超滤膜净化滦河水运行工艺与净化效果的研究
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摘要
随着人类文明的进步、人口的增加以及工农业的快速发展,饮用水的水质问题变得越来越突出。一方面,饮用水水源的水质日益恶化,同时用户也对饮用水水质提出了更高要求,另一方面,水资源在时间和空间上分布不均。两方面都促进水处理技术的不断发展和水质标准的提高。随着新的《生活饮用水卫生标准》(GB5749-2006)的颁布,我国对饮用水水质要求变高,而传统的水处理工艺在一定程度上不能达到新标准要求。为了满足这一新的水质标准要求,需要探讨传统处理工艺的改造以及新技术的应用。
超滤作为一种新的水处理技术,由于膜污染问题和对我国现有各种水体的适应性没有完全被了解,所以在我国还没有大规模的应用于自来水厂。为了考察超滤技术结合水厂现有工艺处理滦河水时产水的水质保障、经济性以及可靠性,本试验采用超滤膜结合水厂混凝、沉淀和砂滤工艺处理滦河水。实验为期一年,经历了高温高藻期、正常水质期和低温低浊期,系统研究了混凝—沉淀—超滤膜和混凝—沉淀—砂滤—超滤膜两种组合工艺在不同水质时期的运行工况,超滤膜进出水的常规和非常规指标的检测,膜进出水、反洗水的分子量分布、消毒副产物及其前体物的分布及浓度,超滤膜运行成本,运行稳定性等。通过研究得出,在水厂现有构筑物能够得到充分利用的同时,有效地保证出水水质,并且抗水质冲击能力较强,相关参数如下：
第一组工艺在不同水质时期优化后的运行参数：在高温高藻期,通量60L/h.m2,过滤时间30 mmin,反洗加氯2 mg/L；在正常水质期,通量为50 L/h·m2,过滤时间30 mmin,预氯化浓度为1.2 mg/L,对于缓解SF衰减来说,在反应池中投加助凝剂HCA的效果好于未投加助凝剂,而投加助凝剂水玻璃的效果劣于未投加助凝剂；在低温低浊期,通量为50 L/h·m2,过滤时间30 mmin,预氯化浓度2 mg/L。第二组工艺：低温低浊水质期和正常水质期的运行参数：通量60 L/h·m2,过滤时间30 mmin,预氯化浓度1 mg/L；高温高藻期,通量75 L/h·m2,过滤时间20 mmin,预氯化加CEB的运行方式,预氯化浓度0.5 mg/L,CEB时间0.5 h,CEB周期24 h,CEB药品NaClO。
第一组工艺的膜出水水质指标中CODMn和UV254的平均值高于第二组工艺中出水相应指标,而浊度则相反,浊度值均低于1 NTU。在两种工艺中,处理沉淀池出水时,除膜出水的菌落总数和大肠菌群数有超标情况出现外,其余各种指标均优于《生活饮用水卫生标准》(GB5749-2006)要求。超滤膜进出水中溶解性有机物(DOM)主要由小分子量DOM构成,且这部分有机物对UV254、三卤甲烷生成潜能(THMFP)和卤乙酸生成潜能(HAAFP)贡献最大。
第一组工艺中,超滤膜的过滤时间越长,在初始阶段跨膜压差(TMP)增长得越快,达到稳定运行的时间越短,反洗跨膜压差(BTMP)达到稳定衰减的时间越长,且BTMP越小。随着过滤时间的延长,’反洗水的浊度、CODMn、UV254和THMFP值逐渐增大,但过滤时间对THMFP、UV254的影响较小。反洗水中DOM主要由分子量大于30 kDa和小于1 kDa两部分DOM组成,而UV254主要由分子量小于1 kDa的DOM构成。反洗水中碎片的分形维数与过滤时间具有较好的相关性。第二组工艺中反洗水的CODMn受温度影响较大,随温度升高变大,而浊度和UV254几乎不受温度的影响。
超滤膜处理砂滤池出时,超滤膜的产水率、单位产水电耗都优于处理沉淀池出水时相对应的数值,而单位产水药耗则相反。
With the progress of human civilization, population growth and rapid development of industry and agriculture, the issue of drinking water quality becomes more prominent. On one hand, drinking water quality of source water is deteriorating and users share higher requirements for drinking water; on the other hand, water resources distribute uneven in time and space. Both sides stimulate the development of the water treatment technology and the improvement of water quality standards. In China, with the promulgation of the new standards for drinking water quality (GB5749-2006), the demand for water quality becomes higher, and therefore, to some extent, the traditional water treatment process cannot meet the demand of the drinking water quality standards. In order to meet the standards, it is necessary to probe into the improvement of traditional process and the application of new technology.
Ultrafiltration as an emerging water treatment technology has not yet been widely applied to waterworks because of membrane fouling and insufficient knowledge of the adaptability of ultrafiltration membrane to various waters in China. In order to detect whether or not the combination of ultrafiltration technology with the existing process in waterworks can guarantee membrane treated water quality and the economy, reliability of the process in treating Luan River, the experiment introduced ultrafiltration membrane to the existing coagulation, sendimentation and sand filter process in waterworks. Experiments lasted one year and experienced three water quality periods, namely, high temperature and algae period, normal water quality period & low temperature and turbidity period. The operating conditions of coagulation—sendimentation—ultrafiltration membrane and coagulation—sendimentation—sand filter—ultrafiltration membrane processes in different water quality periods were systematically studied. The research was on regular indices and non-regular indices in membrane feed water and treated water, the molecular weight distribution of membrane feed water, treated water and membrane backwash water, distribution and concentration of disinfection by-products and their precursors, membrane running cost, operation stability and so on. The conclusions were made based on the research:the existing buildings of waterworks could be fully utilized, and simultaneously the membrane treated water quality was effectively guaranteed and the ability to resist the change of water quality load was stronger, the related parameters were as follows:
The optimized operating parameters of the first process during different water periods were as follows. In the high temperature and algae period, the flux was 60 L/h-m2·mH2O, filtration time 30 min, and backwash chlorination 2 mg/L. At the normal water quality period, the flux was 50 L/h-m2·mH2O, filtration time 30 min and prechlorination concentration 1.2 mg/L. As for alleviating membrane fouling, the effect of adding coagulant aid HCA to reaction tank was better than without adding and the effect of addition of sodium silicate was worse than without adding. At low temperature and turbidity period, the flux was 50 L/h·m2·mH2O, filtration time 30 min, prechlorination concentration 2 mg/L and the chemical NaClO. For the second process, the operating parameters were as follows:at low temperature and turbidity period and normal water quality period, the operating parameters were exhibited, Flux was 60 L/h·m2·mH2O, filtration time 30 min and prechlorination concentration 1 mg/L. During high temperature and algae period, the flux was 75 L/h·m2·mH2O, filtration time 20 min, the operation modes were prechlorination and CEB, the CEB time 0.5 h and the CEB cycle 24 h; the CEB chemical was NaClO and prechlorination concentration was 0.5mg/L.
As for the water quality indices of membrane treated water in the first process, CODMn and UV254 were higher than that in the second process, but turbidity was contrary. Turbidity values were all smaller than 1 NTU. Except that some of the total bacterial colony number and total coliforms exceeded standards for the first process, other indicators were all better than the demand of the standards. The dissolved organic matter (DOM) in treated water of ultrafiltration membrane was mainly small molecular weight DOM, similarly, this part DOM contributed the greatest contribution to UV254, trihalomethane formation potential (THMFP) and haloacetic acids formation potential (HAAFP).
The longer the filtration time was, the faster TMP increased at the beginning, the shorter the filtration time it took to reach stabilization, the longer it took for backwash transmembrane pressure (BTMP) to reach a steady decay, and BTMP was smaller. With the extension of the filtration time, the values of turbidity, CODMn, UV254 and THMFP in backwash water increased, but the change of time had little effect on THMFP and UV254. Most of the DOM in MBW distributed in more than 30 kDa and less than 1 kDa, but for UV254, it was mainly distributed in the range of less than 1 kDa. The fractal dimension of flakes in MBW had a good linear relationship with filtration time. Temperature greatly affected the CODMn in backwash water of the second combined process. The increase of temperature led to increased CODMn value, but it had a little influence on turbidity and UV254 in MBW.
The membrane water productivity, power consumption for specific water production of the process when treating the sand filter were better than that of the process treating sedimentation tank produced water, but it was contrary with power consumption for specific water production.
超滤作为一种新的水处理技术,由于膜污染问题和对我国现有各种水体的适应性没有完全被了解,所以在我国还没有大规模的应用于自来水厂。为了考察超滤技术结合水厂现有工艺处理滦河水时产水的水质保障、经济性以及可靠性,本试验采用超滤膜结合水厂混凝、沉淀和砂滤工艺处理滦河水。实验为期一年,经历了高温高藻期、正常水质期和低温低浊期,系统研究了混凝—沉淀—超滤膜和混凝—沉淀—砂滤—超滤膜两种组合工艺在不同水质时期的运行工况,超滤膜进出水的常规和非常规指标的检测,膜进出水、反洗水的分子量分布、消毒副产物及其前体物的分布及浓度,超滤膜运行成本,运行稳定性等。通过研究得出,在水厂现有构筑物能够得到充分利用的同时,有效地保证出水水质,并且抗水质冲击能力较强,相关参数如下：
第一组工艺在不同水质时期优化后的运行参数：在高温高藻期,通量60L/h.m2,过滤时间30 mmin,反洗加氯2 mg/L；在正常水质期,通量为50 L/h·m2,过滤时间30 mmin,预氯化浓度为1.2 mg/L,对于缓解SF衰减来说,在反应池中投加助凝剂HCA的效果好于未投加助凝剂,而投加助凝剂水玻璃的效果劣于未投加助凝剂；在低温低浊期,通量为50 L/h·m2,过滤时间30 mmin,预氯化浓度2 mg/L。第二组工艺：低温低浊水质期和正常水质期的运行参数：通量60 L/h·m2,过滤时间30 mmin,预氯化浓度1 mg/L；高温高藻期,通量75 L/h·m2,过滤时间20 mmin,预氯化加CEB的运行方式,预氯化浓度0.5 mg/L,CEB时间0.5 h,CEB周期24 h,CEB药品NaClO。
第一组工艺的膜出水水质指标中CODMn和UV254的平均值高于第二组工艺中出水相应指标,而浊度则相反,浊度值均低于1 NTU。在两种工艺中,处理沉淀池出水时,除膜出水的菌落总数和大肠菌群数有超标情况出现外,其余各种指标均优于《生活饮用水卫生标准》(GB5749-2006)要求。超滤膜进出水中溶解性有机物(DOM)主要由小分子量DOM构成,且这部分有机物对UV254、三卤甲烷生成潜能(THMFP)和卤乙酸生成潜能(HAAFP)贡献最大。
第一组工艺中,超滤膜的过滤时间越长,在初始阶段跨膜压差(TMP)增长得越快,达到稳定运行的时间越短,反洗跨膜压差(BTMP)达到稳定衰减的时间越长,且BTMP越小。随着过滤时间的延长,’反洗水的浊度、CODMn、UV254和THMFP值逐渐增大,但过滤时间对THMFP、UV254的影响较小。反洗水中DOM主要由分子量大于30 kDa和小于1 kDa两部分DOM组成,而UV254主要由分子量小于1 kDa的DOM构成。反洗水中碎片的分形维数与过滤时间具有较好的相关性。第二组工艺中反洗水的CODMn受温度影响较大,随温度升高变大,而浊度和UV254几乎不受温度的影响。
超滤膜处理砂滤池出时,超滤膜的产水率、单位产水电耗都优于处理沉淀池出水时相对应的数值,而单位产水药耗则相反。
With the progress of human civilization, population growth and rapid development of industry and agriculture, the issue of drinking water quality becomes more prominent. On one hand, drinking water quality of source water is deteriorating and users share higher requirements for drinking water; on the other hand, water resources distribute uneven in time and space. Both sides stimulate the development of the water treatment technology and the improvement of water quality standards. In China, with the promulgation of the new standards for drinking water quality (GB5749-2006), the demand for water quality becomes higher, and therefore, to some extent, the traditional water treatment process cannot meet the demand of the drinking water quality standards. In order to meet the standards, it is necessary to probe into the improvement of traditional process and the application of new technology.
Ultrafiltration as an emerging water treatment technology has not yet been widely applied to waterworks because of membrane fouling and insufficient knowledge of the adaptability of ultrafiltration membrane to various waters in China. In order to detect whether or not the combination of ultrafiltration technology with the existing process in waterworks can guarantee membrane treated water quality and the economy, reliability of the process in treating Luan River, the experiment introduced ultrafiltration membrane to the existing coagulation, sendimentation and sand filter process in waterworks. Experiments lasted one year and experienced three water quality periods, namely, high temperature and algae period, normal water quality period & low temperature and turbidity period. The operating conditions of coagulation—sendimentation—ultrafiltration membrane and coagulation—sendimentation—sand filter—ultrafiltration membrane processes in different water quality periods were systematically studied. The research was on regular indices and non-regular indices in membrane feed water and treated water, the molecular weight distribution of membrane feed water, treated water and membrane backwash water, distribution and concentration of disinfection by-products and their precursors, membrane running cost, operation stability and so on. The conclusions were made based on the research:the existing buildings of waterworks could be fully utilized, and simultaneously the membrane treated water quality was effectively guaranteed and the ability to resist the change of water quality load was stronger, the related parameters were as follows:
The optimized operating parameters of the first process during different water periods were as follows. In the high temperature and algae period, the flux was 60 L/h-m2·mH2O, filtration time 30 min, and backwash chlorination 2 mg/L. At the normal water quality period, the flux was 50 L/h-m2·mH2O, filtration time 30 min and prechlorination concentration 1.2 mg/L. As for alleviating membrane fouling, the effect of adding coagulant aid HCA to reaction tank was better than without adding and the effect of addition of sodium silicate was worse than without adding. At low temperature and turbidity period, the flux was 50 L/h·m2·mH2O, filtration time 30 min, prechlorination concentration 2 mg/L and the chemical NaClO. For the second process, the operating parameters were as follows:at low temperature and turbidity period and normal water quality period, the operating parameters were exhibited, Flux was 60 L/h·m2·mH2O, filtration time 30 min and prechlorination concentration 1 mg/L. During high temperature and algae period, the flux was 75 L/h·m2·mH2O, filtration time 20 min, the operation modes were prechlorination and CEB, the CEB time 0.5 h and the CEB cycle 24 h; the CEB chemical was NaClO and prechlorination concentration was 0.5mg/L.
As for the water quality indices of membrane treated water in the first process, CODMn and UV254 were higher than that in the second process, but turbidity was contrary. Turbidity values were all smaller than 1 NTU. Except that some of the total bacterial colony number and total coliforms exceeded standards for the first process, other indicators were all better than the demand of the standards. The dissolved organic matter (DOM) in treated water of ultrafiltration membrane was mainly small molecular weight DOM, similarly, this part DOM contributed the greatest contribution to UV254, trihalomethane formation potential (THMFP) and haloacetic acids formation potential (HAAFP).
The longer the filtration time was, the faster TMP increased at the beginning, the shorter the filtration time it took to reach stabilization, the longer it took for backwash transmembrane pressure (BTMP) to reach a steady decay, and BTMP was smaller. With the extension of the filtration time, the values of turbidity, CODMn, UV254 and THMFP in backwash water increased, but the change of time had little effect on THMFP and UV254. Most of the DOM in MBW distributed in more than 30 kDa and less than 1 kDa, but for UV254, it was mainly distributed in the range of less than 1 kDa. The fractal dimension of flakes in MBW had a good linear relationship with filtration time. Temperature greatly affected the CODMn in backwash water of the second combined process. The increase of temperature led to increased CODMn value, but it had a little influence on turbidity and UV254 in MBW.
The membrane water productivity, power consumption for specific water production of the process when treating the sand filter were better than that of the process treating sedimentation tank produced water, but it was contrary with power consumption for specific water production.
引文
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