concentrations (40–250 mg∕L as N) was evaluated. Ethanol at a COD∕N of 2.00 was found sufficient to reduce nitrate concentrations to acceptable levels (<10 mg∕L as N). Within the first 6 min of reaction, nitrite accumulation in the range of 0.03–3.5 mg∕L as N was observed increasing with the increase of initial nitrate concentrations. In the first hour, nitrate removal was significantly high in the range of 85.7–91.5%. Anoxic reaction times of 3, 5, and 7 h were required for nitrate concentrations of 40–160, 200, and 250 mg∕L (as N) to achieve acceptable levels of nitrate and nitrite. Alkalinity of the denitrified water increased on average by 3.53 mg as CaCO3 for each milligram of nitrate reduced and pH increased from 7.3 to the range of 8 to 9. Idle times between the operation cycles, in the range of 1–14 h, had an insignificant effect on denitrification. Residual COD concentrations in the range of 5–15 mg∕L and sulfide concentrations (at initial nitrate concentrations ≥120 mg∕L as N) in the range of 0.2–0.4 mg∕L were recorded in the finished water. Elevated concentrations of COD in general are not advisable in drinking water, and specifically in this case, it could result in toxic sulfide formation in the treated water. There is a need to further study the optimization of the use of ethanol and polishing of the treated water. A sequencing batch reactor has the potential of being used as an alternative configuration for biological denitrification of drinking water.