生化/芬顿试剂氧化组合工艺处理印染废水试验研究
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摘要
印染废水具有污染物浓度高、色度大、成分复杂和水质水量多变等特点,是一种较难处理的有机工业废水。为此在实验室中进行水解酸化—好氧生物接触氧化—Fenton试剂氧化法处理印染废水试验研究,通过分析处理过程中的COD、色度等污染指标的去除效果和变化规律,检验该工艺的处理效果,得出该工艺的设计和控制参数。
首先,进行水解酸化—好氧生物接触氧化法处理印染废水试验研究。试验装置前段设置水解酸化单元,目的在于提高废水可生化性和去除色度,从而为后续处理创造有利条件。后续为两级生物接触氧化单元,主要起去除COD、BOD5的作用。
分别以活性艳蓝KN-R染料废水和活性艳红K-2BP、活性艳橙X-GN、直接大红4BS配置的混合染料废水为原水进行了水解酸化—生物接触氧化反应器的挂膜启动,运行结果表明,用该工艺分别处理活性艳蓝KN-R染料废水和混合染料废水,系统运行稳定,得到了很好的处理效果,出水水质前者达到《纺织染整工业水污染物排放标准(GB4287-92)》中的一级标准,后者达到二级标准。
通过正交试验对影响水解酸化-生物接触氧化反应器运行效果的因素如进水流量(水力停留时间)、一级生物接触氧化柱气水比和二级生物接触氧化柱气水比进行了影响分析,正交试验结果表明,影响废水处理效果的因素主次顺序为：进水流量(水力停留时间)>一级生物接触氧化柱气水比>二级生物接触氧化柱气水比。以COD去除率和色度的去除率为评价指标,采用综合评分法中的指标叠加法,将多指标问题转化为单指标问题,得出了反应器处理活性艳蓝KN-R染料废水的最佳运行条件：进水流量10L/h(反应器总的水力停留时间30h),一级生物接触氧化柱气水比8：1,二级生物接触氧化柱气水比7.2：1。反应器处理混合染料废水的最佳运行条件：进水流量5L/h(反应器总的水力停留时间60h),一级生物接触氧化柱气水比为11：1,二级生物接触氧化柱的气水比为9：1。
进行了水解酸化—生物接触氧化—芬顿试剂氧化工艺处理偶氮胭脂红G废水试验研究,结果表明该工艺处理偶氮胭脂红G废水是可行的。当进水COD为724.6mg/L,色度为300倍时,出水COD小于50mg/L,色度小于30倍,不但达到国家标准《纺织染整工业水污染物排放标准(GB4287—92)》中的一级标准,而且达到要求更高的江苏省地方标准《太湖地区城镇污水处理厂及重点工业行业主要水污染物排放限值(DB32/T1072—-2007)》以及山东省地方标准《山东省纺织染整工业水污染物排放标准(DB37/533—2005)》。
根据莫诺(Monod)方程,在假设水解酸化—生物接触氧化处理偶氮胭脂红G废水系统中单个反应池是一个完全混合的稳态反应器的条件下,推导了该系统中单个反应池生化反应的动力学方程,通过试验测定和线性回归方程确定了动力学方程中的相关参数,得到水解酸化池生化反应的动力学方程为v=0.3096(Le-0.4238)(d-1),一级生物接触氧化池生化反应的动力学方程为v=0.4532(Le-0.0647)(d-1),二级生物接触氧化池生化反应的动力学方程为v=0.2882(Le-0.0647)(d-1)。
在温度保持不变的条件下,Fenton氧化降解偶氮胭脂红G的反应影响因素主要有：初始pH值、染料初始浓度、亚铁离子初始浓度以及过氧化氢初始浓度。在反应初始pH值保持不变的条件下,根据化学反应动力学原理,建立了Fenton氧化降解偶氮胭脂红G的动力学模型,通过试验测定Fenton氧化反应过程中各时间段的染料浓度,计算出动力学模型中的参数,从而得到Fenton氧化降解偶氮胭脂红G的动力学方程为v=-dC/dt=0.0228C0.9050R0.5150S0.3478(mg L-1min-1)。
Printing and dyeing wastewater contained high concentration of pollutant, high chromaticity and complex component. And its quality and quantity changes frequently. So it is a kind of organic industrial wastewater which is difficult to treat. In this paper, hydrolytic acidification-biological contact oxidation-Fenton's reagent oxidation processes were used to treat printing and dyeing wastewater in the laboratory. The effective design and control parameters of the processes were found out by analyzing the removal efficencies, variation of COD and chromaticity in the processes.
Firstly, the experiment on hydrolytic acidification-biological contact oxidation processes to treat printing and dyeing wastewater was carried out. Hydrolytic acidification cell in the first part was used to improve biodegradability of the wastewater and reduces chromaticity, which was benefical for subsequent treatment. Two subsequent biological contact oxidation stages was aimed mainly to reduce COD and BOD5.
Hydrolytic acidification-biological contact oxidation processes were started up to treat two kinds of printing and dyeing wastewater, i.e. reactive brilliant blue KN-R dye wastewater and mixed dyes wastewater which contained reactive brilliant red K-2BP, reactive brilliant orange X-GN and direct scarlet4BS. The results showed that the system run well, and the effluent qualities respectively meet standard I and standard Ⅱ of 《Discharge standard of water pollutants for dyeing and finishing of textile industry(GB4287-92)》
By orthogonal tests the impacts of reactor effect factors such as influent flow (hydraulic retention time), gas water ratio of the first and the secondary bio-contact oxidation column were analyzed. The final results showed that influent flow is the most prominent effect factor, followed by gas water ratio of the first bio-contact oxidation column and gas water ratio of the secondary bio-contact oxidation column.
Selecting the removal rate of COD and color as evaluation indexes, multi-index problem was transformed into a single index problem by the index overlay method. The best operation conditions of the reactor to treat reactive brilliant blue KN-R dye wastewater were obtained, which are:influent flow=10L/h (hydraulic retention time =30h), gas water ratio of the first bio-contact oxidation column=8:1, and gas water ratio of the secondary bio-contact oxidation column=7.2:1. The best operation conditions of the reactor to treat mixed dyes wastewater are:influent flow=5L/h (hydraulic retention time=60h), gas water ratio of the first bio-contact oxidation column=11:1. gas water ratio of the secondary bio-contact oxidation column=9:1.
Secondly, the experiment on hydrolytic acidification-biological contact oxidation-Fenton's reagent oxidation processes to treat azocarmine G wastewater was carried out. The results showed it was a feasible process for treating azocarmine G wastewater, with effluent COD and chromaticity of less than50mg/L and30, respectively. The effluent qualities not only meet standard I of 《Discharge standard of water pollutants for dyeing and finishing of textile industry(GB4287-92)》, but also meet two more stringent local discharge standard of water pollutants for dyeing and finishing of textile industry standards of Jiangsu Province and Shandong Province.
According to the Monod equation, when the single reaction cell in the hydrolytic acidification-biological contact oxidation processes to treat azocarmine G waste water was assumed as a completely mixed steady-state reactor, its kinetic equation was derived and the relevant parameters of the equation were determined by experimental measurements and linear regression equations. The kinetic equation of biochemical reaction in the hydrolytic acidification cell was v=0.3096(Le-0.4238)(d-1). The kinetic equation of biochemical reaction in the first biological contact oxidation cell was v=0.4532(Le-0.0647)(d-1). The kinetic equation of biochemical reaction in the secondary biological contact oxidation cell was v=0.2882(Le-0.0647)(d-1).
When temperature remained unchanged, the influencing factors of Fenton oxidative degradation of azocarmine G are:initial pH, initial dye concentration, initial concentration of ferrous ions and initial concentration of hydrogen peroxide. When initial pH remained unchanged, the apparent kinetic model of Fenton oxidative degradation of azocarmine G was derived. Then the parameters of the model were calculated by measuring the dye concentrations in different time when the reaction of Fenton oxidative degradation of azocarmine G was conducted. The kinetic equation of reaction of Fenton oxidative degradation of azocarmine G was v=-dC/dt=0.0228C0.9050R0.5150S0.3478(mg L-1min-1)。
首先,进行水解酸化—好氧生物接触氧化法处理印染废水试验研究。试验装置前段设置水解酸化单元,目的在于提高废水可生化性和去除色度,从而为后续处理创造有利条件。后续为两级生物接触氧化单元,主要起去除COD、BOD5的作用。
分别以活性艳蓝KN-R染料废水和活性艳红K-2BP、活性艳橙X-GN、直接大红4BS配置的混合染料废水为原水进行了水解酸化—生物接触氧化反应器的挂膜启动,运行结果表明,用该工艺分别处理活性艳蓝KN-R染料废水和混合染料废水,系统运行稳定,得到了很好的处理效果,出水水质前者达到《纺织染整工业水污染物排放标准(GB4287-92)》中的一级标准,后者达到二级标准。
通过正交试验对影响水解酸化-生物接触氧化反应器运行效果的因素如进水流量(水力停留时间)、一级生物接触氧化柱气水比和二级生物接触氧化柱气水比进行了影响分析,正交试验结果表明,影响废水处理效果的因素主次顺序为：进水流量(水力停留时间)>一级生物接触氧化柱气水比>二级生物接触氧化柱气水比。以COD去除率和色度的去除率为评价指标,采用综合评分法中的指标叠加法,将多指标问题转化为单指标问题,得出了反应器处理活性艳蓝KN-R染料废水的最佳运行条件：进水流量10L/h(反应器总的水力停留时间30h),一级生物接触氧化柱气水比8：1,二级生物接触氧化柱气水比7.2：1。反应器处理混合染料废水的最佳运行条件：进水流量5L/h(反应器总的水力停留时间60h),一级生物接触氧化柱气水比为11：1,二级生物接触氧化柱的气水比为9：1。
进行了水解酸化—生物接触氧化—芬顿试剂氧化工艺处理偶氮胭脂红G废水试验研究,结果表明该工艺处理偶氮胭脂红G废水是可行的。当进水COD为724.6mg/L,色度为300倍时,出水COD小于50mg/L,色度小于30倍,不但达到国家标准《纺织染整工业水污染物排放标准(GB4287—92)》中的一级标准,而且达到要求更高的江苏省地方标准《太湖地区城镇污水处理厂及重点工业行业主要水污染物排放限值(DB32/T1072—-2007)》以及山东省地方标准《山东省纺织染整工业水污染物排放标准(DB37/533—2005)》。
根据莫诺(Monod)方程,在假设水解酸化—生物接触氧化处理偶氮胭脂红G废水系统中单个反应池是一个完全混合的稳态反应器的条件下,推导了该系统中单个反应池生化反应的动力学方程,通过试验测定和线性回归方程确定了动力学方程中的相关参数,得到水解酸化池生化反应的动力学方程为v=0.3096(Le-0.4238)(d-1),一级生物接触氧化池生化反应的动力学方程为v=0.4532(Le-0.0647)(d-1),二级生物接触氧化池生化反应的动力学方程为v=0.2882(Le-0.0647)(d-1)。
在温度保持不变的条件下,Fenton氧化降解偶氮胭脂红G的反应影响因素主要有：初始pH值、染料初始浓度、亚铁离子初始浓度以及过氧化氢初始浓度。在反应初始pH值保持不变的条件下,根据化学反应动力学原理,建立了Fenton氧化降解偶氮胭脂红G的动力学模型,通过试验测定Fenton氧化反应过程中各时间段的染料浓度,计算出动力学模型中的参数,从而得到Fenton氧化降解偶氮胭脂红G的动力学方程为v=-dC/dt=0.0228C0.9050R0.5150S0.3478(mg L-1min-1)。
Printing and dyeing wastewater contained high concentration of pollutant, high chromaticity and complex component. And its quality and quantity changes frequently. So it is a kind of organic industrial wastewater which is difficult to treat. In this paper, hydrolytic acidification-biological contact oxidation-Fenton's reagent oxidation processes were used to treat printing and dyeing wastewater in the laboratory. The effective design and control parameters of the processes were found out by analyzing the removal efficencies, variation of COD and chromaticity in the processes.
Firstly, the experiment on hydrolytic acidification-biological contact oxidation processes to treat printing and dyeing wastewater was carried out. Hydrolytic acidification cell in the first part was used to improve biodegradability of the wastewater and reduces chromaticity, which was benefical for subsequent treatment. Two subsequent biological contact oxidation stages was aimed mainly to reduce COD and BOD5.
Hydrolytic acidification-biological contact oxidation processes were started up to treat two kinds of printing and dyeing wastewater, i.e. reactive brilliant blue KN-R dye wastewater and mixed dyes wastewater which contained reactive brilliant red K-2BP, reactive brilliant orange X-GN and direct scarlet4BS. The results showed that the system run well, and the effluent qualities respectively meet standard I and standard Ⅱ of 《Discharge standard of water pollutants for dyeing and finishing of textile industry(GB4287-92)》
By orthogonal tests the impacts of reactor effect factors such as influent flow (hydraulic retention time), gas water ratio of the first and the secondary bio-contact oxidation column were analyzed. The final results showed that influent flow is the most prominent effect factor, followed by gas water ratio of the first bio-contact oxidation column and gas water ratio of the secondary bio-contact oxidation column.
Selecting the removal rate of COD and color as evaluation indexes, multi-index problem was transformed into a single index problem by the index overlay method. The best operation conditions of the reactor to treat reactive brilliant blue KN-R dye wastewater were obtained, which are:influent flow=10L/h (hydraulic retention time =30h), gas water ratio of the first bio-contact oxidation column=8:1, and gas water ratio of the secondary bio-contact oxidation column=7.2:1. The best operation conditions of the reactor to treat mixed dyes wastewater are:influent flow=5L/h (hydraulic retention time=60h), gas water ratio of the first bio-contact oxidation column=11:1. gas water ratio of the secondary bio-contact oxidation column=9:1.
Secondly, the experiment on hydrolytic acidification-biological contact oxidation-Fenton's reagent oxidation processes to treat azocarmine G wastewater was carried out. The results showed it was a feasible process for treating azocarmine G wastewater, with effluent COD and chromaticity of less than50mg/L and30, respectively. The effluent qualities not only meet standard I of 《Discharge standard of water pollutants for dyeing and finishing of textile industry(GB4287-92)》, but also meet two more stringent local discharge standard of water pollutants for dyeing and finishing of textile industry standards of Jiangsu Province and Shandong Province.
According to the Monod equation, when the single reaction cell in the hydrolytic acidification-biological contact oxidation processes to treat azocarmine G waste water was assumed as a completely mixed steady-state reactor, its kinetic equation was derived and the relevant parameters of the equation were determined by experimental measurements and linear regression equations. The kinetic equation of biochemical reaction in the hydrolytic acidification cell was v=0.3096(Le-0.4238)(d-1). The kinetic equation of biochemical reaction in the first biological contact oxidation cell was v=0.4532(Le-0.0647)(d-1). The kinetic equation of biochemical reaction in the secondary biological contact oxidation cell was v=0.2882(Le-0.0647)(d-1).
When temperature remained unchanged, the influencing factors of Fenton oxidative degradation of azocarmine G are:initial pH, initial dye concentration, initial concentration of ferrous ions and initial concentration of hydrogen peroxide. When initial pH remained unchanged, the apparent kinetic model of Fenton oxidative degradation of azocarmine G was derived. Then the parameters of the model were calculated by measuring the dye concentrations in different time when the reaction of Fenton oxidative degradation of azocarmine G was conducted. The kinetic equation of reaction of Fenton oxidative degradation of azocarmine G was v=-dC/dt=0.0228C0.9050R0.5150S0.3478(mg L-1min-1)。
引文
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