UV/H_2O_2/O_3联用降解饮用水中的三氯硝基甲烷

分别采用O3、H2O2、UV及其联用技术降解饮用水中的含氮消毒副产物三氯硝基甲烷(TCNM),考察了不同反应条件下对TCNM的降解效果及其影响因素,并探讨了其降解机理。结果表明,单独O3、H2O2和UV工艺对TCNM的去除效果不理想,而UV/H2O2和UV/H2O2/O3组合工艺能够有效去除TCNM。当TCNM初始浓度为20μg/L、紫外光强为31μW/cm2、H2O2投加量为15 mg/L、臭氧投加量为10 mg/L时,反应150 min后,UV/H2O2、UV/H2O2/O3组合工艺对TCNM的去除率分别为82.26%和97.28%,两种工艺对TCNM的降解均符合一级反应动力学。     

微电解/Fenton法深度处理土霉素废水的研究

采用微电解/Fenton法对土霉素废水二级出水进行深度处理。正交和单因素试验结果表明,微电解法的最佳工艺条件:Fe投量为125 g/L、铁炭质量比为1.5∶1、初始pH值为4.0、反应时间为2 h,在进水COD为361～395 mg/L的条件下,处理后出水COD可降至198～207 mg/L,对COD的去除率可达44%以上;采用Fenton法进一步处理微电解出水,其最佳工艺条件:H2O2(浓度为30%)投加量为2 mL/L、初始pH值为3.0、反应时间为60 min,处理后出水COD<120 mg/L,组合工艺对COD的总去除率达到70%以上,满足《发酵类制药工业水污染物排放标准》(GB21903—2008)的要求。     

Fe-H2O2深度处理造纸中段废水的研究

为解决零价铁法处理废水时效率偏低的问题,采用Fe-H2O2法对造纸中段废水的二级处理出水进行了深度处理,分别考察了pH值、反应时间、铁炭比、曝气量和H2O2投量对色度和COD去除率的影响.结果表明：在pH值为3.5、铁炭比（体积比）为1.2、曝气量为1.4 L/min、铁屑粒径为60～80目、H2O2投量为40～60 mg/L的最优条件下,当处理时间控制在35 min时,对色度和COD的去除率可分别达到98%和77%左右,出水可回用.     

铁炭微电解/Fenton预处理对叔丁酚甲醛树脂合成废水

采用铁炭微电解/Fenton试剂法联合工艺预处理对叔丁酚甲醛树脂合成废水,考察了pH、反应时间及H_2O_2投量等因素的影响.结果表明,当原水COD为12 300～17 600 mg/L时,在控制原水pH值为2.0、反应时间为120 min的条件下,铁炭微电解对COD的去除率>50%;向铁炭微电解出水中再投加2.4 mL/L的H_2O_2(30%)进行Fenton反应,在常温(20～30℃)下反应60min对COD的总去除率>83%,废水的B/C值从最初的0.034提高到0.35左右.对预处理出水(调节pH并稀释)进行后续的生化处理,出水水质能够稳定达到<污水综合排放标准>(GB 8978-1996)的二级排放标准要求.     

Fe/C微电解耦合Fenton处理煤化工废水的效能研究

采用Fe/C微电解耦合Fenton处理煤化工废水,高效pH范围为3.0~5.0,最优Fe/C比为1.0∶1,高效H2O2投加量范围为40 mg/L~60 mg/L。微电解和Fenton的HRT均为90 min时,升流式连续流反应器经过30 d的运行,表现出较高的处理效能和稳定性,COD去除率稳定在86%左右。     

粉末活性炭/超滤工艺处理微污染原水的中试研究

采用粉末活性炭/超滤组合工艺处理微污染原水,考察了对浊度和UV254的去除效果,并根据由无因次和赋权法推导出的综合评价指标确定了最佳操作条件.结果表明,各工况的出水浊度<0.39 NTU,UV254<0.06 cm-1,水质稳定可靠;混凝剂(聚合氯化铝铁)投加量和抽停时间比对去除浊度的影响显著,粉末活性炭投加量对出水UV254的影响明显;使出水浊度和UV254达最低的运行条件不同,可分别由最小水平效应值确定各自的因素最佳水平组合;综合考虑出水水质和经济因素,确定较佳的运行工况为:混凝剂投量为1 mg/L,粉末活性炭投加量为300 mg,抽停时间比为15 min/3 min,曝气量为0.25 m3/h.     

改良A~2/O-MBBR装置处理城镇河道污水研究

分别采用2种不同填料的改良A2/O-MBBR中试装置处理深圳市布吉河道污水,考察了该工艺的启动和雨季运行特征。经过一个月的启动运行,2组系统K3和XD填料上附着的生物量分别为14.76和6.18 mg,工艺挂膜成功。雨季的进水SS为14～3 492 mg/L,平均为232mg/L,大量的泥沙进入中试装置导致污泥的MLVSS/MLSS值从0.40降至0.19,SVI从63 mL/g降至23 mL/g。通过减小污泥排放量提高MLSS至4 000～5 000 mg/L,当进水COD为42.1～215.0mg/L时,2组系统出水COD分别为2.7～80.9 mg/L和4.7～87.6 mg/L,平均去除率分别为81.8%和79.1%;当进水氨氮和总氮分别为1.58～20.88 mg/L和5.4～26.2 mg/L时,对氨氮的去除率在98.0%以上,对总氮的去除率均为23.7%。通过投加60 mg/L的甲醇作为外加碳源,可使出水总氮稳定在15 mg/L以下,达到一级A标准。当进水总磷为0.80～6.12 mg/L时,2组系统的出水值分别为0.24～0.92 mg/L和0.26～0.92 mg/L,平均去除率分别为63.6%和67.2%。     

混凝联合O_3、O_3/UV深度处理焦化废水的研究

采用混凝联合O3、O3/UV深度处理焦化废水的生物处理出水。试验结果表明:当混凝剂Al2(SO4)3的投量为900 mg/L时,对TOC、COD、色度和UV254的去除率分别为23.2%、19.5%、33.6%和27.1%,相应的出水值分别为55.5 mg/L、196 mg/L、680倍和2.53 cm-1。混凝出水经O3/UV深度处理的效果优于单独O3氧化的,当臭氧投量为2.8 g/L、反应时间为80 min、UV照射强度为30 W时,对TOC、COD、色度和UV254的去除率分别达到91.8%、73.1%、96.1%和97.6%,相应的出水值分别为5.9 mg/L、60 mg/L、40倍和0.081 cm-1,出水COD浓度达到《污水综合排放标准》(GB 8978—1996)的一级标准,且大大提高了废水的可生化性。     

铁碳微电解法预处理炸药生产废水

对炸药生产废水先采用铁碳微电解法进行预处理,其出水再采用加碱混凝曝气法进行处理.最佳处理条件:微电解的pH值为3～4,停留时间为3 h,铁碳比(体积比)为1:1,微电解出水加碱调节pH值至9-10后再曝气混凝沉淀5 h.试验结果表明,系统对COD、硝基苯类化合物、色度的去除率分别为77.8%、70.8%、95.8%.苯胺类化合物的浓度由零升至19.62mg/L,pH值由3.1升至6.9,色度由l200倍降至50倍,达到了预处理的效果.     

处理低碳源污水的倒置A2/O工艺强化脱氮技术研究

针对重庆鸡冠石污水处理厂的倒置A2/O工艺在低碳源情况下脱氮效果不佳的问题进行了生产性试验研究.在采取了投加垃圾渗滤液(投配率为0.1%)、缩短初沉池的水力停留时间为原来的1/3和控制好氧第3段的DO为0.5 mg/L等措施后,可补充碳源15%以上,系统中活性污泥性状良好,脱氮效果得到大幅提高.出水NH3-N为2 mg/L,对NH3-N的去除率为90%;出水TN为17 mg/L,对TN的去除率为54%,实现了出水达标排放.     

O3／H2O2艺去除饮用水中2-MIB的效能与机制

以2-甲基异莰醇（MIB）为嗅味物质的代表物,采用过氧化氢／臭氧氧化（O3／H2O2）工艺去除水中嗅味物质,考察了O3／H2O2工艺对水中2一MIB的去除效能与主导作用机制。研究表明,投加H2O2显著提高了单独0,氧化对2-MIB的去除效能,H2O2与O3最佳物质的量比为0．3：1,且2-MIB去除效果随pH值的升高而升高。叔丁醇对2-MIB的去除表现出显著的抑制作用,在O3氧化2-MIB过程中,除O3分子氧化2-MIB外,O3在水中自分解产生的强氧化性的羟基自由基（HO·）也具有协同氧化作用。不同浓度的天然有机物（NOM）对2-MIB去除效果的影响不同,较低浓度的NOM促进了2-MIB的去除,但随着其浓度的升高,2-MIB去除率明显降低。O3／H2O2工艺对水中2-MIB表现出良好的去除效果,是强化去除水中2-MIB等致臭微量有机物的重要工艺。     

Comparison of the efficiency of *OH radical formation during ozonation and the advanced oxidation processes O3/H2O2 and UV/H2O2

Comparison of advanced oxidation processes (AOPs) can be difficult due to physical and chemical differences in the fundamental processes used to produce OH radicals. This study compares the ability of several AOPs, including ozone, ozone+H2O2, low pressure UV (LP)+H2O2, and medium pressure UV (MP)+H2O2 in terms of energy required to produce OH radicals. Bench scale OH radical formation data was generated for each AOP using para-chlorobenzoic acid (pCBA) as an OH radical probe compound in three waters, Lake Greifensee water, Lake Zurich water, and a simulated groundwater. Ozone-based AOPs were found to be more energy efficient than the UV/H2O2 process at all H2O2 levels, and the addition of H2O2 in equimolar concentration resulted in 35% greater energy consumption over the ozone only process. Interestingly, the relatively high UV/AOP operational costs were due almost exclusively to the cost of hydrogen peroxide while the UV portion of the UV/AOP process typically accounted for less than 10 percent of the UV/AOP cost and was always less than the ozone energy cost. As the *OH radical exposure increased, the energy gap between UV/H2O2 AOP and ozone processes decreased, becoming negligible in some water quality scenarios.     

UV-based processes for reactive azo dye mineralization

In the present study, advanced oxidation processes, UV/H2O2, UV/O3, and UV/H2O2/O3 have been applied to bleach and degrade organic dye C.I. Reactive Red 45 in water solution. Influence of pH and hydrogen peroxide dosage on process efficiency was investigated. The rate of color removal was studied by measuring the absorbance at the characteristic wavelength while mineralization rates were obtained on the basis of total organic carbon (TOC) and adsorbable organic halides (AOX) measurements. Complete bleaching was achieved by all applied processes after 60 min while the maximal mineralization extent depended on the reaction conditions for each of the processes. It has been found that UV/H2O2/O3 process was the most efficient with 61.1% TOC removal and 72.0% AOX removal, respectively, achieved after a 1-h treatment. Time required for complete mineralization of RR45 by UV/H2O2 and UV/H2O2/O3 processes was determined as well.     

Improvement of oxidative decomposition of aqueous phenol by microwave irradiation in UV/H2O2 process and kinetic study

2.5GHz of microwave irradiation can cause a considerable improvement of oxidative decomposition of aqueous phenol in a UV/H2O2 system. The experimental results showed that the microwave irradiation can raise both the phenol conversion and the TOC removal efficiency up to or above 50%. Also, the microwave irradiation could considerably enhance the oxidative degradation of phenol in the UV/H2O2 system even under a suppression of thermal effect. Addition of hydrogen peroxide by more than a stoichiometric amount was critical to mineralize aqueous phenol to create a short reaction time. Also, microwave irradiation can accelerate the degradation rate of intermediates, hydroquinone and catechol, produced in the course of phenol oxidative decomposition. From the kinetic study, the disappearance rate of phenol can be expressed as dX/dt = kPH[M]0(alpha - X)(1 - X), where alpha equivalent [H2O2]0/[M]0 + kOH[OH*]/kPH[M]0, shows a good correlation with the experimental data. The kinetic analysis showed that an indirect reaction of phenol with OH radical might be dominant in the absence of microwave irradiation, meanwhile a direct reaction of phenol with hydrogen peroxide might be dominant in the presence of microwave irradiation except for low concentrations of hydrogen peroxide.     

UV／H2O2用于中水回用预处理工艺试验研究

本试验采用UV／H2O2光氧化法处理含有较高浓度阴离子表面活性剂（LAS）的洗浴废水,研究了H2O2投加量、pH值、光照时间、紫外灯光强对LAS降解率的影响,并得出了一些有益的结论。     

Photocatalytic oxidation and ozonation of catechol over carbon-black-modified nano-TiO2 thin films supported on Al sheet

The photocatalytic activity of the carbon-black-modified nano-TiO2) (CB-TiO2) thin films was 1.5 times higher than that of TiO2 thin films in degrading Reactive Brilliant Red X-3B. Photocatalytic oxidation and ozonation of catechol over CB-TiO2 thin films supported on Al sheet was investigated. The experiments showed that ozone concentrations had an important effect on TOC removal. The combined photocatalysis with UV irradiation and ozonation (TiO2/UV/O3) process considerably increased TOC removal rate compared to combined photocatalysis with UV irradiation and oxygen oxidation (TiO2/UV/O2) process, ozonation alone (O3) process, combined ozonation and UV irradiation (UV/O3) process. The complete mineralization of catechol followed pseudo-zero-order kinetics dependent upon ozone (oxygen) concentration and indicated catechol concentration did not affect the kinetics during UV/O3 and TiO2/UV/O3 (O2) processes. The kinetic study showed that the rate constants in the complete mineralization of catechol with TiO2/UV/O3 are 1.32-1.80 times higher than that of UV/O3 with the same concentration of ozone. The rate constants are 2.56-5.36 times higher than the maximal rate constants of TiO2/UV/O2 and 4.68-9.8 times higher than the maximal rate constants of TiO2/UV.     

Kinetics and mechanisms of DMSO (dimethylsulfoxide) degradation by UV/H(2)O(2) process

The objective of this study was to elucidate the degradation pathways of dimethylsulfoxide (DMSO) during its mineralization caused by UV/H(2)O(2) treatment. In order to accomplish this, we measured the concentration time-profiles of DMSO and its degradation intermediates during the UV/H(2)O(2) treatment. In addition, we proposed a kinetic model that could account for the degradation pathways of DMSO during its UV/H(2)O(2) treatment. The results show that the degradation of DMSO by the UV/H(2)O(2) treatment can be classified into two major pathways, and this is supported by both the analysis of the intermediates and total organic carbon (TOC) measurements. Firstly, DMSO was degraded into sulfate (SO(4)(2-)) through the formation of methansulfinate (CH(3)SO(2)(-)) and methansulfonate (CH(3)SO(3)(-)) as sulfur-containing intermediates. One of the two carbon constituents of DMSO was highly resistant to mineralization, due to the formation of methansulfonate, which reacted very slowly with (.-)OH k = 0.8 x 10(7) M(-1)s(-1)). Secondly, the other carbon constituent of DMSO was relatively easily mineralized through the formation of formaldehyde (HCHO) and formate (HCO(2)(-)) as non-sulfur-containing intermediates. The kinetic model proposed in this study for the degradation of DMSO by (.-)OH in the UV/H(2)O(2) process was able to successfully predict the patterns of concentration time-profiles of all components during the UV/H(2)O(2) treatment of DMSO.     

垃圾渗滤液为碳源时A~2/O法的脱氮除磷研究

以垃圾渗滤液为碳源,进行了A2/O法的脱氮除磷试验研究.结果表明,在一定范围内,随着垃圾渗滤液投量的增加,A2/O工艺的出水总氮浓度降低,而对总磷的去除率却呈下降趋势.当垃圾渗滤液投量为0.2%时,出水总氮为11.38 mg/L,对总氮的去除率为62.40%,较对照的提高了13.96%;出水总磷为0.21 mg/L,对总磷的去除率为94.35%,较对照的下降了2.61%.当垃圾渗滤液投量为0.4%时,出水总氮为9.16 mg/L,对总氮的去除率为68.59%,较对照的提高了20.15%;出水总磷为0.26 mg/L,对总磷的去除率为92.37%,较对照的下降了4.59%.之后随着垃圾渗滤液投量的进一步提高,出水总氮和总磷浓度均高于对照试验的.可见,适当掺加垃圾渗滤液可提高脱氮效果,解决原水碳源不足的问题.     

Advanced oxidation of the pharmaceutical drug diclofenac with UV/H2O2 and ozone

Diclofenac, a widely used anti-inflammatory drug, has been found in many Sewage Treatment Plant effluents, rivers and lake waters, and has been reported to exhibit adverse effects on fish. Advanced oxidation processes, ozonation and H2O2/UV were investigated for its degradation in water. The kinetic of the degradation reaction and the nature of the intermediate products were still poorly defined. Under the conditions adopted in the present study, both ozonation and H2O2/UV systems proved to be effective in inducing diclofenac degradation, ensuring a complete conversion of the chlorine into chloride ions and degrees of mineralization of 32% for ozonation and 39% for H2O2/UV after a 90 min treatment. The reactions were found to follow similar, but not identical, reaction pathways leading to hydroxylated intermediates (e.g. 2-[(2,6-dichlorophenyl)amino]-5-hydroxyphenylacetic acid) and C-N cleavage products (notably 2,5-dihydroxyphenylacetic acid) through competitive routes. Subsequent oxidative ring cleavage leads to carboxylic acid fragments via classic degradation pathways. In the pH range 5.0-6.0 kinetic constants (1.76 x 10(4)-1.84 x 10(4) M(-1) s(-1)) were estimated for diclofenac ozonation.     

Degradation of Pb--EDTA complex by a H(2)O(2)/UV process

The degradation of PbEDTA in aqueous solution by a H(2)O(2)/UV process was studied. The effect of H(2)O(2) content, pH of the solution and the presence of nitrate were investigated. PbEDTA degradation by a H(2)O(2)/UV process was shown to be accompanied by simultaneous lead precipitation. PbEDTA was decomposed rapidly in acidic solutions while lead precipitation was achieved only when the pH of the solution was higher than 6. The presence of nitrate in significant amounts (0.04 M) inhibited remarkably the degradation of the complex and metal precipitation. The degradation of CdEDTA and ZnEDTA was also studied. It was found that the decomposition of metal-EDTA complex and metal removal by the H(2)O(2)/UV process depend greatly on the nature of the metal. CdEDTA and ZnEDTA were decomposed rapidly but metal precipitation was not achieved. The major by-products of the degradation of metal-EDTA complexes observed were nitrilotriacetic acid (NTA), iminodiacetic acid (IDA), oxalic acid and nitrate.