CN114804298A - Membrane-process tap water plant production wastewater treatment system and method - Google Patents
Membrane-process tap water plant production wastewater treatment system and method Download PDFInfo
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000004065 wastewater treatment Methods 0.000 title claims description 13
- 239000008399 tap water Substances 0.000 title claims description 6
- 235000020679 tap water Nutrition 0.000 title claims description 6
- 238000004062 sedimentation Methods 0.000 claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000002351 wastewater Substances 0.000 claims abstract description 68
- 238000005345 coagulation Methods 0.000 claims abstract description 62
- 230000015271 coagulation Effects 0.000 claims abstract description 62
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 56
- 238000001728 nano-filtration Methods 0.000 claims abstract description 42
- 239000012528 membrane Substances 0.000 claims abstract description 28
- 238000004140 cleaning Methods 0.000 claims abstract description 26
- 239000010802 sludge Substances 0.000 claims abstract description 20
- 239000006228 supernatant Substances 0.000 claims abstract description 19
- 238000004659 sterilization and disinfection Methods 0.000 claims abstract description 17
- 239000000126 substance Substances 0.000 claims abstract description 13
- 238000012423 maintenance Methods 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 11
- 239000006227 byproduct Substances 0.000 claims abstract description 10
- 229910021645 metal ion Inorganic materials 0.000 claims abstract description 9
- 239000000084 colloidal system Substances 0.000 claims abstract description 7
- 239000012535 impurity Substances 0.000 claims abstract description 6
- 230000001105 regulatory effect Effects 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 14
- 238000005189 flocculation Methods 0.000 claims description 9
- 230000016615 flocculation Effects 0.000 claims description 9
- 230000004907 flux Effects 0.000 claims description 6
- 238000005374 membrane filtration Methods 0.000 claims description 6
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 238000003825 pressing Methods 0.000 claims 4
- 230000001112 coagulating effect Effects 0.000 claims 3
- 150000003839 salts Chemical class 0.000 claims 1
- 238000011085 pressure filtration Methods 0.000 abstract description 7
- 238000011084 recovery Methods 0.000 abstract description 6
- 239000005416 organic matter Substances 0.000 abstract description 4
- 230000003750 conditioning effect Effects 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 150000002505 iron Chemical class 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000011001 backwashing Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000007654 immersion Methods 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000004009 herbicide Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000002243 precursor Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
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- 239000008394 flocculating agent Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
本发明公开了一种膜法自来水厂生产废水处理系统及方法，包括一号混凝沉淀池、一号超滤系统、清水池，一号混凝沉淀池的污泥经压滤后的废水、一号超滤系统的物理清洗废水和维护性化学清洗废水送入调节池，生产废水中杂质初步沉淀，上清液进入二号混凝沉淀池，去除有机物、悬浮固体、胶体，二号混凝沉淀池上清液依次进入超滤系统、纳滤系统，去除水中消毒副产物和金属离子，纳滤处理后的水直接进入清水池，消毒后供给管网用户；二号混凝沉淀池的污泥经压滤后的废水、二号超滤系统的物理清洗废水和维护性化学清洗废水、纳滤系统的浓水回流至调节池。本发明可以提高自来水厂的回收率，提高水资源利用率。
The invention discloses a system and method for the treatment of wastewater produced in a membrane water plant, comprising a No. 1 coagulation sedimentation tank, a No. 1 ultrafiltration system, a clear water tank, and the waste water after the sludge in the No. 1 coagulation sedimentation tank is filtered by pressure, The physical cleaning wastewater and maintenance chemical cleaning wastewater of the No. 1 ultrafiltration system are sent to the conditioning tank, the impurities in the production wastewater are preliminarily precipitated, and the supernatant enters the No. 2 coagulation sedimentation tank to remove organic matter, suspended solids, and colloids. The No. 2 coagulation The supernatant of the sedimentation tank enters the ultrafiltration system and the nanofiltration system in turn to remove the disinfection by-products and metal ions in the water. The water after the nanofiltration treatment directly enters the clear water tank, and is supplied to the users of the pipe network after disinfection; the sludge in the No. 2 coagulation sedimentation tank The waste water after pressure filtration, the physical cleaning waste water and maintenance chemical cleaning waste water of the No. 2 ultrafiltration system, and the concentrated water of the nanofiltration system are returned to the adjustment tank. The invention can improve the recovery rate of the water plant and improve the utilization rate of water resources.
Description
技术领域technical field
本发明属于市政废水处理领域，更具体地说，是涉及一种膜法自来水厂生产废水处理系统及方法。The invention belongs to the field of municipal wastewater treatment, and more particularly relates to a system and method for treating production wastewater in a membrane-based waterworks.
背景技术Background technique
膜技术日趋成熟，膜产品价格大幅下降，超滤膜在自来水提质，市政污水再生的领域逐渐普及，十年前的万吨级膜法水厂逐渐发展到目前的几十万吨级膜法水厂，超滤甚至纳滤已是新建或改造水厂的首选技术。Membrane technology is becoming more and more mature, the price of membrane products has dropped significantly, ultrafiltration membranes have gradually become popular in the field of tap water quality improvement and municipal sewage regeneration. Waterworks, ultrafiltration and even nanofiltration are the technologies of choice for new or retrofitted waterworks.
超滤膜技术主要包括两种形式，浸没式膜过滤和连续膜过滤，每运行20-60min需进行自动反清洗，超滤反清洗废水一般是直接入管网或者打到原水池，超滤反洗废水含有大量的悬浮物、细菌等，经过曝气后，反洗废水中的泥比较细腻，沉淀不好，打到前段原水池，易影响系统正常产水。Ultrafiltration membrane technology mainly includes two forms, submerged membrane filtration and continuous membrane filtration. Automatic backwashing is required every 20-60 minutes of operation. Ultrafiltration backwashing wastewater is generally directly fed into the pipe network or sent to the raw water pool, and ultrafiltration backwashing is performed. The wastewater contains a large amount of suspended solids, bacteria, etc. After aeration, the mud in the backwashing wastewater is relatively fine, and the sedimentation is not good. If it hits the raw water tank in the front section, it will easily affect the normal water production of the system.
采用超滤技术的自来水整体水回收率一般在85％-92％之间，对于50万吨的水厂来说，每天清洗废水损失4-7.5万吨水,相当于一个小型水自来水厂的处理量。中国专利CN200710058727.5将收集反洗废水，采用铁盐絮凝剂进行管道絮凝，絮凝后的水进入到浸没式超滤系统，投加粉末活性炭到浸没式超滤系统，粉末活性炭会加剧浸没式超滤系统的水中悬浮物的含量，加剧膜污染。中国专利CN201110094872.5也是采用铁盐和粉末活性炭将收集的反洗废水进行混凝沉淀，然后经过自清洗过滤器以后，进入超滤系统前段。The overall water recovery rate of tap water using ultrafiltration technology is generally between 85% and 92%. For a water plant with a capacity of 500,000 tons, 40,000 to 75,000 tons of water is lost from cleaning wastewater every day, which is equivalent to the treatment of a small water plant. quantity. Chinese patent CN200710058727.5 will collect backwash wastewater, use iron salt flocculant for pipeline flocculation, the water after flocculation enters the immersion ultrafiltration system, and add powder activated carbon to the immersion ultrafiltration system, powder activated carbon will aggravate the immersion ultrafiltration system. The content of suspended solids in the water of the filtration system aggravates membrane fouling. Chinese patent CN201110094872.5 also uses iron salt and powdered activated carbon to coagulate and precipitate the collected backwash wastewater, and then pass through the self-cleaning filter before entering the front section of the ultrafiltration system.
发明内容SUMMARY OF THE INVENTION
针对现有技术粉末活性炭投加量会给浸没式膜过滤带来污染，管道絮凝混凝剂反应不彻底等技术不足，本发明提出一种膜法自来水厂生产废水处理系统及方法，可以提高自来水厂的回收率，提高水资源利用率。In view of the technical deficiencies in the prior art, such as the amount of powdered activated carbon that will cause pollution to the immersed membrane filtration, and the incomplete reaction of the pipeline flocculant coagulant, the present invention proposes a membrane-based water treatment plant production wastewater treatment system and method, which can improve the efficiency of tap water. The recovery rate of the plant increases the utilization rate of water resources.
本发明的目的可通过以下技术方案实现。The object of the present invention can be achieved through the following technical solutions.
本发明膜法自来水厂生产废水处理系统，包括通过管道依次连通的一号混凝沉淀池、一号超滤系统、清水池，所述一号混凝沉淀池的污泥出口通过管道连接至压滤池，所述压滤池的废水出口通过管道依次连接有调节池、二号混凝沉淀池、超滤系统、纳滤系统，所述二号混凝沉淀池的污泥出口通过管道连接至压滤池，所述一号超滤系统、二号超滤系统、纳滤系统的废水出口均通过管道连接至调节池，所述纳滤系统的清水出口通过管道连接至清水池；The membrane method water treatment plant production wastewater treatment system of the present invention includes a No. 1 coagulation sedimentation tank, a No. 1 ultrafiltration system, and a clear water tank that are connected in sequence through pipes, and the sludge outlet of the No. 1 coagulation and sedimentation tank is connected to the pressure through pipes. The filter tank, the waste water outlet of the filter press is connected to the regulating tank, the No. 2 coagulation sedimentation tank, the ultrafiltration system, and the nanofiltration system in turn through the pipeline, and the sludge outlet of the No. 2 coagulation sedimentation tank is connected to the No. 2 coagulation sedimentation tank through the pipeline. Pressure filter tank, the waste water outlet of the No. 1 ultrafiltration system, the No. 2 ultrafiltration system, and the nanofiltration system are all connected to the regulating tank through pipelines, and the clean water outlet of the nanofiltration system is connected to the clean water tank through pipelines;
一号混凝沉淀池的污泥经压滤后的废水、一号超滤系统的物理清洗废水和维护性化学清洗废水均作为生产废水送入调节池，生产废水中的杂质初步沉淀，上清液进入二号混凝沉淀池，去除有机物、悬浮固体和胶体，二号混凝沉淀池的上清液依次进入超滤系统、纳滤系统，去除水中的消毒副产物和金属离子，纳滤处理后的水直接进入清水池，消毒后供给管网用户；其中，二号混凝沉淀池的污泥经压滤后的废水、二号超滤系统的物理清洗废水和维护性化学清洗废水、纳滤系统的浓水均通过管道回流至调节池。The sludge of No. 1 coagulation and sedimentation tank after pressure filtration, the physical cleaning wastewater and maintenance chemical cleaning wastewater of No. 1 ultrafiltration system are all sent to the adjustment tank as production wastewater. The impurities in the production wastewater are preliminarily precipitated, and the supernatant The liquid enters the No. 2 coagulation and sedimentation tank to remove organic matter, suspended solids and colloids. The supernatant of the No. 2 coagulation and sedimentation tank enters the ultrafiltration system and the nanofiltration system in turn to remove the disinfection by-products and metal ions in the water. Nanofiltration treatment The purified water directly enters the clear water tank and is supplied to the users of the pipe network after disinfection; among them, the sludge in the No. 2 coagulation and sedimentation tank is filtered by the waste water, the physical cleaning waste water and the maintenance chemical cleaning waste water of the No. 2 ultrafiltration system, and the sodium The concentrated water of the filtration system is returned to the adjustment tank through the pipeline.
所述调节池设置为半地下，生产废水在重力作用下流入调节池，在调节池停留0.5～5h后，上清液溢流进入二号混凝沉淀池中的混凝池，絮凝时间约30min，然后进入二号混凝沉淀池中的沉淀池，沉淀池上清液依次进入二号超滤系统和纳滤系统。The regulating tank is set as semi-underground, and the production wastewater flows into the regulating tank under the action of gravity. After staying in the regulating tank for 0.5 to 5 hours, the supernatant overflows into the coagulation tank in the No. 2 coagulation sedimentation tank, and the flocculation time is about 30 minutes. , and then enter the sedimentation tank in the No. 2 coagulation sedimentation tank, and the supernatant of the sedimentation tank enters the No. 2 ultrafiltration system and nanofiltration system in turn.
所述一号混凝沉淀池和二号混凝沉淀池均由混凝池和沉淀池构成，所述混凝池为网格絮凝池，采用氯化铁或硫酸铁作为铁盐絮凝剂，投加量为10-50mg/L，所述沉淀池采用斜管沉淀。The No. 1 coagulation sedimentation tank and the No. 2 coagulation sedimentation tank are composed of a coagulation tank and a sedimentation tank. The coagulation tank is a grid flocculation tank, and ferric chloride or ferric sulfate is used as the iron salt flocculant. The added amount is 10-50 mg/L, and the sedimentation tank adopts inclined tube sedimentation.
所述二号超滤系统和纳滤系统构成双膜系统，所述二号超滤系统采用超滤膜，为连续膜过滤系统，采用80平米组件，设计通量40-60L/m2*h；所述纳滤系统采用卷式纳滤膜，设计通量20-30L/m2*h。The No. 2 ultrafiltration system and the nanofiltration system constitute a double-membrane system. The No. 2 ultrafiltration system adopts an ultrafiltration membrane, which is a continuous membrane filtration system, using 80 square meters of components, and the designed flux is 40-60L/m 2 *h ; The nanofiltration system adopts roll-type nanofiltration membrane, and the designed flux is 20-30L/m 2 *h.
本发明的目的还可通过以下技术方案实现。The object of the present invention can also be achieved through the following technical solutions.
本发明膜法自来水厂生产废水处理方法，包括以下过程：The membrane method water treatment plant production wastewater treatment method of the present invention comprises the following processes:
原水依次经一号混凝沉淀池、一号超滤系统、清水池处理后工管网用户使用；一号混凝沉淀池的污泥经压滤后的废水、一号超滤系统的物理清洗废水和维护性化学清洗废水均作为生产废水送入调节池，生产废水中的杂质初步沉淀，上清液进入二号混凝沉淀池，去除有机物、悬浮固体和胶体，二号混凝沉淀池的上清液依次进入超滤系统、纳滤系统，去除水中的消毒副产物和金属离子，纳滤处理后的水直接进入清水池，消毒后供给管网用户；其中，二号混凝沉淀池的污泥经压滤后的废水、二号超滤系统的物理清洗废水和维护性化学清洗废水、纳滤系统的浓水均通过管道回流至调节池。The raw water is processed by No. 1 coagulation sedimentation tank, No. 1 ultrafiltration system, and clean water tank for use by the users of the pipeline network; the sludge in the No. 1 coagulation sedimentation tank is filtered by waste water, and the physical cleaning of the No. 1 ultrafiltration system Wastewater and maintenance chemical cleaning wastewater are sent to the conditioning tank as production wastewater, the impurities in the production wastewater are preliminarily precipitated, and the supernatant enters the No. 2 coagulation and sedimentation tank to remove organic matter, suspended solids and colloids. The supernatant enters the ultrafiltration system and the nanofiltration system in turn to remove the disinfection by-products and metal ions in the water. The water after the nanofiltration treatment directly enters the clear water tank and is supplied to the users of the pipe network after disinfection; among them, the No. 2 coagulation sedimentation tank The waste water after sludge pressure filtration, the physical cleaning waste water and maintenance chemical cleaning waste water of the No. 2 ultrafiltration system, and the concentrated water of the nanofiltration system are all returned to the adjustment tank through the pipeline.
与现有技术相比，本发明的技术方案所带来的有益效果是：Compared with the prior art, the beneficial effects brought by the technical solution of the present invention are:
(1)本发明纳滤系统作为生产废水处理的终端工艺，可去除除草剂，TOC、UV254消毒副产物的前驱物等，消毒副产物的去除率达到80％以上，钙、镁和铁等二价金属离子去除率90％以上。(1) The nanofiltration system of the present invention is used as a terminal process for production wastewater treatment, which can remove herbicides, TOC, UV254 precursors of disinfection by-products, etc., the removal rate of disinfection by-products reaches more than 80%, calcium, magnesium and iron etc. The removal rate of valence metal ions is more than 90%.
(2)本发明工艺简单，自动化程度高，双膜系统集成度高，占地面积小，操作方便。(2) The process of the invention is simple, the degree of automation is high, the integration degree of the double-membrane system is high, the occupation area is small, and the operation is convenient.
(3)本发明水厂各工艺段的生产废水均回用再处理，双膜系统回收率90％-95％可将自来水厂的回收率提高5-10％以上，整体水回收率提高至98％以上，提高水资源利用率，减少了水厂的外排水量。(3) The production wastewater in each process section of the water plant of the present invention is reused and reprocessed. The recovery rate of the double-membrane system is 90%-95%, which can increase the recovery rate of the water plant by more than 5-10%, and the overall water recovery rate is increased to 98%. % or more, the utilization rate of water resources is improved, and the external drainage of the water plant is reduced.
(4)本发明工艺处理后的水可直接进入清水池，消毒后供给用户。不会增加原有处理工艺的负担，影响水厂的出水水质。(4) The water treated by the process of the present invention can directly enter the clear water pool, and be supplied to the user after being sterilized. It will not increase the burden of the original treatment process and affect the effluent quality of the water plant.
附图说明Description of drawings
图1是本发明的工艺流程图。Fig. 1 is a process flow diagram of the present invention.
具体实施方式Detailed ways
下面结合附图对本发明作进一步的描述。The present invention will be further described below in conjunction with the accompanying drawings.
如图1所示，本发明膜法自来水厂生产废水处理系统，包括通过管道依次连通的一号混凝沉淀池、一号超滤系统、清水池，所述一号混凝沉淀池的污泥出口通过管道连接至压滤池，所述压滤池的废水出口通过管道依次连接有调节池、二号混凝沉淀池、超滤系统、纳滤系统，所述二号混凝沉淀池的污泥出口通过管道连接至压滤池，所述一号超滤系统、二号超滤系统、纳滤系统的废水出口均通过管道连接至调节池，所述纳滤系统的清水出口通过管道连接至清水池。As shown in Figure 1, the membrane process water treatment plant production wastewater treatment system of the present invention comprises No. 1 coagulation sedimentation tank, No. 1 ultrafiltration system, and clear water tank connected in turn through pipelines, and the sludge in the No. 1 coagulation sedimentation tank is The outlet is connected to the filter press tank through a pipeline, and the waste water outlet of the filter press tank is sequentially connected to a regulating tank, a No. 2 coagulation sedimentation tank, an ultrafiltration system, and a nanofiltration system through a pipeline. The mud outlet is connected to the filter press through a pipeline, the waste water outlets of the No. 1 ultrafiltration system, the No. 2 ultrafiltration system, and the nanofiltration system are all connected to the regulating tank through a pipeline, and the clean water outlet of the nanofiltration system is connected to the pressure filter through a pipeline. Clean water tank.
其中，所述一号混凝沉淀池和二号混凝沉淀池均由混凝池和沉淀池构成，主要去除生产废水中的部分金属离子、固体悬浮物和胶体等物质。所述混凝池为网格絮凝池，采用氯化铁或硫酸铁等铁盐絮凝剂，投加量为10-50mg/L。所述沉淀池采用斜管沉淀。Among them, the No. 1 coagulation sedimentation tank and the No. 2 coagulation sedimentation tank are composed of a coagulation tank and a sedimentation tank, and mainly remove some metal ions, solid suspended solids, colloids and other substances in the production wastewater. The coagulation tank is a grid flocculation tank, and an iron salt flocculant such as ferric chloride or ferric sulfate is used, and the dosage is 10-50 mg/L. The sedimentation tank adopts inclined tube sedimentation.
其中，所述二号超滤系统和纳滤系统构成双膜系统，双膜系统集成度高，占地面积小，自动化程度高。所述二号超滤系统采用超滤膜，为连续膜过滤系统，采用80平米组件，设计通量40-60L/m2*h。所述纳滤系统采用卷式纳滤膜，设计通量20-30L/m2*h，纳滤处理后的废水可直接进入清水池，消毒后供给用户。纳滤系统作为生产废水处理的终端工艺，可去除除草剂，TOC、UV254消毒副产物的前驱物等，消毒副产物的去除率达到80％以上，钙、镁和铁等二价金属离子去除率90％以上。Among them, the No. 2 ultrafiltration system and nanofiltration system constitute a double-membrane system, and the double-membrane system has a high degree of integration, a small footprint and a high degree of automation. The No. 2 ultrafiltration system adopts ultrafiltration membrane, which is a continuous membrane filtration system, adopts 80 square meters of components, and has a designed flux of 40-60L/m 2 *h. The nanofiltration system adopts a roll-type nanofiltration membrane, and the designed flux is 20-30L/m 2 *h. The wastewater after nanofiltration treatment can directly enter the clean water tank and be supplied to users after disinfection. Nanofiltration system, as the terminal process of production wastewater treatment, can remove herbicides, precursors of TOC, UV254 disinfection by-products, etc. The removal rate of disinfection by-products reaches more than 80%, and the removal rate of divalent metal ions such as calcium, magnesium and iron is more than 90 percent.
其中，所述调节池设置为半地下，生产废水在重力作用下流入调节池，在调节池停留0.5～5h后，上清液溢流进入二号混凝沉淀池中的混凝池，絮凝时间约30min，然后进入二号混凝沉淀池中的沉淀池，沉淀池上清液依次进入二号超滤系统和纳滤系统。Wherein, the regulating tank is set as semi-underground, and the production wastewater flows into the regulating tank under the action of gravity. After staying in the regulating tank for 0.5 to 5 hours, the supernatant overflows into the coagulation tank in the No. 2 coagulation sedimentation tank, and the flocculation time About 30min, and then enter the sedimentation tank in the No. 2 coagulation sedimentation tank, and the supernatant of the sedimentation tank enters the No. 2 ultrafiltration system and nanofiltration system in turn.
本发明膜法自来水厂生产废水处理方法，包括以下过程：The membrane method water treatment plant production wastewater treatment method of the present invention comprises the following processes:
原水依次经一号混凝沉淀池、一号超滤系统、清水池处理后工管网用户使用。一号混凝沉淀池的污泥经压滤后的废水、一号超滤系统的物理清洗废水和维护性化学清洗废水均作为生产废水送入调节池，停留时间0.5-2h，生产废水中的杂质初步沉淀，上清液进入二号混凝沉淀池中的混凝池，絮凝时间约30min，采用氯化铁、硫酸铁等铁盐絮凝剂，投加量为30mg/L，然后进入二号混凝沉淀池中的沉淀池，去除有机物、悬浮固体和胶体等，二号混凝沉淀池中沉淀池的上清液依次进入超滤系统、纳滤系统，去除水中的消毒副产物和金属离子等，纳滤处理后的水直接进入清水池，消毒后供给管网用户。其中，二号混凝沉淀池的污泥经压滤后的废水、二号超滤系统的物理清洗废水和维护性化学清洗废水、纳滤系统的浓水均通过管道回流至调节池。一号混凝沉淀池和二号混凝沉淀池的污泥经压滤后得到的泥巴均可收集外排掉。实现生产废水全部再生回用，自来水水厂外排废水很少，外排的固体为压滤后的污泥滤饼，实现了废水减量。The raw water is processed by the No. 1 coagulation sedimentation tank, the No. 1 ultrafiltration system, and the clear water tank for use by the users of the pipeline network. The sludge from the No. 1 coagulation and sedimentation tank after pressure filtration, the physical cleaning wastewater and the maintenance chemical cleaning wastewater of the No. 1 ultrafiltration system are all sent to the adjustment tank as production wastewater, and the residence time is 0.5-2h. The impurities are preliminarily precipitated, and the supernatant liquid enters the coagulation tank in the No. 2 coagulation sedimentation tank. The flocculation time is about 30 minutes. Iron salt flocculants such as ferric chloride and ferric sulfate are used, and the dosage is 30 mg/L, and then enters the No. 2 coagulation and sedimentation tank. The sedimentation tank in the coagulation sedimentation tank removes organic matter, suspended solids and colloids, etc. The supernatant of the sedimentation tank in the second coagulation sedimentation tank enters the ultrafiltration system and nanofiltration system in turn to remove disinfection by-products and metal ions in water Wait, the water after nanofiltration treatment directly enters the clear water tank, and is supplied to the users of the pipe network after disinfection. Among them, the waste water after pressure filtration of sludge in the No. 2 coagulation sedimentation tank, the physical cleaning waste water and maintenance chemical cleaning waste water of the No. 2 ultrafiltration system, and the concentrated water of the nanofiltration system are all returned to the adjustment tank through the pipeline. The sludge obtained by the pressure filtration of the sludge in the No. 1 coagulation and sedimentation tank and the No. 2 coagulation and sedimentation tank can be collected and discharged. All production wastewater can be recycled and reused. The water plant discharges very little waste water, and the discharged solid is the sludge filter cake after pressure filtration, which realizes the reduction of waste water.
尽管上面结合附图对本发明的功能及工作过程进行了描述，但本发明并不局限于上述的具体功能和工作过程，上述的具体实施方式仅仅是示意性的，而不是限制性的，本领域的普通技术人员在本发明的启示下，在不脱离本发明宗旨和权利要求所保护的范围情况下，还可以做出很多形式，这些均属于本发明的保护之内。Although the functions and working process of the present invention have been described above in conjunction with the accompanying drawings, the present invention is not limited to the above-mentioned specific functions and working processes. Under the inspiration of the present invention, those of ordinary skill in the art can also make many forms without departing from the scope of the present invention and the protection scope of the claims, which all belong to the protection of the present invention.
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