CN202729946U - Two-stage anoxic/oxic (A/O)-membrane biological reactor (MBR) nitrogen and phosphorus removal device - Google Patents
Two-stage anoxic/oxic (A/O)-membrane biological reactor (MBR) nitrogen and phosphorus removal device Download PDFInfo
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- 239000012528 membrane Substances 0.000 title claims abstract description 48
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title abstract description 54
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title abstract description 44
- 229910052698 phosphorus Inorganic materials 0.000 title abstract description 44
- 239000011574 phosphorus Substances 0.000 title abstract description 44
- 229910052757 nitrogen Inorganic materials 0.000 title abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 238000005273 aeration Methods 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims 2
- 239000010802 sludge Substances 0.000 abstract description 31
- 239000010865 sewage Substances 0.000 abstract description 30
- 238000004062 sedimentation Methods 0.000 abstract description 15
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- 239000005416 organic matter Substances 0.000 abstract 1
- 238000011112 process operation Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 17
- 230000008569 process Effects 0.000 description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 10
- 241000894006 Bacteria Species 0.000 description 8
- 239000011259 mixed solution Substances 0.000 description 7
- 238000000926 separation method Methods 0.000 description 5
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000012017 passive hemagglutination assay Methods 0.000 description 4
- 229920000903 polyhydroxyalkanoate Polymers 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000012851 eutrophication Methods 0.000 description 3
- 230000003834 intracellular effect Effects 0.000 description 3
- 238000009285 membrane fouling Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000006213 oxygenation reaction Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000009360 aquaculture Methods 0.000 description 1
- 244000144974 aquaculture Species 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000009528 severe injury Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
本实用新型公开了一种两级A/O—MBR脱氮除磷装置。所述脱氮除磷装置包括依次连通的厌氧池、第一缺氧池、第一好氧池、第二缺氧池、第二好氧池和膜池;所述厌氧池和第二缺氧池均与进水管相连通,所述进水管上设有进水泵;所述膜池内设有膜组件,所述膜组件与出水管相连通,所述出水管上设有出水泵;所述膜池的底部设有沉淀池,所述沉淀池通过污泥混合液回流管与所述厌氧池相连通,所述污泥混合液回流管上设有回流泵。利用该脱氮除磷装置,既能够很好地去除污水中有机物、氮、磷等污染物,又能降低MBR工艺运行能耗,因此适合于处理城镇生活污水。
The utility model discloses a two-stage A/O-MBR nitrogen and phosphorus removal device. The denitrification and phosphorus removal device includes an anaerobic tank, a first anoxic tank, a first aerobic tank, a second anoxic tank, a second aerobic tank and a membrane tank connected in sequence; the anaerobic tank and the second The anoxic pools are all connected to the water inlet pipes, and the water inlet pipes are provided with water inlet pumps; the membrane modules are arranged in the membrane pools, and the membrane modules are connected to the water outlet pipes, and the water outlet pipes are provided with water outlet pumps; A sedimentation tank is provided at the bottom of the membrane pool, and the sedimentation tank is connected with the anaerobic tank through a sludge mixed liquid return pipe, and a return pump is arranged on the sludge mixed liquid return pipe. The nitrogen and phosphorus removal device can not only remove organic matter, nitrogen, phosphorus and other pollutants in sewage well, but also reduce the energy consumption of MBR process operation, so it is suitable for treating urban domestic sewage.
Description
技术领域 technical field
本实用新型涉及一种脱氮除磷装置,具体涉及一种应用膜-生物反应器的两级A/O—MBR脱氮除磷装置。The utility model relates to a nitrogen and phosphorus removal device, in particular to a two-stage A/O-MBR nitrogen and phosphorus removal device using a membrane-biological reactor.
背景技术 Background technique
城市污水中含有大量的氮、磷污染物质,当污水排入湖泊、水库、河口、海湾等缓流水体后,氮、磷逐渐积累下来,使水生生物特别是藻类大量繁殖,最终导致水体生态平衡遭到严重破坏,即发生所谓的富营养化现象。富营养化不仅会破坏水体原有的生态系统,还会对渔业、养殖业等造成重大的经济损失,严重时甚至危害到人类健康。为了有效遏制水体富营养化,越来越多的国家和地区制定了严格的氮、磷排放标准。但传统的污水处理工艺由于在脱氮和除磷之间存在对碳源需求的矛盾,出水氮、磷浓度难以同时达标,这使得污水脱氮除磷成为了污水处理领域的热点和难点。Urban sewage contains a large amount of nitrogen and phosphorus pollutants. When the sewage is discharged into slow-flowing water bodies such as lakes, reservoirs, estuaries, and bays, nitrogen and phosphorus gradually accumulate, causing aquatic organisms, especially algae, to proliferate, and eventually leading to ecological balance of the water body. severe damage, that is, the occurrence of the so-called eutrophication phenomenon. Eutrophication will not only destroy the original ecosystem of the water body, but also cause significant economic losses to fisheries and aquaculture, and even endanger human health in severe cases. In order to effectively curb the eutrophication of water bodies, more and more countries and regions have formulated strict nitrogen and phosphorus discharge standards. However, due to the contradiction between the demand for carbon sources between denitrification and phosphorus removal in the traditional sewage treatment process, it is difficult to meet the nitrogen and phosphorus concentrations in the effluent at the same time, which makes the denitrification and phosphorus removal of sewage become a hot and difficult point in the field of sewage treatment.
MBR是一种将膜分离技术与生物处理单元相组合的新型污水处理与回用工艺。该工艺由于采用高效的膜分离替代传统活性污泥工艺中的二沉池,固液分离效率高,出水好且稳定,可直接回用;反应器内可保持高浓度的微生物量,处理容积负荷高,占地面积省;剩余污泥产生量小;操作管理方便,自动化程度高等。鉴于MBR的优点,国内外已建立了相当规模和数量的MBR污水处理和资源化工程。MBR由于可以在高污泥浓度下运行,因此可以提高系统的处理能力,但过高污泥浓度对膜污染控制不利,需要较高曝气能耗来控制膜污染。MBR is a new sewage treatment and reuse process that combines membrane separation technology and biological treatment unit. Because the process adopts efficient membrane separation to replace the secondary sedimentation tank in the traditional activated sludge process, the solid-liquid separation efficiency is high, the effluent is good and stable, and can be reused directly; the reactor can maintain a high concentration of microbial biomass and handle volume load High, low floor space; small amount of excess sludge; convenient operation and management, high degree of automation. In view of the advantages of MBR, a considerable scale and number of MBR sewage treatment and recycling projects have been established at home and abroad. Because MBR can operate under high sludge concentration, it can improve the treatment capacity of the system, but too high sludge concentration is not good for membrane fouling control, and high aeration energy consumption is required to control membrane fouling.
污水脱氮除磷和降低系统运行能耗是MBR的重要应用领域和发展方向,由于机理复杂,影响因素众多,现有研究大多独立考察MBR的脱氮除磷或者节能降耗,难以两者兼顾。部分研究采用外加碳源的方式同时改善脱氮除磷效果,但由于增加了工艺的复杂度和运行成本,不适合大规模推广。有研究通过应用A2O工艺反硝化除磷技术,使脱氮和除磷可以共用一部分碳源,能在一定程度上缓解两者的矛盾,但其效果仍然有限,在应对低碳氮比污水时脱氮效果不理想。也有采用内源反硝化技术,利用微生物的胞内物质作为碳源,无需污水中的碳源,因而非常适用于通常碳源含量有限的城市污水的脱氮除磷处理,该技术稳定性还需优化。节能方面主要以优化膜组器结构、开发更高效的曝气方式来达到节能降耗的目的。Sewage denitrification and phosphorus removal and reduction of system energy consumption are important application fields and development directions of MBR. Due to the complex mechanism and many influencing factors, most of the existing researches independently investigate the denitrification and phosphorus removal or energy saving and consumption reduction of MBR, and it is difficult to balance both. . Some studies use the method of adding an external carbon source to improve the nitrogen and phosphorus removal effect at the same time, but it is not suitable for large-scale promotion due to the increase of process complexity and operating cost. Some studies have used the denitrification and phosphorus removal technology of A 2 O process to make denitrification and phosphorus removal share part of the carbon source, which can alleviate the contradiction between the two to a certain extent, but the effect is still limited. The denitrification effect is not ideal. There is also an endogenous denitrification technology that uses the intracellular substances of microorganisms as a carbon source and does not require carbon sources in sewage. Therefore, it is very suitable for the denitrification and phosphorus removal of urban sewage with limited carbon source content. The stability of this technology still needs to be improved. optimization. In terms of energy saving, the goal of saving energy and reducing consumption is mainly achieved by optimizing the structure of membrane modules and developing more efficient aeration methods.
实用新型内容 Utility model content
为了克服传统污水处理工艺不能有效地去除污水中的氮和磷的不足,本实用新型的目的是提供一种两级A/O—MBR脱氮除磷装置,利用该装置进行脱氮除磷时,可针对低碳氮比污水可以在不需额外投加碳源的条件下,进行高效脱氮除磷处理,而且工艺简单,运行能耗低于传统MBR,出水可达到国家回用水标准。In order to overcome the deficiency that the traditional sewage treatment process cannot effectively remove nitrogen and phosphorus in sewage, the purpose of this utility model is to provide a two-stage A/O-MBR nitrogen and phosphorus removal device. , for low carbon-to-nitrogen ratio sewage, it can perform efficient nitrogen and phosphorus removal treatment without adding additional carbon sources, and the process is simple, the operating energy consumption is lower than that of traditional MBR, and the effluent can meet the national reuse water standard.
本实用新型所提供的一种两级A/O—MBR脱氮除磷装置,包括依次连通的厌氧池、第一缺氧池、第一好氧池、第二缺氧池、第二好氧池和膜池;A two-stage A/O-MBR denitrification and phosphorus removal device provided by the utility model includes an anaerobic pool, a first anoxic pool, a first aerobic pool, a second anoxic pool, and a second anoxic pool connected in sequence. Oxygen pools and membrane pools;
所述厌氧池和第二缺氧池均与进水管相连通,所述进水管上设有进水泵;Both the anaerobic pool and the second anoxic pool are connected with a water inlet pipe, and a water inlet pump is arranged on the water inlet pipe;
所述膜池内设有膜组件,所述膜组件与出水管相连通,所述出水管上设有出水泵;所述膜池的底部设有沉淀池,所述沉淀池通过污泥混合液回流管与所述厌氧池相连通,所述污泥混合液回流管上设有回流泵。The membrane pool is provided with a membrane module, and the membrane module is connected with the outlet pipe, and the outlet pipe is provided with an outlet pump; the bottom of the membrane pool is provided with a sedimentation tank, and the sedimentation tank is refluxed through the sludge mixture. The pipe communicates with the anaerobic tank, and the sludge mixed liquid return pipe is provided with a return pump.
上述的两级A/O—MBR脱氮除磷装置中,所述进水管上设有流量调节阀,以调节进入所述厌氧池和第二缺氧池中的进入比例。In the above-mentioned two-stage A/O-MBR denitrification and phosphorus removal device, the water inlet pipe is provided with a flow regulating valve to adjust the ratio of entering the anaerobic tank and the second anoxic tank.
上述的两级A/O—MBR脱氮除磷装置中,所述沉淀池可为倒锥体形,以利于污泥混合液的沉降。In the above-mentioned two-stage A/O-MBR nitrogen and phosphorus removal device, the sedimentation tank may be in the shape of an inverted cone to facilitate the sedimentation of the sludge mixture.
上述的两级A/O—MBR脱氮除磷装置中,所述厌氧池、第一缺氧池和第二缺氧池内设有搅拌装置。In the above-mentioned two-stage A/O-MBR nitrogen and phosphorus removal device, the anaerobic tank, the first anoxic tank and the second anoxic tank are provided with stirring devices.
上述的两级A/O—MBR脱氮除磷装置中,所述第一好氧池、第二好氧池和膜池内设有曝气充氧装置。In the above-mentioned two-stage A/O-MBR nitrogen and phosphorus removal device, the first aerobic tank, the second aerobic tank and the membrane tank are provided with aeration and oxygenation devices.
上述的两级A/O—MBR脱氮除磷装置中,所述厌氧池、第一缺氧池、第一好氧池、第二缺氧池、第二好氧池和膜池均可由一个或多个单元池组成。In the above-mentioned two-stage A/O-MBR nitrogen and phosphorus removal device, the anaerobic tank, the first anoxic tank, the first aerobic tank, the second anoxic tank, the second aerobic tank and the membrane tank can be formed by Consists of one or more cell pools.
本实用新型提供的两级A/O—MBR脱氮除磷装置,具有如下优点:本实用新型将两级A/O与MBR相结合,传统的MBR工艺具有很好的去氨氮能力,能将污水种的氨氮完全硝化,而两级A/O系统具有较强的反硝化能力,两者结合提高系统对总氮降解能力,适合低碳氮比污水的处理,系统总氮去除能力强,能够确保出水总氮明显优于其他传统工艺;通过在膜池设计沉淀区,可降低了进入膜分离区混合液的污泥浓度,降低膜组件工作负荷,由于降低了膜组件区域的污泥浓度,运行期间可适当降低膜组件的曝气强度,降低MBR系统的运行能耗。The two-stage A/O-MBR denitrification and phosphorus removal device provided by the utility model has the following advantages: the utility model combines two-stage A/O and MBR, and the traditional MBR process has a good ability to remove ammonia and nitrogen, and can The ammonia nitrogen of the sewage species is completely nitrified, and the two-stage A/O system has a strong denitrification ability. The combination of the two can improve the system’s ability to degrade total nitrogen, which is suitable for the treatment of sewage with a low carbon-to-nitrogen ratio. The system has a strong ability to remove total nitrogen and can To ensure that the total nitrogen in the effluent is obviously superior to other traditional processes; by designing the sedimentation zone in the membrane tank, the sludge concentration of the mixed solution entering the membrane separation zone can be reduced, and the workload of the membrane module can be reduced. Due to the reduction of the sludge concentration in the membrane module area, During operation, the aeration intensity of the membrane module can be appropriately reduced to reduce the operating energy consumption of the MBR system.
附图说明 Description of drawings
图1为本实用新型提供的两级A/O-MBR脱氮除磷装置。Fig. 1 is a two-stage A/O-MBR nitrogen and phosphorus removal device provided by the utility model.
图中各标记如下:1厌氧池、2第一缺氧池、3第一好氧池、4第二缺氧池、5第二好氧池、6膜池、7进水管、8进水泵、9流量调节阀、10膜组件、11出水管、12沉淀池、13污泥混合液回流管、14回流泵、15曝气充氧装置、16出水泵。The marks in the figure are as follows: 1 anaerobic pool, 2 the first anoxic pool, 3 the first aerobic pool, 4 the second anoxic pool, 5 the second aerobic pool, 6 membrane pool, 7 water inlet pipe, 8 water inlet pump , 9 flow regulating valve, 10 membrane module, 11 outlet pipe, 12 sedimentation tank, 13 sludge mixed liquid return pipe, 14 return pump, 15 aeration and oxygenation device, 16 outlet pump.
具体实施方式 Detailed ways
下述实施例中所使用的实验方法如无特殊说明,均为常规方法。The experimental methods used in the following examples are conventional methods unless otherwise specified.
下述实施例中所用的材料、试剂等,如无特殊说明,均可从商业途径得到。The materials and reagents used in the following examples can be obtained from commercial sources unless otherwise specified.
本实用新型提供的两级A/O—MBR脱氮除磷装置包括依次连通的厌氧池1、第一缺氧池2、第一好氧池3、第二缺氧池4、第二好氧池5和膜池6;其中厌氧池1和第二缺氧池4均与进水管7相连通,该进水管7上设有进水泵8和流量调节阀9,以调节进入厌氧池1和第二缺氧池4中的进入比例;膜池6内设有膜组件10,该膜组件10与出水管11相连通,出水管11上设有出水泵16,将净化后的水排出;膜池6的底部设有倒锥体形的沉淀池12,可利于污泥混合液的沉降;该沉淀池12通过污泥混合液回流管13与厌氧池1相连通,该污泥混合液回流管13上设有回流泵14,用于将污泥混合液泵送至厌氧池1中;厌氧池1、第一缺氧池2和第二缺氧池4内均设有搅拌装置14;第一好氧池3、第二好氧池5和膜池6内均设有曝气充氧装置15。The two-stage A/O-MBR denitrification and phosphorus removal device provided by the utility model includes an anaerobic pool 1, a first anoxic pool 2, a first aerobic pool 3, a second anoxic pool 4, and a second anoxic pool connected in sequence. Oxygen pool 5 and membrane pool 6; Wherein the anaerobic pool 1 and the second anoxic pool 4 are all communicated with the water inlet pipe 7, and the water inlet pipe 7 is provided with an inlet water pump 8 and a flow regulating valve 9 to regulate the flow into the anaerobic pool 1 and the entering ratio in the second anoxic pool 4; the membrane pool 6 is provided with a membrane module 10, which communicates with the outlet pipe 11, and the outlet pipe 11 is provided with an outlet pump 16 to discharge the purified water The bottom of the membrane pool 6 is provided with an inverted cone-shaped settling tank 12, which can facilitate the settlement of the sludge mixed solution; the settling tank 12 is communicated with the anaerobic tank 1 through the sludge mixed solution return pipe 13, and the sludge mixed solution The return pipe 13 is provided with a return pump 14 for pumping the sludge mixture to the anaerobic tank 1; the anaerobic tank 1, the first anoxic tank 2 and the second anoxic tank 4 are equipped with stirring devices 14. The first aerobic tank 3, the second aerobic tank 5 and the membrane tank 6 are equipped with aeration and oxygenation devices 15.
本实用新型提供的脱氮除磷装置中,厌氧池1、第一缺氧池2、第一好氧池3、第二缺氧池4、第二好氧池5和膜池6均可由多个单元池组成。In the denitrification and dephosphorization device provided by the utility model, the anaerobic pool 1, the first anoxic pool 2, the first aerobic pool 3, the second anoxic pool 4, the second aerobic pool 5 and the membrane pool 6 can be formed by Composed of multiple unit pools.
使用本实用新型提供的脱氮除磷装置进行污水处理时,其流程如下:污水经进水泵8进入厌氧池1,污水中的有机底物被聚磷菌吸收并合成为PHAs储存于胞内,同时聚磷菌释放出溶解性正磷酸盐,表现为上清液的COD降低而磷浓度升高。在厌氧池1中,有机氮也被转化为氨氮。之后污水进入第一缺氧池2,反硝化菌利用污水碳源将污泥混合液回流管13从沉淀池12输送来的硝酸盐进行反硝化脱氮,同时反硝化聚磷菌在此处可利用胞内PHAs进行反硝化除磷,去除部分硝酸盐和磷。之后污水依次进入第一好氧池3和第二缺氧池7。在该工艺流程中部分原水经过原水分流管12直接进入第二缺氧池7,反硝化菌利用污水碳源将第一好氧池产生的硝酸盐进行反硝化脱氮。污水混合再自流进入第二好氧区,在此阶段,聚磷菌利用胞内PHAs迅速吸收去除溶解性的磷,COD由于好氧微生物的作用继续减少,同时硝化菌将氨氮转化为亚硝酸盐氮和硝酸盐氮,经过以上的一系列生化反应之后,污水中的氮、磷及其它污染物质已基本被去除。而最后混合液进入膜池6,膜池6污泥浓度较高,在膜池6设定了沉淀池12,部分污泥经沉淀浓缩后回流至前端工艺,通过污泥浓缩回流降低膜池污泥浓度,减小控制膜污染的曝气强度,降低运行能耗;而膜池6则起到进一步保障水质的作用,通过膜截留分离去除胶体磷等悬浮态的污染物质,最终经出水泵16抽吸排水,获得满足国家回用标准的出水。When the nitrogen and phosphorus removal device provided by the utility model is used for sewage treatment, the process is as follows: the sewage enters the anaerobic pool 1 through the water inlet pump 8, and the organic substrate in the sewage is absorbed by the phosphorus accumulating bacteria and synthesized into PHAs and stored in the cell , and at the same time the phosphorus accumulating bacteria released soluble orthophosphate, which showed that the COD of the supernatant decreased and the phosphorus concentration increased. In the anaerobic tank 1, organic nitrogen is also converted to ammonia nitrogen. Afterwards, the sewage enters the first anoxic tank 2, and the denitrifying bacteria use the sewage carbon source to carry out denitrification and denitrification of the nitrate transported by the sludge mixed liquid return pipe 13 from the sedimentation tank 12. Intracellular PHAs are used for denitrification and phosphorus removal to remove part of nitrate and phosphorus. The sewage then enters the first aerobic pool 3 and the second anoxic pool 7 in sequence. In this technological process, part of the raw water directly enters the second anoxic tank 7 through the raw water distribution pipe 12, and the denitrifying bacteria use the sewage carbon source to denitrify and denitrify the nitrate produced in the first aerobic tank. The sewage is mixed and then flows into the second aerobic zone. At this stage, the phosphorus accumulating bacteria use intracellular PHAs to quickly absorb and remove the dissolved phosphorus, and the COD continues to decrease due to the action of aerobic microorganisms. At the same time, the nitrifying bacteria convert ammonia nitrogen into nitrite Nitrogen and nitrate nitrogen, after the above series of biochemical reactions, the nitrogen, phosphorus and other pollutants in the sewage have been basically removed. Finally, the mixed solution enters the membrane pool 6, where the sludge concentration in the membrane pool 6 is relatively high, and a sedimentation tank 12 is set in the membrane pool 6, and part of the sludge is returned to the front-end process after being concentrated by sedimentation, and the sewage in the membrane pool is reduced through the sludge concentration and backflow. mud concentration, reduce the aeration intensity for controlling membrane pollution, and reduce operating energy consumption; while the membrane pool 6 plays a role in further ensuring water quality, removes suspended pollutants such as colloidal phosphorus through membrane interception and separation, and finally passes through the outlet pump 16 Suction and drainage to obtain effluent that meets national reuse standards.
在上述的处理过程中,污水水质条件为:COD含量为200至300mg/L,总氮含量为80至100mg/L,总磷含量为5至10mg/L。污泥混合液回流管的污泥混合液回流比可为200%,污泥浓度为5g/L,水力停留时间为17小时。项目进水COD:TN≈3:1,出水COD含量小于30mg/L,出水TN含量小于10mg/L,最终出水达到国家回用标准。In the above treatment process, the sewage water quality conditions are: COD content is 200 to 300 mg/L, total nitrogen content is 80 to 100 mg/L, and total phosphorus content is 5 to 10 mg/L. The return ratio of the sludge mixed solution in the sludge mixed solution return pipe can be 200%, the sludge concentration is 5g/L, and the hydraulic retention time is 17 hours. COD in the project water: TN≈3:1, COD content in the effluent is less than 30mg/L, TN content in the effluent is less than 10mg/L, and the final effluent meets the national reuse standard.
本实用新型仅设一条污泥混合液回流管,回流量可依据需要进行调整。回流比一般为100%-400%;本实用新型设两条进水管,即两点进水,部分污水通过进水管直接进入厌氧池,进水中的有机底物被聚磷菌吸收并合成为PHAs储存于胞内,同时聚磷菌释放出溶解性正磷酸盐,表现为上清液的COD降低而磷浓度升高;另一部分污水通过进水管的分流管超越部分第一缺氧池和第一好氧池直接进入第二缺氧池,为第一好氧池产生的硝氮进行反硝化提供碳源。The utility model only has one return pipe for the sludge mixed liquid, and the return flow can be adjusted according to the needs. The reflux ratio is generally 100%-400%; the utility model is equipped with two water inlet pipes, that is, two water inlet points, and part of the sewage directly enters the anaerobic pool through the water inlet pipes, and the organic substrate in the water inlet is absorbed and synthesized by phosphorus-accumulating bacteria. Because PHAs are stored in the cells, and phosphorus accumulating bacteria release soluble orthophosphate at the same time, the COD of the supernatant is reduced and the phosphorus concentration is increased; another part of the sewage passes through the diversion pipe of the water inlet pipe and surpasses part of the first anoxic pool and The first aerobic pool directly enters the second anoxic pool to provide a carbon source for denitrification of the nitrate nitrogen produced in the first aerobic pool.
本实用新型在膜池设置了沉淀池,高浓度活性污泥进入膜池后,会因为泥水比重差,部分污泥将沉入沉淀池,污泥在漏斗状的沉淀池浓缩压实,可以提高污泥回流效率,同时部分污泥被浓缩后回流可以降低膜池污泥浓度。膜池低污泥浓度可以减小膜污染的潜势,同样也可以适当降低膜曝气强度,达到节能的目的。The utility model is equipped with a sedimentation tank in the membrane pool. After the high-concentration activated sludge enters the membrane pool, part of the sludge will sink into the sedimentation tank due to the poor specific gravity of mud and water. The sludge is concentrated and compacted in the funnel-shaped sedimentation tank, which can improve Sludge return efficiency, at the same time, part of the sludge is concentrated and returned to reduce the sludge concentration of the membrane tank. The low sludge concentration in the membrane tank can reduce the potential of membrane fouling, and can also appropriately reduce the intensity of membrane aeration to achieve the purpose of energy saving.
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
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CN104058554A (en) * | 2014-07-04 | 2014-09-24 | 哈尔滨工业大学深圳研究生院 | A2O2-MBR sewage treatment process and device |
CN105217789A (en) * | 2015-10-29 | 2016-01-06 | 天津万峰环保科技有限公司 | A kind of high-efficient denitrification and dephosphorization technique being applicable to low carbon-nitrogen ratio sewage |
CN107973402A (en) * | 2017-11-28 | 2018-05-01 | 华夏碧水环保科技有限公司 | Pulling flow type AO reactors |
CN111170586A (en) * | 2020-02-24 | 2020-05-19 | 大禹环保(天津)有限公司 | Control room of water treatment integrated equipment |
CN113428978A (en) * | 2021-06-11 | 2021-09-24 | 贵州大学 | Low-carbon-source urban sewage improvement A2O-MBR (membrane bioreactor) combined process and device thereof |
CN113955851A (en) * | 2021-08-18 | 2022-01-21 | 北京工业大学 | Post-selection anoxic/aerobic internal carbon source reinforced municipal sewage deep denitrification device and method |
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
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CN104058554A (en) * | 2014-07-04 | 2014-09-24 | 哈尔滨工业大学深圳研究生院 | A2O2-MBR sewage treatment process and device |
CN105217789A (en) * | 2015-10-29 | 2016-01-06 | 天津万峰环保科技有限公司 | A kind of high-efficient denitrification and dephosphorization technique being applicable to low carbon-nitrogen ratio sewage |
CN107973402A (en) * | 2017-11-28 | 2018-05-01 | 华夏碧水环保科技有限公司 | Pulling flow type AO reactors |
CN111170586A (en) * | 2020-02-24 | 2020-05-19 | 大禹环保(天津)有限公司 | Control room of water treatment integrated equipment |
CN113428978A (en) * | 2021-06-11 | 2021-09-24 | 贵州大学 | Low-carbon-source urban sewage improvement A2O-MBR (membrane bioreactor) combined process and device thereof |
CN113955851A (en) * | 2021-08-18 | 2022-01-21 | 北京工业大学 | Post-selection anoxic/aerobic internal carbon source reinforced municipal sewage deep denitrification device and method |
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