CN1587123A - Physiochemical and biochemical interactive city sewage treating method - Google Patents

Physiochemical and biochemical interactive city sewage treating method Download PDF

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CN1587123A
CN1587123A CN 200410066451 CN200410066451A CN1587123A CN 1587123 A CN1587123 A CN 1587123A CN 200410066451 CN200410066451 CN 200410066451 CN 200410066451 A CN200410066451 A CN 200410066451A CN 1587123 A CN1587123 A CN 1587123A
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CN100522847C (en
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周琪
郑兴灿
曾庆福
杨殿海
顾国维
颜秀勤
邱兆富
张秀华
钱鸣
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Wuhan Fangyuan Environment Tech Co ltd
Tongji University
North China Municipal Engineering Design and Research Institute Co Ltd
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Tongji University
North China Municipal Engineering Design and Research Institute Co Ltd
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Abstract

本发明属环保技术领域,具体涉及一种物化生化交互式城市污水处理方法。本发明通过在一个反应器内设置预缺氧、厌氧、缺氧、好氧等生化处理单元及可投加絮凝剂的物化处理单元,物化单元在不同运行模式下可用作生化处理,根据进水水质水量的不同和处理要求的变化改变各反应单元的反应条件,实现生化与物化处理系统的串联或并联运行,始终在最低运行费用的情况下,有效去除有机污染物、悬浮固体、氮、磷等营养性物质,保证达到排放要求。

The invention belongs to the technical field of environmental protection, and in particular relates to a physical-chemical-biochemical interactive urban sewage treatment method. The present invention sets pre-anoxic, anaerobic, anoxic, aerobic and other biochemical treatment units in a reactor and a physical and chemical treatment unit that can add flocculants. The physical and chemical units can be used for biochemical treatment under different operating modes. The difference of influent water quality and water quantity and the change of treatment requirements change the reaction conditions of each reaction unit, realize the series or parallel operation of biochemical and physical chemical treatment systems, and effectively remove organic pollutants, suspended solids, and nitrogen at the lowest operating cost. , phosphorus and other nutrients to ensure that the discharge requirements are met.

Description

一种物化生化交互式城市污水处理方法A Physicochemical-Biochemical Interactive Urban Sewage Treatment Method

技术领域technical field

本发明属环保技术领域,具体涉及一种物化生化交互式城市污水处理方法。The invention belongs to the technical field of environmental protection, and in particular relates to a physical-chemical-biochemical interactive urban sewage treatment method.

背景技术Background technique

污水处理技术总体而言可分为物理处理技术、物理化学处理技术、生物化学处理技术和化学处理技术,其中以污水的生物化学处理技术最为常用。生化处理技术亦有很多种,主要是根据微生物的生长条件和供氧方式的不同状况进行分类。生物处理要达到脱氮除磷目的就必须在反应器的空间或时间上创造厌氧、缺氧、好氧等区域,以实现不同形式的厌氧—好氧除磷、好氧—缺氧脱氮,所需的水力停留时间较长,有些工艺达到12小时以上,基建费用和运行费用均较高。目前国际上普遍使用生物脱氮除磷工艺,常用的有:常规的厌氧/缺氧/好氧工艺(A/A/O工艺)、Bardenpho、UCT、VIP、SBR、ICEAS、CASS、UNITANK及各种氧化沟工艺。随着我国污水处理排放要求的提高,我国在污水处理工艺研究上也取得了很大进展,除了使用上述处理工艺外,国内还自行研究开发了倒置A/A/O工艺、水解-厌氧-微氧联合工艺、高负荷活性污泥工艺、生物曝气滤池、高效复合污水生物处理系统、集约化处理工艺等。Generally speaking, sewage treatment technology can be divided into physical treatment technology, physical chemical treatment technology, biochemical treatment technology and chemical treatment technology, among which biochemical treatment technology of sewage is the most commonly used. There are also many kinds of biochemical treatment technologies, which are mainly classified according to the different conditions of microbial growth conditions and oxygen supply methods. In order to achieve the purpose of nitrogen and phosphorus removal in biological treatment, it is necessary to create anaerobic, anoxic, and aerobic regions in the space or time of the reactor, so as to realize different forms of anaerobic-aerobic phosphorus removal and aerobic-anoxic dephosphorization. Nitrogen, the required hydraulic retention time is longer, and some processes reach more than 12 hours, and the capital construction cost and operating cost are high. At present, biological nitrogen and phosphorus removal processes are widely used in the world. The commonly used ones are: conventional anaerobic/anoxic/aerobic process (A/A/O process), Bardenpho, UCT, VIP, SBR, ICEAS, CASS, UNITANK and Various oxidation ditch processes. With the improvement of sewage treatment and discharge requirements in our country, great progress has been made in the research of sewage treatment process in our country. In addition to the above-mentioned treatment process, my country has also researched and developed the inverted A/A/O process, hydrolysis-anaerobic- Micro-oxygen combined process, high-load activated sludge process, biological aeration filter, high-efficiency composite sewage biological treatment system, intensive treatment process, etc.

水的物理化学处理方法有很多种,其中化学混凝处理最常用、最具代表性。由于城市污水水量大,投加混凝剂使得运行费用较高,产泥量大,因此,过去单独采用化学混凝工艺处理城市污水较少。近年来,高效、廉价药剂的不断推出,加上对除磷效果的要求越来越高,化学混凝亦开始受到重视。同济大学、中国市政工程华北设计研究院等单位对上海市合流污水进行了物化强化一级处理的中试研究,向污水中投加三氯化铁,聚合硫酸铝、硫酸铁以及和聚丙烯酰胺(PAM)复配使用,取得了良好的效果,特别是对总磷的去除效果稳定。There are many physical and chemical treatment methods for water, among which chemical coagulation treatment is the most commonly used and most representative. Due to the large volume of urban sewage, the addition of coagulants results in high operating costs and large sludge production. Therefore, in the past, the use of chemical coagulation alone to treat urban sewage was seldom. In recent years, with the continuous introduction of high-efficiency and cheap chemicals, coupled with the increasingly high requirements for phosphorus removal, chemical coagulation has also begun to receive attention. Tongji University, China North China Design and Research Institute of Municipal Engineering and other units have carried out a pilot study on physical and chemical enhanced primary treatment of Shanghai's combined sewage, adding ferric chloride, polyaluminum sulfate, ferric sulfate and polyacrylamide to the sewage (PAM) used in combination has achieved good results, especially the removal of total phosphorus is stable.

采用物化和生化相结合的污水处理工艺目前也有应用,其最显著的特点是流程中投加化学混凝剂,其余则与普通活性污泥法相同或类似,这类工艺反硝化效果差,主要目的是帮助除磷,污水处理运行成本较高。The sewage treatment process that combines physicochemical and biochemical processes is also currently used. Its most notable feature is the addition of chemical coagulants in the process, and the rest are the same or similar to the ordinary activated sludge process. The denitrification effect of this type of process is poor, mainly The purpose is to help remove phosphorus, and the operating cost of sewage treatment is relatively high.

几种主要的城市污水处理工艺如下:Several main urban sewage treatment processes are as follows:

(1)A/A/O及其改良工艺(1) A/A/O and its improved process

随着水体富营养化的不断加重,城市污水处理厂出水的氮磷排放标准越来越高,目前应用最为广泛的脱氮除磷工艺为A/A/O及其改良工艺,该工艺主要由厌氧池、缺氧池、好氧池及二沉池组成,对有机污染物质及悬浮固体去除效果较好,但存在以下一些缺点:①氮和磷的去除效果不稳定;②进水水质水量的变化对运行效果影响较大;③设计水力停留时间较长,运行费用较高。With the increasing eutrophication of water bodies, the nitrogen and phosphorus discharge standards of urban sewage treatment plants are getting higher and higher. At present, the most widely used nitrogen and phosphorus removal process is A/A/O and its improved process. This process is mainly composed of Composed of anaerobic tank, anoxic tank, aerobic tank and secondary sedimentation tank, the removal effect of organic pollutants and suspended solids is good, but there are some disadvantages: ①The removal effect of nitrogen and phosphorus is unstable; ②Influent water quality and quantity The change of the hydraulic pressure has a great influence on the operation effect; ③The designed hydraulic retention time is longer, and the operating cost is higher.

(2)SBR及其变型工艺(2) SBR and its modification process

SBR及其变型工艺是在时间序列上实现厌氧、缺氧及好氧从而达到脱氮除磷功能,反应和沉淀过程集中在一个池体中完成,具有处理构筑物少,占地小,运行灵活等特点,但它也具有一些缺点:①SBR及其变型工艺都使用滗水器,受滗水器出水量的限制,单池处理水量不可能很大,故该工艺不适用于大型污水处理厂;②反应器容积利用率低,水头损失大;③系统设备利用率低,控制复杂;④受反应时间影响,不能完全保证厌氧、缺氧及好氧的反应条件;⑤出水不连续,后续处理困难。SBR and its variant process realize anaerobic, anoxic and aerobic in time series to achieve the function of denitrification and phosphorus removal. The reaction and sedimentation process are concentrated in one pool, which has the advantages of less processing structures, small footprint and flexible operation. and other characteristics, but it also has some disadvantages: ①SBR and its variants both use decanters. Due to the limitation of the water output of the decanters, it is impossible to treat a large amount of water in a single tank, so this process is not suitable for large-scale sewage treatment plants; ②The volume utilization rate of the reactor is low, and the water head loss is large; ③The utilization rate of the system equipment is low, and the control is complicated; ④Affected by the reaction time, the reaction conditions of anaerobic, anoxic and aerobic cannot be fully guaranteed; ⑤The effluent is not continuous, and subsequent treatment difficulty.

(3)UNITANK工艺(3) UNITANK process

UNITANK工艺其实与三沟式氧化沟工艺非常类似,虽然可以省去二沉池及污泥回流系统,但它们存在①没有明显独立的厌氧、缺氧区域,从而影响脱氮除磷效果;②反应池内污泥浓度不平衡,反应周期的后期,进水侧污泥浓度低,沉淀侧污泥浓度高,③UNITANK工艺设备台套数多,设备利用率低,控制复杂;④出水堰固定,初期出水量难以确定,且需要回流处理。The UNITANK process is actually very similar to the three-ditch oxidation ditch process. Although the secondary settling tank and the sludge return system can be omitted, they have ① no obvious independent anaerobic and anoxic areas, which affect the nitrogen and phosphorus removal effect; ② The sludge concentration in the reaction tank is unbalanced. In the later stage of the reaction cycle, the sludge concentration on the inlet side is low, and the sludge concentration on the sedimentation side is high. ③The number of UNITANK process equipment is large, the utilization rate of the equipment is low, and the control is complicated; ④The outlet weir is fixed, and the initial outlet The amount of water is difficult to determine and requires reflux.

发明内容Contents of the invention

本发明目的在于针对城市污水普遍存在的低有机物浓度、低碳氮比、高氮磷浓度的处理难题,提出一种灵活多变的可普遍适应各种水质和处理要求的物化生化交互式城市污水处理方法。The purpose of the present invention is to propose a flexible physical-chemical-biochemical interactive urban sewage that can generally adapt to various water quality and treatment requirements in view of the ubiquitous treatment problems of low organic matter concentration, low carbon-to-nitrogen ratio, and high nitrogen-phosphorus concentration in urban sewage Approach.

本发明提出的一种物化生化交互式城市污水处理方法,采用生化处理单元、物化处理单元组成的交互式反应器,其中生化处理单元由预缺氧池1、厌氧池2、缺氧池3、好氧池4、后曝气池5依次通过隔墙的过水孔相连组成,物化处理单元由絮凝池6组成,后曝气池5通过管道和阀门与絮凝池6相连,生化处理单元的预缺氧池1与回流污泥管道相连,生化处理单元的厌氧池2与进水管道相连,生化处理单元的后曝气池5与沉淀池7相连,物化处理单元一端与进水管相连,另一端与沉淀池7相连,同时生化处理单元与物化处理单元之间通过管道和阀门连接;城市污水经过沉砂处理后进入物化生化交互式反应器,根据水量及水质的不同,选择生化处理单元、物化处理单元串联、并联、或同时生物硝化反硝化运行方式,对污水进行生化处理、物化处理,最后反应器内的混合液进入沉淀池进行泥水分离,沉淀的污泥部分回流至预缺氧池,部分作为剩余污泥排放,其中:A physical-chemical-biochemical interactive urban sewage treatment method proposed by the present invention adopts an interactive reactor composed of a biochemical treatment unit and a physical-chemical treatment unit, wherein the biochemical treatment unit consists of a pre-anoxic pool 1, an anaerobic pool 2, and an anoxic pool 3 , aerobic pool 4, and post-aeration pool 5 are connected successively through the water holes of the partition wall. The physical and chemical treatment unit is composed of flocculation pool 6. The post-aeration pool 5 is connected with flocculation pool 6 through pipelines and valves. The biochemical treatment unit The pre-anoxic tank 1 is connected to the return sludge pipeline, the anaerobic tank 2 of the biochemical treatment unit is connected to the water inlet pipeline, the post-aeration tank 5 of the biochemical treatment unit is connected to the sedimentation tank 7, and one end of the physical and chemical treatment unit is connected to the water inlet pipe. The other end is connected to the sedimentation tank 7, and at the same time, the biochemical treatment unit and the physical and chemical treatment unit are connected through pipes and valves; the urban sewage enters the physical, chemical, biochemical and biochemical interactive reactor after being treated with grit, and the biochemical treatment unit is selected according to the difference in water quantity and quality. , Physical and chemical treatment units in series, parallel, or simultaneous biological nitrification and denitrification operation mode, biochemical treatment, physical and chemical treatment of sewage, and finally the mixed solution in the reactor enters the sedimentation tank for mud-water separation, and part of the precipitated sludge returns to the pre-anoxic pool, partly discharged as excess sludge, of which:

(1)当进水水量为设计流量的0.7-1.5倍、进水水质化学需氧量为70mg/L-800mg/L,生化需氧量为30mg/L-400mg/L,悬浮固体为150mg/L-300mg/L,凯氏氮为20mg/L-60mg/L,总磷为2mg/L-8mg/L时,反应器采用串联运行方式,反应器中预缺氧池(1)、厌氧池(2),缺氧池(3)、好氧池(4)、后曝气池(5)、絮凝池(6)、沉淀池(7)通过管道依次相连;(1) When the influent water volume is 0.7-1.5 times of the design flow rate, the chemical oxygen demand of the influent water is 70mg/L-800mg/L, the biochemical oxygen demand is 30mg/L-400mg/L, and the suspended solids are 150mg/L When L-300mg/L, Kjeldahl nitrogen is 20mg/L-60mg/L, and total phosphorus is 2mg/L-8mg/L, the reactor adopts a series operation mode, and the pre-anoxic pool (1), anaerobic Pool (2), anoxic tank (3), aerobic tank (4), post-aeration tank (5), flocculation tank (6), and sedimentation tank (7) are connected in sequence through pipelines;

(2)当进水流量大于设计流量的1.5倍,进水水质化学需氧量为70mg/L-400mg/L,生化需氧量为30mg/L-200mg/L,悬浮固体为150mg/L-300mg/L,凯氏氮为10mg/L-40mg/L,总磷为1mg/L-5mg/L时;反应器采用并联运行方式,反应器国生化处理单元的厌氧池(2)、缺氧池(3)、好氧池(4)依次相连,并与物化处理单元的絮凝池(6)通过管道并联;(2) When the influent flow rate is greater than 1.5 times the design flow rate, the chemical oxygen demand of the influent water is 70mg/L-400mg/L, the biochemical oxygen demand is 30mg/L-200mg/L, and the suspended solids are 150mg/L- 300mg/L, when the Kjeldahl nitrogen is 10mg/L-40mg/L, and the total phosphorus is 1mg/L-5mg/L; The oxygen tank (3) and the aerobic tank (4) are connected in sequence, and are connected in parallel with the flocculation tank (6) of the physical and chemical treatment unit through pipelines;

(3)当进水流量为设计流量的0.7-1.0倍,进水水质化学需氧量为100mg/L-300mg/L,生化需氧量为50mg/L-150mg/L,悬浮固体为150mg/L-300mg/L,凯氏氮为20mg/L-60mg/L,总磷为2mg/L-4mg/L时,采用同时生物硝化反硝化运行方式,反应器中厌氧池(2)、后曝气池(5)、沉淀池(7)依次相连。(3) When the influent flow rate is 0.7-1.0 times of the design flow rate, the chemical oxygen demand of the influent water is 100mg/L-300mg/L, the biochemical oxygen demand is 50mg/L-150mg/L, and the suspended solids are 150mg/L When L-300mg/L, Kjeldahl nitrogen is 20mg/L-60mg/L, and total phosphorus is 2mg/L-4mg/L, the simultaneous biological nitrification and denitrification operation mode is adopted, and the anaerobic pool (2) in the reactor, after The aeration tank (5) and the sedimentation tank (7) are connected successively.

本发明中,采用串联运行方式时,其控制条件如下:使城市污水全部依次进入生化处理单元中的厌氧池2、缺氧池3、好氧池4,与化学药剂反应,在生化处理单元中停留4-8小时;然后进入物化处理单元中的絮凝池6,与絮凝剂充分混合,在物化处理单元停留0.5-1小时;最后混合液进入沉淀池进行泥水分离,沉淀时间为2-4小时,沉淀污泥回流至预缺氧池1进行内源反硝化去除硝态氮,回流比为25-100%,去除硝态氮并经过缺氧稳定后的污泥进入厌氧池。In the present invention, when adopting the tandem operation mode, its control conditions are as follows: all urban sewage enters the anaerobic pool 2, the anoxic pool 3, and the aerobic pool 4 in the biochemical treatment unit in sequence, and reacts with chemical agents, and the biochemical treatment unit stay in the physical and chemical treatment unit for 4-8 hours; then enter the flocculation tank 6 in the physical and chemical treatment unit, fully mix with the flocculant, and stay in the physical and chemical treatment unit for 0.5-1 hour; finally the mixed solution enters the sedimentation tank for mud-water separation, and the sedimentation time is 2-4 Hours, the settled sludge returns to the pre-anoxic tank 1 for endogenous denitrification to remove nitrate nitrogen, the reflux ratio is 25-100%, the sludge after removing nitrate nitrogen and stabilized by anoxic enters the anaerobic tank.

本发明中,采用并联方式运行时,其控制条件如下:将污水分为2股,一股污水进入生化处理单元中的厌氧池2、缺氧池3、好氧池4,与化学药剂反应,进水流量为总进水量的50%--80%,从好氧池4末端出水,在生化处理单元中停留4-6小时;一股污水进入物化处理单元,与絮凝剂充分混合,絮凝时间为0.5-1.5小时,进水量为总进水量的20%--50%;两股污水经处理后混合进入沉淀池进行泥水分离,沉淀时间为1.5-3小时,部分污泥回流至预缺氧池,污泥回流比为25-80%,部分回流污泥回流至化学絮凝池,污泥回流比为0--25%。In the present invention, when adopting parallel operation, its control conditions are as follows: the sewage is divided into 2 stocks, and one stream of sewage enters the anaerobic pool 2, the anoxic pool 3, and the aerobic pool 4 in the biochemical treatment unit, and reacts with chemical agents , the influent flow is 50%--80% of the total influent, and the water is discharged from the 4th end of the aerobic tank, and stays in the biochemical treatment unit for 4-6 hours; a stream of sewage enters the physical and chemical treatment unit, fully mixed with the flocculant, and flocculated The time is 0.5-1.5 hours, and the water intake is 20%-50% of the total water intake; after the two streams of sewage are treated, they are mixed into the sedimentation tank for mud-water separation. The sedimentation time is 1.5-3 hours, and part of the sludge is returned to the pre-sludge Oxygen tank, the sludge return ratio is 25-80%, part of the returned sludge is returned to the chemical flocculation tank, the sludge return ratio is 0--25%.

本发明中,采用同时硝化反硝化运行方式时,其控制条件为:使污水全部从厌氧池2进入,经后曝气池5曝气,再进入沉淀池7进行泥水分离,同时硝化反硝化运行时间6-10小时,沉淀时间为3-5小时,絮凝池6一同作为后曝气池5进行曝气,污泥回流至预缺氧池(1),污泥回流比为50%-100%,溶解氧为0.6mg/L-1.0mg/L。In the present invention, when the simultaneous nitrification and denitrification operation mode is adopted, the control conditions are as follows: all the sewage enters from the anaerobic tank 2, aerates through the rear aeration tank 5, and then enters the sedimentation tank 7 for mud-water separation, and simultaneously nitrifies and denitrifies The running time is 6-10 hours, the settling time is 3-5 hours, the flocculation tank 6 is used together as the post-aeration tank 5 for aeration, the sludge returns to the pre-anoxic tank (1), and the sludge return ratio is 50%-100 %, dissolved oxygen is 0.6mg/L-1.0mg/L.

本发明中,所述絮凝剂为聚硅铁、聚硅铝等之一种,投加量为20mg/L--80mg/L。In the present invention, the flocculant is one of polysilicon, polysilicon and aluminum, and the dosage is 20mg/L--80mg/L.

本发明中,物化生化交互式反应器由预缺氧池、厌氧池、缺氧池、好氧池、后曝气池、絮凝池及沉淀池组成。预缺氧池用于回流污泥的缺氧反硝化,反硝化碳源主要来自污泥组分,或由部分城市污水加入;厌氧池用于在系统生化除磷时进行厌氧释磷;缺氧池用于系统的反硝化脱氮;好氧池用于系统有机物降解、氨氮硝化、磷的吸收等好氧反应过程;后曝气池在前端流程采用同时硝化反硝化工艺时,用于短时间的高强度曝气,促进沉淀作用;絮凝池在系统生化物化串联运行时,作为辅助物化处理单元,加强系统的除磷效果,也可作为生化单元运行,强化后曝气作用,在系统为生化物化并联运行时,作为单独的物化处理单元,承担部分污水的物化处理任务。In the present invention, the physical-chemical-biochemical interactive reactor is composed of a pre-anoxic tank, an anaerobic tank, an anoxic tank, an aerobic tank, a post-aeration tank, a flocculation tank and a sedimentation tank. The pre-anoxic tank is used for anoxic denitrification of return sludge, and the denitrification carbon source is mainly from sludge components, or added by some urban sewage; the anaerobic tank is used for anaerobic phosphorus release during systemic biochemical phosphorus removal; The anoxic tank is used for denitrification and denitrification of the system; the aerobic tank is used for aerobic reaction processes such as organic matter degradation, ammonia nitrogen nitrification, and phosphorus absorption in the system; the post-aeration tank is used for simultaneous nitrification and denitrification in the front-end process Short-term high-intensity aeration promotes sedimentation; the flocculation tank is used as an auxiliary physicochemical treatment unit to enhance the phosphorus removal effect of the system when the system biochemical physicochemical series is running, and can also be operated as a biochemical unit to strengthen post-aeration. When running in parallel for biochemical and physical chemistry, as a separate physical and chemical treatment unit, it undertakes the physical and chemical treatment of part of the sewage.

本发明的特点是反应系统的综合性和灵活性。The present invention is characterized by the comprehensiveness and flexibility of the reaction system.

本发明通过物化生化交互式反应能有效去除有机污染物、总凯氏氮、悬浮固体及部分磷酸盐。经本发明方法处理后,可使出水COD≤60mg/L,5日生化需氧量BOD5≤20mg/L,悬浮固体SS≤20mg/L,总氮TN-N≤20mg/L,NH3-N≤8mg/L(温度>12℃),NH3-N≤15mg/L(温度≤12℃)等指示均可达到或优于国家《城镇污水处理厂污染物排放标准》(GB18918-2002)的一级标准(B标准)要求。The invention can effectively remove organic pollutants, total Kjeldahl nitrogen, suspended solids and part of phosphate through physical, chemical and biochemical interactive reactions. After being treated by the method of the present invention, effluent COD≤60mg/L, 5-day biochemical oxygen demand BOD 5≤20mg /L, suspended solid SS≤20mg/L, total nitrogen TN-N≤20mg/L, NH 3 - N≤8mg/L (temperature>12°C), NH 3 -N≤15mg/L (temperature≤12°C) and other indications can all meet or exceed the national "Urban Sewage Treatment Plant Pollutant Discharge Standard" (GB18918-2002) The primary standard (B standard) requirements.

附图说明Description of drawings

图1为本发明的交互式反应器平面布置示意图。Fig. 1 is a schematic diagram of the layout of the interactive reactor of the present invention.

图中标号:1为预缺氧池,2为厌氧池,3为缺氧池,4为好氧池,5为后曝气池,6为絮凝池,7为沉淀池。Numbers in the figure: 1 is the pre-anoxic tank, 2 is the anaerobic tank, 3 is the anoxic tank, 4 is the aerobic tank, 5 is the post-aeration tank, 6 is the flocculation tank, and 7 is the sedimentation tank.

具体实施方式Detailed ways

实施例1:Example 1:

正常水质、水量时选择串联运行方式,具体步骤为:将某地经沉砂处理后的城市污水引入交互式反应器,进水进入厌氧池2,好氧池中的混合液通过过墙推流泵回流至缺氧池3;回流污泥进入预缺氧池1,污水依次流过厌氧池2、缺氧池3、好氧池4、后曝气池5,从絮凝池6流出反应器,经过沉淀池7出水。进水平均水温22℃,平均pH值为7.37。污水在反应器内的水力停留时间为9h,平均污泥回流比为100%,平均混合液回流比为200%,污泥浓度维持在3.5g/L上下,平均污泥龄为10d。When the water quality and water quantity are normal, the series operation mode is selected. The specific steps are: introduce the urban sewage treated by sand settling in a certain place into the interactive reactor, the influent water enters the anaerobic pool 2, and the mixed solution in the aerobic pool is pushed through the wall. The flow pump returns to the anoxic tank 3; the return sludge enters the pre-anoxic tank 1, and the sewage flows through the anaerobic tank 2, the anoxic tank 3, the aerobic tank 4, and the post-aeration tank 5 in turn, and flows out of the flocculation tank 6 for reaction device, through the settling tank 7 water outlet. The average temperature of influent water is 22°C, and the average pH value is 7.37. The hydraulic retention time of sewage in the reactor is 9h, the average sludge reflux ratio is 100%, the average mixed liquid reflux ratio is 200%, the sludge concentration is maintained at 3.5g/L, and the average sludge age is 10d.

经检测,进水时CODCr平均值为335mg/L,出水时平均值为42mg/L,去除率为87.5%;进水时SS平均值为212mg/L,出水平均值为17mg/L,去除率为92%;进水时氨氮平均值为30mg/L,出水平均值为3.4mg/L,去除率为88.7%;进水时TN平均值为35mg/L,出水时平均值为12mg/L,去除率为65.7%。进水时TP平均值为3.89mg/L,不投加絮凝剂时,出水时平均值为1.1mg/L,去除率为71.7%;在化学絮凝池投加聚硅铁絮凝剂20mg/L时,平均出水中的TP浓度小于0.5mg/L。After testing, the average value of COD Cr is 335mg/L when entering water, and the average value is 42mg/L when effluent, with a removal rate of 87.5%; The rate is 92%; the average value of ammonia nitrogen is 30mg/L when entering water, the average value of effluent is 3.4mg/L, and the removal rate is 88.7%; the average value of TN is 35mg/L when entering water, and the average value is 12mg/L when effluent , and the removal rate was 65.7%. The average value of TP in the water inlet is 3.89mg/L. When no flocculant is added, the average value of the water outlet is 1.1mg/L, and the removal rate is 71.7%. , the average TP concentration in the effluent is less than 0.5mg/L.

实施例2:Example 2:

对于合流制污水管道在暴雨时,或者分流制管道由于管网渗漏等原因造成暴雨期水量增大时运行物化与生化工艺并联的模式。此时除了污水通过单元厌氧池2、缺氧池3、好氧池4(按好氧方式运行)处理后出水至二沉池(使生物处理系统保持有机负荷不变),超负荷部分污水分流至后曝气池5和絮凝池6,经物化强化处理后合并进入二沉池。For combined sewage pipelines during heavy rains, or when the water volume increases during heavy rains due to pipe network leakage and other reasons in separate pipelines, the mode of parallel connection of physicochemical and biochemical processes is run. At this time, except that the sewage is treated through the unit anaerobic pool 2, anoxic pool 3, and aerobic pool 4 (running in an aerobic mode), the water is discharged to the secondary sedimentation tank (to keep the organic load of the biological treatment system unchanged), and the overloaded part of the sewage The flow is diverted to the rear aeration tank 5 and the flocculation tank 6, and after physical and chemical strengthening treatment, it is merged into the secondary sedimentation tank.

将某地经沉砂处理后的城市污水引入交互式反应器,进水平均水温26.5℃,平均pH值为7.44。污水在生化处理单元的水力停留时间为5.6h,平均污泥回流比为100%,平均混合液回流比为150%,污泥浓度维持在3.0g/L左右,平均污泥龄为15d。物化处理单元水力停留时间为0.4h,平均污泥回流比为25%。The urban sewage treated by sand settling in a certain place is introduced into the interactive reactor. The average water temperature of the incoming water is 26.5°C, and the average pH value is 7.44. The hydraulic retention time of sewage in the biochemical treatment unit is 5.6h, the average sludge return ratio is 100%, the average mixed liquid return ratio is 150%, the sludge concentration is maintained at about 3.0g/L, and the average sludge age is 15d. The hydraulic retention time of the physical and chemical treatment unit is 0.4h, and the average sludge return ratio is 25%.

经检测,进水时CODCr平均值为123mg/L,出水时平均值为38mg/L,去除率为69%;进水时SS平均值为90mg/L,出水平均值为16mg/L,去除率为82%;进水时氨氮平均值为18mg/L,出水平均值为3.9mg/L,去除率为78.2%;进水时TN平均值为21mg/L,出水时平均值为14.2mg/L,去除率为32.4%。进水时TP平均值为2.4mg/L,聚硅铁絮凝剂投加量在30mg/L时,可使得出水中的TP在0.6mg/L以下。After testing, the average value of COD Cr is 123mg/L when entering the water, and the average value is 38mg/L when the water is discharged, and the removal rate is 69%. The removal rate is 82%; the average value of ammonia nitrogen is 18mg/L when entering water, the average value of effluent is 3.9mg/L, and the removal rate is 78.2%; the average value of TN is 21mg/L when entering water, and the average value is 14.2mg/L L, the removal rate was 32.4%. The average value of TP in the water inlet is 2.4mg/L, and when the dosage of polysilicon ferrosilicon flocculant is 30mg/L, the TP in the outlet water can be kept below 0.6mg/L.

实施例3:Example 3:

当进水COD和TN浓度不高或水量不大时的污水处理运行并联模式。此时进水的70%进入后曝气池5和絮凝池6,以充分利用化学生物絮凝,在不到1小时的反应时间内,达到去除有机物和除磷的目的,30%污水依次进入预缺氧池1、厌氧池2、缺氧池3、好氧池4,进行有机物降解和脱氮,这时预缺氧池1、厌氧池2、缺氧池3、好氧池4也可以部分运行,部分单元处于待机状态。When the influent COD and TN concentrations are not high or the water volume is not large, the sewage treatment runs in parallel mode. At this time, 70% of the influent water enters the rear aeration tank 5 and the flocculation tank 6 to make full use of the chemical biological flocculation, and achieve the purpose of removing organic matter and phosphorus within a reaction time of less than 1 hour, and 30% of the sewage enters the pre-aeration tank in turn. Anoxic pool 1, anaerobic pool 2, anoxic pool 3, and aerobic pool 4 are used for organic matter degradation and denitrification. At this time, pre-anoxic pool 1, anaerobic pool 2, anoxic pool 3, and aerobic pool 4 also Partial operation is possible, and some units are on standby.

将某地经沉砂处理后的城市污水泵入交互式反应器,进水平均水温25℃,平均pH值为7.32。污水在生化处理单元的水力停留时间为5.6h,平均污泥回流比为100%,平均混合液回流比为150%,污泥浓度维持在3.0g/L上下,平均污泥龄为20d。物化处理单元水力停留时间为0.5h,平均污泥回流比为50%。The urban sewage treated by sand settling in a certain place is pumped into the interactive reactor, the average temperature of the influent water is 25°C, and the average pH value is 7.32. The hydraulic retention time of sewage in the biochemical treatment unit is 5.6h, the average sludge return ratio is 100%, the average mixed liquid return ratio is 150%, the sludge concentration is maintained at around 3.0g/L, and the average sludge age is 20d. The hydraulic retention time of the physical and chemical treatment unit is 0.5h, and the average sludge return ratio is 50%.

经检测,进水时CODCr平均值为90mg/L,出水时平均值为28mg/L,去除率为68.9%;进水时SS平均值为79mg/L,出水平均值为17mg/L,去除率为78.5%;进水时氨氮平均值为12mg/L,出水平均值为3.6mg/L,去除率为71%;进水时TN平均值为12.7mg/L,出水时平均值为7.6mg/L,去除率为12.1%。进水时TP平均值为1.5mg/L,聚硅铝絮凝剂投加量在20mg/L时,可使得出水中的TP在0.6mg/L以下。After testing, the average value of COD Cr is 90mg/L when entering the water, and the average value is 28mg/L when the water is discharged, and the removal rate is 68.9%. The rate is 78.5%; the average value of ammonia nitrogen is 12mg/L when entering water, the average value of effluent is 3.6mg/L, and the removal rate is 71%; the average value of TN is 12.7mg/L when entering water, and the average value is 7.6mg when effluent /L, the removal rate was 12.1%. The average value of TP in the water inlet is 1.5mg/L, and when the dosage of polysilicon aluminum flocculant is 20mg/L, the TP in the outlet water can be kept below 0.6mg/L.

实施例4:Example 4:

在正常水量,污染物浓度较低时运行同时硝化反硝化模式。此时将厌氧池2、缺氧池3、好氧池4均按低氧运行,达到同时硝化反硝化目的,后曝气池5和絮凝池6按好氧运行。Run the simultaneous nitrification and denitrification mode when the water volume is normal and the pollutant concentration is low. At this time, the anaerobic pool 2, the anoxic pool 3, and the aerobic pool 4 are all operated according to low oxygen to achieve the purpose of simultaneous nitrification and denitrification, and the post-aeration pool 5 and the flocculation pool 6 are operated according to aerobic conditions.

沉砂处理后的城市污水泵入交互式反应器,进水平均水温22℃,平均pH值为7.32。污水在生化处理单元的理论水力停留时间为7.6h,平均污泥回流比为100%,无需混合液回流,污泥浓度维持在2.5g/L左右,平均污泥龄为18d,反应器的溶解氧浓度控制在0.6mg/L-1.0mg/L,后曝气池溶解氧浓度控制3mg/L-4mg/L。The urban sewage after grit settling treatment is pumped into the interactive reactor, the average temperature of the influent water is 22°C, and the average pH value is 7.32. The theoretical hydraulic retention time of sewage in the biochemical treatment unit is 7.6h, the average sludge reflux ratio is 100%, no mixed liquid reflux is required, the sludge concentration is maintained at about 2.5g/L, the average sludge age is 18d, and the dissolution of the reactor The oxygen concentration is controlled at 0.6mg/L-1.0mg/L, and the dissolved oxygen concentration in the rear aeration tank is controlled at 3mg/L-4mg/L.

经检测,进水时CODCr平均值为145mg/L,出水时平均值为38mg/L,去除率为73.8%;进水时SS平均值为129mg/L,出水平均值为15mg/L,去除率为88.4%;进水时氨氮平均值为18mg/L,出水平均值为2.6mg/L,去除率为85%;进水时TN平均值为22.7mg/L,出水时平均值为8.4mg/L,去除率为63%。进水时TP平均值为1.5mg/L,出水中的TP平均值在1.0mg/L以下。After testing, the average value of COD Cr is 145mg/L when entering water, and the average value is 38mg/L when leaving water, with a removal rate of 73.8%; the average value of SS is 129mg/L when entering water, and the average value of effluent is 15mg/L The rate is 88.4%; the average value of ammonia nitrogen is 18mg/L when entering water, the average value of effluent is 2.6mg/L, and the removal rate is 85%; the average value of TN is 22.7mg/L when entering water, and the average value is 8.4mg when effluent /L, the removal rate is 63%. The average value of TP in water inflow is 1.5mg/L, and the average value of TP in water outflow is below 1.0mg/L.

Claims (5)

1, a kind of Physiochemical and biochemical interactive city sewage treating method, it is characterized in that adopting the biochemical treatment unit, the interactive reactor that physicochemical treatment unit is formed, wherein the biochemical treatment unit is by pre-anoxic pond (1), anaerobic pond (2), anoxic pond (3), Aerobic Pond (4), back aeration tank (5) is connected to form by the water hole of partition wall successively, physicochemical treatment unit is made up of flocculation basin (6), back aeration tank (5) links to each other with flocculation basin (6) with valve by pipeline, the unitary pre-anoxic pond of biochemical treatment (1) links to each other with the returned sluge pipeline, the unitary anaerobic pond of biochemical treatment (2) links to each other with inlet channel, biochemical treatment aeration tank, unitary back (5) links to each other with settling tank (7), physicochemical treatment unit one end links to each other with water inlet pipe, the other end links to each other with settling tank (7), be connected with valve by pipeline between biochemical treatment unit and the physicochemical treatment unit simultaneously, municipal effluent enters the Physiochemical and biochemical interactive reactor after handling through sand setting, difference according to the water yield and water quality, select the biochemical treatment unit, the physicochemical treatment unit series connection, in parallel, or while biological nitration denitrification operation scheme, sewage is carried out biochemical treatment, materialization is handled, mixed solution in the final reactor enters settling tank and carries out mud-water separation, sedimentary sludge part is back to pre-anoxic pond, part is as excess sludge discharge, wherein:
(1) when amount of inlet water be design discharge 0.7-1.5 doubly, the influent quality chemical oxygen demand (COD) is 70mg/L-800mg/L, biochemical oxygen demand (BOD) is 30mg/L-400mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-8mg/L, reactor adopts the series operation mode, pre-anoxic pond (1), anaerobic pond (2) in the reactor, anoxic pond (3), Aerobic Pond (4), aeration tank (5), back, flocculation basin (6), settling tank (7) link to each other successively by pipeline;
(2) when flooding velocity 1.5 times greater than design discharge, the influent quality chemical oxygen demand (COD) is 70mg/L-400mg/L, and biochemical oxygen demand (BOD) is 30mg/L-200mg/L, and suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 10mg/L-40mg/L, when total phosphorus is 1mg/L-5mg/L; Reactor adopts the parallel running mode, and the unitary anaerobic pond of reactor state biochemical treatment (2), anoxic pond (3), Aerobic Pond (4) link to each other successively, and in parallel by pipeline with the flocculation basin (6) of physicochemical treatment unit;
(3) when flooding velocity be design discharge 0.7-1.0 doubly, the influent quality chemical oxygen demand (COD) is 100mg/L-300mg/L, biochemical oxygen demand (BOD) is 50mg/L-150mg/L, suspended solids is 150mg/L-300mg/L, kjeldahl nitrogen is 20mg/L-60mg/L, when total phosphorus is 2mg/L-4mg/L, adopt biological nitration denitrification operation scheme simultaneously, anaerobic pond in the reactor (2), aeration tank (5), back, settling tank (7) link to each other successively.
2, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting the series operation mode, its control condition is as follows: make municipal effluent all enter anaerobic pond (2), anoxic pond (3), Aerobic Pond (4) in the biochemical treatment unit successively, stopped 4-8 hour in the biochemical treatment unit; Enter the flocculation basin (6) in the physicochemical treatment unit then,, stopped 0.5-1 hour in physicochemical treatment unit with the flocculation agent thorough mixing; Last mixed solution enters settling tank and carries out mud-water separation, sedimentation time is 2-4 hour, precipitating sludge is back to pre-anoxic pond (1) and carries out endogenous denitrification removal nitric nitrogen, and reflux ratio is 25-100%, and the mud of removing after nitric nitrogen and process anoxic are stablized enters anaerobic pond.
3, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting the parallel way operation, its control condition is as follows: sewage is divided into 2 strands, one sewage enters anaerobic pond (2), anoxic pond (3), the Aerobic Pond (4) in the biochemical treatment unit, flooding velocity is the 50%--80% of total inflow, from the terminal water outlet of Aerobic Pond (4), in the biochemical treatment unit, stopped 4-6 hour; One sewage enters physicochemical treatment unit, and with the flocculation agent thorough mixing, flocculation time is 0.5-1.5 hour, and flooding quantity is the 20%--50% of total inflow; Two strands of sewage are mixed into settling tank after treatment and carry out mud-water separation, and sedimentation time is 1.5-3 hour, and part mud is back to pre-anoxic pond, and return sludge ratio is 25-80%, and partial reflux mud is back to chemical flocculation basin, and return sludge ratio is 0--25%.
4, Physiochemical and biochemical interactive city sewage treating method according to claim 1, when it is characterized in that adopting simultaneously the nitration denitrification operation scheme, its control condition is: sewage is all entered from anaerobic pond (2), through after aeration tank (5) aeration, enter settling tank (7) again and carry out mud-water separation, nitration denitrification is 6-10 working time hour simultaneously, sedimentation time is 3-5 hour, flocculation basin (6) together carries out aeration as aeration tank, back (5), mud is back to pre-anoxic pond (1), return sludge ratio is 50%-100%, and dissolved oxygen is 0.6mg/L--1.0mg/L.
5, the method for Treating Municipal Sewage according to claim 1, its feature also are described flocculation agent for gathering a kind of of ferrosilicon, poly-sial, and dosage is 20mg/L--80mg/L.
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