臭氧-MBR工艺深度处理印染废水中试研究

采用臭氧-膜式生物反应器(MBR)工艺对某工业园印染废水二级生化处理出水进行了深度处理,达到企业回用水要求。结果表明,在进水COD低于100 mg/L、色度为40倍的条件下,当臭氧投加量为15～20 mg/L、MBR的水力停留时间为4～6 h、气水比为15∶1时,出水COD<40 mg/L、色度为2倍,出水水质可满足企业对回用水的水质要求。     

印染废水色度深度处理的实验研究

印染废水由于色度高,处理难度较大.通过生化处理的印染废水,仍然具有一定的色度.本研究使用混凝剂和Fenton试剂对膜生物反应器(MBR)出水进行深度处理.实验分别考察了混凝沉淀法和Fenton试剂法中加药比、投药量、pH值及反应时间对印染废水色度去除率的影响.结果显示Fenton试剂法效果明显优于混凝沉淀法,色度去除率达到92%.Fenton试剂法的最优参数如下:加药摩尔比(双氧水:硫酸亚铁)为1:3.1,投药量为500 mL膜出水投加10 mL浓度为10 g/L的FeSO4+0.126 mL浓度为30%的H2O2,pH值为4.45,反应时间为5 min.     

微生物强化处理印染废水的中试研究

以绍兴县综合性印染废水为处理对象,采用混凝一水解酸化一好氧工艺,并且在好氧单元中投加微生物菌剂进行中试研究,探讨了该工艺对印染废水的处理效能。结果表明,投加菌剂后,该系统出水大大改善。投加茵剂前,出水CODl91mg／L,投加菌剂后,出水111mg／L。当该系统高效茵群已形成后,不投加茵剂20天内,该系统仍然可以保持出水CODl21mg／L。当该系统MLSS大量降低后,该系统出水仍然可达120mg／L,此现象说明该系统耐受冲击能力强,且为污泥的减量化研究可能指明了一个新方向。     

用固定化细菌处理印染废水的中试研究

<正> 印染废水数量大、分布广、污染环境严重,印染废水中染料是生物难降解的化合物,多年来人们为寻找高效、稳定、经济的处理方法做了大量的研究工作。通常采用絮凝、电解、吸附和氧化等物理化学的方法,由于耗电量大,成本高,并具有二次污染,在我国也难于推广,国内目前处理印染废水多用活性污泥生化曝气工艺,处理效果不大理想,脱色效果难以达到排放标准。     

水解酸化0生物接触氧化0混凝气浮工艺处理印染废水

根据印染废水水质特点，选择了水解酸化．生物接触氧化．混凝气浮处理工艺。运行结果表明：在平均进水水质CODcr 1100mg／L，BOD5294．5mg／L，SS197．2mg／L，色度580倍的条件下，其去除率分别为89．6％、89．4％、71．0％和87．8％，出水水质可达到（GB4287-92）中的二级标准。     

改性高岭土处理模拟印染废水效果研究

本文采用煅烧方法活化高岭土,采用聚合硫酸铁处理煅烧活化后的高岭土,通过对比2种高岭土的表征,利用它们处理大红染料模拟印染废水的色度,分析2种高岭土表征对模拟印染废水色度处理效果的相关性。结果表明,聚合硫酸铁改性煅烧活化后的高岭土比煅烧活化高岭土在BET表面积、吸附体积及BJH吸附平均孔径的数据显示更优,而运用聚合硫酸铁改性煅烧活化后的高岭土处理模拟印染废水色度的去除率更高,可高达99.94%。     

印染废水的生物处理技术

本文对高效脱色菌株与菌群的筛选、驯化和利用、藻类和藻菌共生系统对染料的分解代谢以及固定化细胞生物反应器等印染废水的生物处理技术及其作用机理作了扼要的综述。     

新型膜生物反应器处理印染废水的研究

印染废水在工业废水中占有较大的比重,其成分复杂,污染物浓度高、难于降解,因而也是处理难度大、治理费用高的废水。本试验将膜生物反应器与活性炭技术结合应用,着重研究其在处理印染废水时的规律和活性炭去除色度的作用。通过厌氧槽内厌氧微生物的处理,好氧反应器中好氧活性污泥与PAC的综合处理,中空纤维膜的过滤,用新型膜生物反应器处理印染废水,使出水达到排放标准,并对实验结果以及各处理单元的贡献及作用进行了分析研究。     

用无机载体固定脱色混合菌处理印染废水的模拟试验

<正> 随着印染工业的发展,印染废水排放量增大,废水中染料、浆料和化学助剂等使废水的成份复杂,色度深,水质不稳定,COD高。这些生物难降解的化合物在环境中造成污染。近年来,人们借助微生物对染料进行降解及处理废水,收到了较好的效果。国内外已分离到能降解染料的菌株有十几个属,几十种,其中以假单胞菌属的菌最多。这些菌多数对偶氮染料起降解作用。也有人分离到对染料脱色的酵母菌。沈如玉等分离到一混合脱色菌株ZE—1,投加到丝绸印染废水生化处理系统中起到良好的效果,韩树琴等利用蜡状芽孢杆菌固定化细胞降解酸性红B的研究。本实验室筛选出能对90     

印染废水治理研究

本文介绍了用生物接触氧化法治理南充地区印染厂废水试验工艺条件选择，研究了有机负荷、水力负荷和温度对废水处理效果的影响，并观察了微生物的生长和发展规律。试验证明，本法能有效的处理印染废水，在适宜条件下，COD和色度的去除率分别为74．4％、92．0％，而后再经混凝处理可使二沉池出水COD去除率高达88～90％、色度为0、pH在7～8。     

生物-微电解组合工艺处理染料废水研究

采用上流式污泥床过滤器（upflow blanket filter，UBF）＋曝气生物滤池（biological aerated filter，BAF）＋微电解的组合工艺，对盐度接近2％、色度和COD分别约为8000倍和600．5mg／L的染料废水进行处理。经过连续120d的稳定运行后，组合系统处理效果良好，脱色率和COD去除率分别达到99％和75％以上。UBF和微电解单元均可以大幅度提高废水的可生化性，有利于进一步的生物处理。UV—Vis扫描和GC—MS分析表明，该组合工艺能破坏染料的发色基团和共轭双键，并能高效降解原水中的酚类、氯代有机物和复杂的杂环类化合物。实验结果表明，UBF＋BAF＋微电解的组合工艺是处理染料废水的一种有效方法。     

水解酸化/生物膜法SBR处理印染废水实验研究

针对印染废水污染物浓度高、种类多、色度高、可生化降解性差等特点,对印染废水采用水解酸化/生物膜法SBR进行处理,结果表明,该处理工艺处理效果较好,出水COD、色度、BOD5、NH3-N浓度分别为60~100 mg/L、50~70倍、20~24 mg/L、5~10 mg/L,平均去除率分别达到92.1%、86.5%、95%、90%。     

电絮凝-微纳米气泡臭氧氧化工艺处理高盐印染废水的研究

高盐印染废水具有色度大、可生化性差、水质水量不稳定等特点,以致难以通过传统生化方法得到高效处理。将微纳米气泡臭氧（O₃）高级氧化工艺与电絮凝（EC）工艺组合处理高盐印染废水,探究2种工艺的耦合作用,并研究电流密度、盐浓度、pH等因素对组合工艺处理效果的影响。结果表明,单独EC法处理印染废水在一定程度有脱色和去除有机物的效果,但效率低。在相同条件下,EC和O₃同时处理(EC+O₃)150 min与EC处理30 min后再经O₃处理120 min (EC→O₃)过程相比,EC+O₃处理印染废水的效率更高,去除1 mg COD消耗的O₃仅为0.46~1.39 mg。随着电流密度和pH的升高,EC+O₃工艺的色度、UV₂₅₄、COD和TOC去除率增加;盐浓度的增加对色度、UV₂₅₄、COD和TOC去除率影响不大。比较了O₃微纳米气泡工艺、高级氧化法H₂O₂/O₃、EC+O₃ 3种方法对新疆和浙江实际印染废水的处理效果,并进行了经济性分析。3种微纳米气泡处理工艺的单位污染物电能消耗量（EE/O）由低到高为EC+O₃ < H₂O₂/O₃ < O₃。

     

粉末活性焦强化A/A/O工艺处理煤气化废水的中试研究

煤气化废水水质复杂,是一种典型的难降解工业废水,而常规A/A/O工艺生化处理效率不高,严重制约了此类废水的处理和回用.因此,试验进行了粉末活性焦强化A/A/O工艺处理煤气化废水的中试研究,向好氧池投加粉末活性焦形成生物膜-悬浮污泥复合系统,并将剩余污泥回流至系统前段对原水进行预处理.研究结果表明,在活性焦投加量为250 mg·L-1,系统总HRT为105 h的优化条件下,CODCr、氨氮、总氮的去除率分别为97.4%、98.1%和80.5%,出水浓度分别为76 mg·L-1、0.3 mg·L-1和22.4 mg·L-1,达到《循环冷却水用再生水水质标准》(HG/T3923—2007)中CODCr≤80 mg·L-1、NH3-N≤15 mg·L-1、TN≤30 mg·L-1的要求.进一步机理研究表明,向好氧池中投加的粉末活性焦可作为微生物载体和菌胶团核心,投加活性焦后,好氧池的活性污泥浓度增加了57.9%.含焦剩余污泥对原水进行吸附预处理,石油类和SS的去除率分别为34.8%和61.5%,降低了废水对生化系统的毒害作用和冲击负荷,从而提高了系统的整体效率.     

Stability of expanded granular sludge bed process for terylene artificial silk printing and dyeing wastewater treatment

Terylene artificial silk printing and dyeing wastewater(TPD wastewater), containing averaged 710 mg/L terephthalic acid(TA) as the main carbon source and the character pollutant, was subjected to expanded granular sludge bed(EGSB) process. The stability of the EGSB process was firstly conducted by laboratory experiment. TA ionization was the predominated factor influencing the acid-base balance of the system. High concentration of TA in wastewater resulted in sufficient buffering capacity to neutralize the volatile fatty acids(VFA)generated from substrate degradation and provided strong base for anaerobic system to resist the pH decrease below 6.5. VFA and UFA caused almost no inhibition on the anaerobic process and biogas production except that pH was below 6.35 and VFA was at its maximum value. Along with the granulating of the activated sludge, the efficiency of organic removal and production rate of biogas increased gradually and became more stable. After start-up, the efficiency of COD removal increased to 57%—64%, pH stabilized in a range of 7.99—8.04, and production rate of biogas was relatively high and stable. Sludge granulating, suitable influent of pH and loading were responsible for the EGSB stability. The variation of VFA concentration only resulted in neglectable rebound of pH, and the inhibition from VFA could be ignored in EGSB. The EGSB reactor was stable for TPD wastewater treatment.     

Treatment of a dyeing wastewater from a woolen mill using an A/O membrane bio-reactor

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A/O生物法处理石化废水的研究

为了处理水质组成复杂,毒性大、有机物浓度较高的石化废水,采用先厌氧后好氧（即A/O生物法）的处理方法。研究结果表明,石化废水经厌氧处理后,其好氧可生化性提高20％～40％;当厌氧反应器进水有机负荷为5.2kgCOD/m³·d,水力停留时间为24h时,BOD5去除率为85％,COD去除率为83％,油去除率为91.1％;当曝气池污泥负荷为0.45kgCOD/kgMLSS·d,水力停留时间为4h时,BOD₅去除率为94.1％,COD去除率为92.7％,油去除率为96.3％。系统COD总去除率为85％～96％,BOD₅总去除率为95％～99％。A/O生物法为石化废水处理提供了理论依据。     

Performance of bioferric-submerged membrane bioreactor for dyeing wastewater treatment

Adding iron salt or iron hydroxide to sludgemixed liquor in an aeration tank of a conventional activated sludge processes (bioferric process) can simultaneously improve the sludge’s filterability and enhance the system’s treatment capacity. In view of this, Fe(OH)₃ was added to a submerged membrane bioreactor (SMBR) to enhance the removal efficiency and to mitigate membrane fouling. Bioferric process and SMBR were combined to create a novel process called Bioferric-SMBR. A side-by-side comparison study of Bioferric-SMBR and common SMBR dealing with dyeing wastewater was carried out. Bioferric-SMBR showed potential superiority, which could enhance removal efficiency, reduce membrane fouling and improve sludge characteristic. When volumetric loading rate was 25% higher than that of common SMBR, the removal efficiencies of Bioferric-SMBR on COD, dye, and NH₄ ⁺-N were 1.0%, 9.5%, and 5.2% higher than that of common SMBR, respectively. The trans-membrane pressure of Bioferric-SMBR was only 36% of that in common SMBR while its membrane flux was 25% higher than that of common SMBR. The stable running period in Bioferric-SMBR was 2.5 times of that in common SMBR when there was no surplus sludge discharged. The mixed liquor suspended solids concentration of Bioferric-SMBR was higher than that of common SMBR with more diversified kinds of microorganisms such as protozoans and metazoans. The mean particle diameter and specific oxygen uptake rate of Bioferric-SMBR were 3.10 and 1.23 times the common SMBR, respectively. Translated from Environmental Science, 2005, 26(6): 65–70 [译自: 环境科学]     

Treatment of a dyeing wastewater from a woolen mill using an A/O membrane bio-reactor

An anaerobic/oxic membrane bioreactor (A/O MBR) was used for treatment of dyeing wastewater from a woolen mill.COD and color of the wastewater were 54-473 mg/L and 40-400 dilution time (DT) respectively. The ratio of BOD5/COD was less than 0.13. By the A/O MBR process, the average removal of COD, BOD5, color and turbidity was 82％, 96％, 71％ and 99％, respectively. The average COD, BOD5, color and turbidity of effluent was 37 nag/L, 0.8 mg/L, 40 DT and 0.44 NUT respectively. The effluent COD met the local standard of reuse water in Beijing, China. The average COD volume load of the anaerobic biological tank was 0. 0483 kgCOD/(m3·d) and that of the aeration tank of the MBR was 0. 3589 kgCOD/(m3·d). The sludge load of the MBR was 0.19 kgCOD/(kg· MLSS· d) on average and the maximum of that was 0.4 kgCOD/( kg· MLSS· d).The flux of the A/O membrane bioreactor could be remained at larger than 50 L/(h· m2· 0.1MPa). The results indicated that A/O membrane bioreactor has technical feasibility for treatment of woolen mill wastewater.     

Advanced treatment of dyeing wastewater towards reuse by the combined Fenton oxidation and membrane bioreactor process

The performance of combined Fenton oxidation and membrane bioreactor (MBR) process for the advanced treatment of an effluent from an integrated dyeing wastewater treatment plant was evaluated. The experimental results revealed that under the optimum Fenton oxidation conditions (initial pH 5, H 2 O 2 dosage 17 mmol/L, and Fe 2+ 1.7 mmol/L) the average total organic carbon (TOC) and color removal ratios were 39.3% and 69.5% after 35 min of reaction, respectively. Results from Zahn-Wallens Test also represented that Fenton process was effective to enhance the biodegradability of the test wastewater. As for the further purification of MBR process, TOC removal capacity was examined at different hydraulic retention times (HRT) of 10, 18 and 25 hr. Under the optimum HRT of 18 hr, the average TOC concentration and color of the final MBR effluent were 16.8 mg/L and 2 dilution time, respectively. The sludge yield coefficient was 0.13 g MLSS/g TOC and TOC degradation rate was 0.078 kg TOC/(m 3 ·day). The final effluent of MBR can meet the reuse criteria of urban recycling water-water quality standard for miscellaneous water consumption GBT18920-2002.