酸性印染废水的生物处理连续厌氧好氧生物反应系统

1、目 录酸性印染废水的生物处理-连续厌氧好氧生物反应系统1摘要11 概述12 材料和方法22.1 实验室规模的反应器系统，菌种和操作条件22.2 酸性染色废水32.3 分析过程42.4 统计分析53 结论与讨论53.1 在 UASB 反应器中产甲烷率、VFA 和 B.Alk 的变化53.2 UASB/CAST反应器系统的COD去除效率63.3 UASB/CSTR反应堆系统色度去除83.4 在UASB/CSTR序列系统中TAA变化104 结论11致谢11Biological treatment of acid dyeing wastewater using a sequential anaerob

2、ic/aerobic reactor system12Abstract121. Introduction122. Material and methods142.1. Laboratory-scale reactor system, seed and operating conditions142.2. Acid dyeing wastewater152.3. Analytical procedures162.4. Statistical analysis173. Results and discussion183.1. Variations in the methane production

3、 rate, the VFA and the B.Alk. in the UASB reactor183.2. COD removal efficiencies of UASB/CSTR reactor system193.3. Performance of color removal in UASB/CSTR reactor system213.4. Variation of TAA in UASB/CSTR sequential system244. Conclusions24Acknowledgements25References251 概述 dm3 kg-1之间而羊毛洗涤达到dm3 k

4、g-1上流式厌氧污泥床(UASB)，全混合好氧工艺2.1 实验室规模的反应器系统，菌种和操作条件31.7 gdm-3 和 22.4 g VSS dm-3，而CSTR反应器中调节污泥年龄到20天时混合液悬浮固体2.2 酸性染色废水表2.1 酸性染色过程中用到的染料2.3 分析过程aDr¨ager Pac®Ex=A × f/d色度的单位是m-1，A 是分光光度计测出的值，d 是试样长度（单位长度是10mm），f是因素（1000）可溶性COD用回流法测量2.4 统计分析3.1 在 UASB 反应器中产甲烷率、VFA 和 B.Alk 的变化21B.Alk.和 VFA浓度的

5、显著的线性相关关系为(r2 = 0.81, P = 0.07, F = 8.76)。图3.1 在四个操作阶段的甲烷产率、VFA和B.Alk.的浓度变化图3.2 UASB反应器中废水的PH和VFA/B.Alk.比率变化3.2 UASB/CAST反应器系统的COD去除效率在图3可以看出整个系统的COD去除效率。它说明前三个试验的COD去除率在85%到95%之间，而最后一个的去除效率为75%。在第2、3和4阶段将浓度为1000mgdm-3的葡萄糖COD添加到原废水，第1阶段废水中只含有2000mgdm-3葡萄糖COD。阶段1因为只含有葡萄糖COD，出水葡萄糖COD浓度降至低至60mg dm-3，UA

6、SB/CSTR连续系统的总停留时间为2.3天。这个COD值可归因于COD惰性可溶性微生物产品能被厌氧菌自葡萄降解为有机物或完全消耗23。据可溶性微生物产物(SMP) COD通过代谢和腐化降解必须加以考虑，因为出水可溶性COD可能有大多smp(5090%) 23。在下来的试验中，最终COD值高于阶段1的COD值因为原污水含有大量的惰性COD。在第四个阶段中，系统出水COD已降至约257±27mgdm-3因为原废水含有200mgdm-3的惰性COD(见图3.4)。厌氧系统可以去除所有可溶性COD中所有可降解的COD和部分惰性COD。在阶段4中，UASB及UASB/CSTR系统COD去除率

7、分别从84%和94%下降到51%和83%。可以认为在厌氧/好氧序列反应堆系统中不同的惰性COD的比例，缓慢的、易降解的有机物质，有机酸和芳香胺的比例酸性印染废水是造成去除除效率的变化的原因。试验表明UASB反应和整体(UASB/CSTR)反应器系统的COD 去除率并无显著差异图3.4 在试验4中原废水的惰性COD的测定3.3 UASB/CSTR反应堆系统色度去除图3.5 49天操作中系统的色度去除效率上述情况，研究有关用实验室规模的厌氧/好氧半连续活性污泥(SCAS)的反应堆系统处理地毯印染工厂的纺织废水得出类似结果4。在上述系统在总停留时间为1-2 天，出水COD和色度从6000mgdm-3

8、和0.8吸光度单位下降为79-219mgdm-30和吸光度单位(在波长 500nm)。在一个染料制造工厂， COD浓度为1200mgdm-3、色度为500倍(稀释因子) 的污水在UASB反应(4.5L)和活性污泥罐(5L)的系统中处理，COD和色度的去除率超过83%和90%，在厌氧和好氧阶段中的停留时间分别为6-10小时和6.5小时。图3.6显示第四阶段UASB/CSTR系统处理酸性印染废水的吸光度在不同波长的测得的值。进水在可见光波长为500和620nm测得有两个波峰。在厌氧处理阶段，波峰出现在紫外区的波长为360纳米， 表明偶氮键断开，从而提供染料退色的证据。CSTR反应器污水样品显示最大

9、吸收光谱在低波长(325nm)由于厌氧条件下生产的芳香胺在好氧条件被去除。这表明，父母染料在UASB反应转为其他中间有机形式， 然后，这些中间体在CSTR反应器中除解。图3.6 在第四阶段反应器的进水和出水在不同波长下的吸光度图3.7 CSTR反应器中TAA的去除效率3.4 在UASB/CSTR序列系统中TAA变化NigdeBiological treatment of acid dyeing wastewater using a sequential anaerobic/aerobic reactor systemMustafa Is¸ka, Delia Teresa Sponza

10、 ba Nigde University, Aksaray Engineering Faculty, Environmental Engineering Department, 68100 Aksaray, Turkeyb Dokuz Eylul University, Engineering Faculty, Environmental Engineering Department, Buca Kaynaklar Campus, 35160 Izmir, TurkeyReceived 16 March 2004; received in revised form 25 April 2005;

11、 accepted 22 May 2005AbstractThe treatment of the wastewater taken from a wool dyeing processing in a wool manufacturing plant was investigated using an anaerobic/aerobic sequential system. The process units consisted of an anaerobic UASB reactor and an aerobic CSTR reactor. Glucose, alkalinity and

12、azo dyes were added to the raw acid dyeing wastewater in order to simulate the dye industry wastewater since the raw wastewater contained low levels of carbon, NaHCO3 and color through anaerobic/aerobic sequential treatment. The UASB reactor gave COD and color removals of 5184% and 8196%, respective

13、ly, at a HRT of 17 h. The COD and color removal efficiencies of the UASB/CSTR sequential reactor system were 9783% and 8780%, respectively, at a hydraulic retention time (HRTs) of 3.3 days. The aromatic amines (TAA) formed in the anaerobic stage were effectively removed in the aerobic stage. Keyword

14、s: Acid wool dyeing; Azo dyes; Sequential; Biological treatment1 2 13456714sludge blanket reactor (UASB)/aerobic continuous stirred tankreactor (CSTR) system.a Glucose, alkalinity and dyes were added to feed in order to simulate the acid dyeing wastewater since the raw wastewater contained low level

15、 of carbon (COD), NaHCO3 and color. COD is required for the reductive conditions through the cleavage of azo bonds under anaerobic conditions. The values given in second colon represent the data measured through the experiments.2.1. Laboratory-scale reactor system, seed and operating conditionsTable

16、 12.2. Acid dyeing wastewater6,13,14Table 11Table 1Table 2 Table2 The dyes used through acid dyeing in operation period2.3. Analytical procedures1516 =A × f/dwhere is the color in m1 unit (m1 = A/10mm×1000), A the measured absorbance value from spectrophotometer, d the sample length (cell

17、width,10 mm) and f is a factor (1000).1718 191720 202.4. Statistical analysis3.1. Variations in the methane production rate, the VFA and the B.Alk. in the UASB reactor Fig. 1 Fig. 221 22 A significant linear correlation between B.Alk. and VFA concentration was observed (r2 = 0.81, P = 0.07, F = 8.76

18、).Fig. 1. Variation in methane production rate, VFA and B.Alk. concentrations infour operation runs.Fig. 2. Variation of pH and VFA/B.Alk. ratios in the effluent of UASB reactor.3.2. COD removal efficiencies of UASB/CSTR reactor systemFig. 32323Fig. 3. The COD removal performance of the UASB/CSTR se

19、quential system.Fig. 4. Determination of inert COD in raw wastewater through Run 4.Fig. 43.3. Performance of color removal in UASB/CSTR reactor systemFig. 5Fig. 5Fig. 5. Color removal efficiencies of the system through the operation of 49 days.4 9Fig. 6 sample from the CSTR reactor exhibited maximum

20、 absorbance spectra at low wavelengths (325 nm) due to aromatic amines produced under anaerobic conditions was removed under aerobic conditions. This shows that the parent dye was converted to other intermediate organic forms in UASB reactor, and then these intermediates were degraded in the CSTR re

21、actor.Fig. 6. Absorbance spectra in influents and effluents of the reactor system at different wavelengths in Run 4.Fig. 7. TAA removal efficiencies in CSTR reactor.ANOVA test indicated that there were no significant differences between color removal efficiencies between UASB reactor and whole (UASB

22、/CSTR) system through operation days (p = 0.05, F = 0.23, d.f. = 3).3.4. Variation of TAA in UASB/CSTR sequential systemFig. 7Fig. 724,254. ConclusionsThe treatment of real textile wastewater has been carried out using aerobic biological processes, physico/chemical processes and their modifications.

23、 The addition of an anaerobic stage prior to the aerobic stage could be favorable in the treatment of the acid dyeing wastewaters since anaerobic stage can degrade the azo dyes resulting in decolorization of textile wastewater and reduce the organic loading rate on aerobic stage. The reducing enviro

24、nment prevailing in the UASB reactor by the electrons releasing from the azo dyes and its intermetabolite products (TAA) provide the color removal. The UASB/CSTR combined rector system showed a stable performance for the treatment of acid dyeing wastewater. Therefore, this system would have a potent

25、ial to meet the effluent discharge limitations of the receiving medium for the acid dyeingwastewaters on the basis of COD, BOD and color removal, although color removal has no limitations yet in the Turkish receiving water discharge standards.AcknowledgementsThis study was supported by the Turkish S

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