WO2019169980A1 - 一种结合mbr的厌氧氨氧化污水处理工艺 - Google Patents

一种结合mbr的厌氧氨氧化污水处理工艺 Download PDF

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WO2019169980A1
WO2019169980A1 PCT/CN2019/073551 CN2019073551W WO2019169980A1 WO 2019169980 A1 WO2019169980 A1 WO 2019169980A1 CN 2019073551 W CN2019073551 W CN 2019073551W WO 2019169980 A1 WO2019169980 A1 WO 2019169980A1
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anaerobic ammonium
ammonium oxidation
reactor
treatment process
sewage
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French (fr)
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张显超
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上海世浦泰膜科技有限公司
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Publication of WO2019169980A1 publication Critical patent/WO2019169980A1/zh

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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
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • 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
    • 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
    • C02F1/5281—Installations for water purification using chemical agents
    • 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
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • 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
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C02F3/1273—Submerged membrane bioreactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
    • 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

Definitions

  • the invention relates to the field of sewage treatment, in particular to an anaerobic ammonium oxidation sewage treatment process combined with MBR.
  • Anammox can directly convert ammonia nitrogen and nitrite nitrogen into nitrogen under anaerobic conditions using nitrite as an electron acceptor.
  • the anaerobic ammonium oxidation process only needs to oxidize ammonia nitrogen to nitrite nitrogen in the aerobic section, thereby eliminating the subsequent oxidation of nitrite nitrogen to nitrate.
  • the nitrogen process saves about 60% of the aeration.
  • Anammox acts as a self-supporting bacteria, and its biochemical reaction eliminates all the additional organic carbon sources required for the traditional denitrification process and reduces greenhouse gas emissions.
  • the process of denitrification of industrial and municipal wastewater by anaerobic ammonium oxidation was first invented by the Delft University of Technology in the Netherlands. The process is based on the formation of granular autotrophic bacteria (anammox bacteria, Anammox), and has been applied to the lateral treatment of sewage treatment and the mainstream treatment of industrial wastewater with high water temperature, but not yet in municipal wastewater. Implemented in mainstream processing.
  • anammox bacteria are a kind of slow-growing autotrophic bacteria, and their accumulation is the core of commercial anaerobic ammonium oxidation process.
  • the influent wastewater of the anaerobic ammonium oxidation process should have a low COD or BOD 5 and suspended solids concentration values.
  • An anaerobic ammonium oxidation wastewater treatment process combined with MBR includes the following steps:
  • Sewage pretreatment After the large amount of particulate matter is removed by the coarse grid and the sand removing device, the sewage is passed to the coagulation reactor for flocculation, and the solid particulate matter is separated by the pretreated fine grid unit to make the pretreated In the sewage, the solid particle size is not more than the size of the anammox ammonia-oxidizing microparticles in the denitrification treatment step;
  • Denitrification treatment the pretreated sewage is passed to a nitrification tank for nitrification, and the nitrification tank is equipped with an aerator to incompletely oxidize ammonia nitrogen to nitrite and generate an activated sludge liquid containing residual ammonia nitrogen.
  • the activated sludge liquid containing nitrite and residual ammonia nitrogen is put into an anaerobic ammonium oxidation reactor for denitrification reaction;
  • the denitrification treated sewage is put into an MBR membrane reactor for solid-liquid separation, and the MBR membrane reactor is equipped with an aerator to oxidize nitrite to nitrate;
  • the activated sludge rich in anaerobic ammonium oxidizing bacteria particles and nitrate separated by the MBR membrane is refluxed into the anaerobic ammonium oxidation reactor as a reactant for the next denitrification treatment.
  • Adding one step of fine grid filtration in the sewage pretreatment process can effectively reduce the size of solid particles in the sewage, so that the sewage has lower COD or BOD 5 and suspended solid concentration values during denitrification treatment, so that anaerobic self Fertility can multiply.
  • the effluent treated by the anaerobic ammonium oxidation reactor is further treated with an MBR membrane, which has a relatively high concentration of suspended solids in the mixed liquor, and is compatible with the process of treating the sewage by the anaerobic ammonium oxidation process.
  • the solid-liquid separation step further includes disposing a reflow fine grid unit for controlling anaerobic on a path of refluxing the anaerobic ammonium oxidizing bacteria particles and the nitrate-containing sludge to the anaerobic ammonium
  • the use of a reflowed fine grid can limit the amount of anaerobic ammonium oxidizing bacteria in the denitrification treatment by changing the perforation or mesh size of the fine grid to limit the concentration of activated sludge that is refluxed into the anaerobic ammonium oxidation reactor.
  • the coagulation reactor is provided with a stirrer in which an inorganic salt having a flocculation effect and a high molecular polymer are placed.
  • the pre-treatment fine grid unit of the pre-treatment step adopts a drum type or a plane grid; the size of the perforation or mesh of the pre-treatment fine grid is 0.1 mm to 2.0 mm.
  • the reflowing fine grid unit adopts one or more of a drum type, a plane grid, a stepped grid or an inner inlet grille; the size of the perforation or mesh of the reflowing fine grid It is 0.1mm to 2.0mm.
  • the denitrification reaction in the anaerobic ammonium oxidation reactor converts nitrite and residual ammonia nitrogen transported in the nitrification tank into nitrogen; and the anaerobic ammonia oxidation reactor further performs refluxing nitrate-containing sludge. The process of denitrification reaction.
  • the reaction temperature of the anaerobic ammonium oxidation reactor is ⁇ 10 °C.
  • the reaction temperature of the anaerobic ammonium oxidation reactor is from 10 ° C to 35 ° C.
  • the ratio of the activated sludge in the MBR membrane tank to the anaerobic ammonium oxidation reactor is controlled by the concentration of the suspended solids in the anaerobic ammonium oxidation reactor.
  • the sewage pretreatment, the denitrification treatment, and the solid-liquid separation treatment step are continuously performed in synchronization, and the water outlet of the MBR membrane reactor continuously discharges water.
  • the anaerobic ammonium oxidation process is combined with the MBR process, and the land area can be greatly reduced. At the same time, the high concentration of anaerobic ammonium oxidizing bacteria particles in the MBR process ensures efficient operation of municipal and industrial wastewater treatment plants.
  • the anaerobic ammonia water treatment technology can be carried out under low temperature conditions.
  • the present invention can significantly reduce the required nitrate internal circulation. At the same time, the sludge return flow required in the anaerobic ammonium oxidation process is also significantly reduced.
  • FIG. 1 is a flow chart of an anaerobic ammonium oxidation wastewater treatment process of the present invention.
  • the present invention provides an anaerobic ammonium oxidation wastewater treatment process in combination with MBR according to the following steps:
  • Step a inputting the raw water pretreated by the coarse grid and the sand removing device 1 into the coagulation reactor 2 with a stirrer, and adding the inorganic salt flocculant 3 and the polymer to the coagulation reactor 2
  • the polymer flocculant 4 acts as a chemical flocculant, starts a stirrer for mechanical agitation, and destabilizes and flocculates the undissolved inorganic and organic solid materials.
  • Step b the flocculated sewage is removed by pre-treating the fine grid unit 5, and the pre-treated fine grid 6 in the pre-treated fine grid unit 5 is a rotary drum or a flat grid, and the grid The size of the perforations or mesh of the grid is between 0.1 mm and 2.0 mm.
  • the intercepted grid slag 7 is sent to a sludge treatment system for processing.
  • the pre-treated fine grid can also be selected from a stepped grille and an inner inlet grille.
  • Step c The finely sifted sewage 8 is treated by a pretreatment process, and the undissolved solid and organic matter are low in concentration, and are input into the nitrification tank 9, and the nitrification tank 9 is connected to the aerator 10.
  • the amount of aeration of the aerator 10 into the nitrification tank 9 should be less than the critical value of the oxidation of ammonia nitrogen to nitrate.
  • the concentration of activated sludge in the nitrification tank 9 is adjusted by the concentration of the suspended solids suspended solids 12 in the anaerobic ammonium oxidation reactor 11.
  • Step d an activated sludge liquid 13 containing nitrite and residual ammonia nitrogen is introduced into the anaerobic ammonium oxidation reactor 11 from the nitrification tank 9, and the anaerobic ammonium oxidation reactor 11 is preferably an anaerobic environment. Without oxygenation, it is mechanically stirred by agitator 14, wherein Anammox, an anaerobic autotrophic bacteria, uses nitrite as an electron acceptor to carry out biochemical denitrification reaction at a reaction temperature of 10 ° C to 35 ° C. The ammonia nitrogen and nitrite nitrogen in the activated sludge 13 are converted into nitrogen gas to be released, thereby achieving nitrogen removal.
  • the Anammox reaction of the anaerobic autotrophic bacteria in this step can lower the water temperature to a low temperature of 10 ° C, so that the present invention can be applied to denitrification treatment in a low water temperature environment in winter.
  • Step e the sewage enters into the MBR membrane tank 17 along with the mixed liquid suspended solids 15 which combines the membrane separation technology and the biochemical treatment technology, and filters the sludge-containing sewage in the pool through the membrane group 18, The separation of mud and water is realized, and the sludge microorganisms are intercepted, so that the concentration of activated sludge in the pool is significantly increased, and the filtration of the membrane ensures the good effluent quality.
  • the membrane group 18 is scrubbed by the membrane scrubbing gas 16 produced by the aerator in the MBR membrane tank 17, while the excess nitrite in the mixed liquor suspension 15 is oxidized to nitrate.
  • Step f The activated sludge 20 discharged from the MBR membrane tank 17 is refluxed to the anaerobic ammonium oxidation reactor 11, and the reflux ratio is determined by the suspended solid concentration value and denitrification reaction of the mixed liquid in the MBR membrane tank 17. The ratio is controlled.
  • the activated sludge 20 contains granulated anaerobic autobacteria cells which are injected back into the anaerobic ammonium oxidation reactor 11 through the process operating condition control module 21.
  • the excess sludge 22 needs to be discharged, and the excess sludge 22 is first treated by the reflux fine grid unit 23, and then partially returned to the anaerobic ammonium oxidation reactor 11
  • the type and size of the reflow fine grid 24 in the reflow fine grid unit 23 are the same as those of the pre-treated fine grid 6, wherein the perforation or mesh size may also be smaller than the size of the perforation or mesh in the pre-treated fine grid 6. .
  • the anaerobic autotrophic bacterial cell particles separated by the sludge fine grid unit 23 are returned to the anaerobic ammonium oxidation reactor 11 via the sludge reflux 25, and the residual sludge grid slag 26 is discharged to In the sludge treatment system.
  • Step g The water treated in the MBR membrane tank 17 is the filtered liquid 19, which is sucked from the membrane group 18 by a suction pump to the clear water pool for use.

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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Abstract

一种结合MBR的厌氧氨氧化污水处理工艺，包括污水预处理、脱氮处理和固液分离处理步骤，其中污水预处理步骤中采用细格栅分离技术，脱氮处理步骤中采用控制曝气器（10）的曝气量实现氨氮不完全氧化成亚硝酸盐，并通过厌氧氨氧化反应进行脱氮，固液分离处理步骤采用MBR膜对亚硝酸盐进行氧化和分离。

Description

一种结合MBR的厌氧氨氧化污水处理工艺 技术领域
本发明涉及污水处理领域，具体涉及一种结合MBR的厌氧氨氧化污水处理工艺。
背景技术
传统的脱氮除磷系统常采用多段式(厌氧、缺氧、好氧)的活性污泥组合工艺，如A2O和AO工艺等。其运行中，硝化菌、反硝化菌与聚磷菌于污泥内共存，不但存在着对碳源的竞争，还有泥龄上的矛盾，使得菌种作用效率低，曝气耗能大，工艺流程长，需要的池容和占地大。
厌氧氨氧化菌(Anammox)作为一种新的脱氮技术，可在厌氧条件下，以亚硝酸盐为电子受体，直接将氨氮和亚硝态氮转化成氮气。与传统活性污泥的硝化反硝化脱氮技术相比，厌氧氨氧化工艺只需在好氧段将氨氮氧化为亚硝态氮即可，以此免去了后续亚硝态氮氧化为硝态氮的过程，进而节省了60％左右的曝气量。同时，Anammox作为自养菌，其生化反应将传统反硝化过程所需的外加有机碳源全部省去，并减少了温室气体的排放。
以厌氧氨氧化对工业和市政污水进行脱氮的工艺，最早由荷兰代尔夫特理工大学发明。该项工艺基于会形成颗粒状的自养菌(厌氧氨氧化菌，Anammox)，且已被应用于污水处理中的侧流处理以及水温较高的工业废水主流处理，但尚未在市政污水的主流处理中实施。活性污泥中，厌氧氨氧化菌是一类生长缓慢的自养菌，其聚积是商业应用厌氧氨氧化工艺的核心。据悉，高浓度的可生化降解的有机物会使得异氧菌大量繁殖，随之影响厌氧氨氧化菌体颗粒的培养。因此，厌氧氨氧化工艺的进流污水，应具备较低的COD或BOD 5以及悬浮固体浓度值。
目前在污水处理过程中存在以下问题：
(1)厌氧氨氧水处理技术目前只应用到部分工业废水领域，在处理市政污水时存在工艺难以稳定运行，无法在低水温低浓度复杂污染物中应用的技 术问题。
(2)厌氧氨氧化工艺的进流污水需要进行预处理，传统处理方式无法达到对COD或BOD 5以及悬浮固体浓度的低数值要求。
(3)在厌氧氨氧化水处理过程中，需要大量的硝酸盐内循环，污泥的回流量大，污水处理效率差。
发明内容
本发明的目的在于，提供一种结合MBR的厌氧氨氧化污水处理工艺，解决以上技术问题。
本发明所解决的技术问题可以采用以下技术方案来实现：
一种结合MBR的厌氧氨氧化污水处理工艺，包括如下步骤：
(1)污水预处理：污水经粗格栅和除砂装置去除大颗粒物后，通入到混凝反应器中进行絮凝，经预处理细格栅单元对固体颗粒物进行分离，使预处理后的污水中，固体颗粒尺寸不大于脱氮处理步骤中厌氧氨氧化菌体微粒的尺寸；
(2)脱氮处理：预处理后的污水通入到硝化池进行硝化，所述硝化池内配有曝气器，使氨氮不完全氧化为亚硝酸盐，并产生含有残存氨氮的活性污泥液；将含有亚硝酸盐和残存氨氮的活性污泥液投入到厌氧氨氧化反应器内进行脱氮反应；
(3)固液分离处理：将脱氮处理后的污水投入到MBR膜反应器中进行固液分离，所述MBR膜反应器配有曝气器，将亚硝酸盐氧化成硝酸盐；并将MBR膜分离出的富含厌氧氨氧化菌体颗粒和硝酸盐的活性污泥回流到厌氧氨氧化反应器中，作为下次脱氮处理的反应物。
在污水预处理过程中增加一步细格栅过滤能够有效减小污水中固体颗粒的尺寸，使污水在进行脱氮处理时具备较低的COD或BOD 5以及悬浮固体浓度值，以使得厌氧自养菌能够大量繁殖。使用MBR膜对经过厌氧氨氧化反应器处理过的污水进行进一步处理，其具有相对较高的混合液悬浮固体浓度，与厌氧氨氧化工艺处理污水的流程相适应。
所述固液分离步骤还包括在富含厌氧氨氧化菌体颗粒和硝酸盐的污泥回 流到厌氧氨氧化反应器的路径上，设置一回流细格栅单元，其用于控制厌氧氨氧化菌体在厌氧氨氧化反应器中的浓度。
采用回流细格栅可以通过改变细格栅的穿孔或网眼尺寸来限制回流到厌氧氨氧化反应器中的活性污泥的浓度，从而控制脱氮处理中厌氧氨氧化菌体的数量。
所述混凝反应器内设有搅拌器，其内投放有具有絮凝效果的无机盐和高分子聚合物。
优选的，所述预处理步骤的预处理细格栅单元采用转鼓式或者平面格栅；所述预处理细格栅的穿孔或网眼的尺寸为0.1mm～2.0mm。
优选的，所述回流细格栅单元采用转鼓式、平面格栅、阶梯式格栅或内进流式格栅中的一种或多种；所述回流细格栅的穿孔或网眼的尺寸为0.1mm～2.0mm。
所述厌氧氨氧化反应器内的脱氮反应将硝化池内输送来的亚硝酸盐和残余氨氮转化为氮气；所述厌氧氨氧化反应器内还进行将回流的含硝酸盐污泥，进行反硝化反应的工序。
所述厌氧氨氧化反应器的反应温度为≥10℃。
优选的，所述厌氧氨氧化反应器的反应温度为10℃～35℃。
所述MBR膜池内的活性污泥回流至厌氧氨氧化反应器的比率，由厌氧氨氧化反应器内的混合液悬浮固体浓度控制。
由于厌氧氨氧化反应器中存在着生化平衡，需要一个稳定的混合液悬浮固体浓度，但是混合液悬浮固体浓度会随着反应进行而下降，需要MBR膜池内的活性污泥进行补充。
所述污水预处理、脱氮处理和固液分离处理步骤同步连续进行，所述MBR膜反应器的出水口连续出水。
有益效果：由于采用上述技术方案，本发明取得以下技术效果，
(1)在预处理和污泥回流工序中采用细格栅并与MBR膜工艺联动，可以大幅度提高工艺的稳定运行能力并提高处理效率。
(2)将厌氧氨氧化工艺结合MBR工艺实施，还能够大大减小用地面积。同时，MBR工艺内高浓度的厌氧氨氧化菌体颗粒，保证了市政和工业废水污水 处理厂的高效运行。
(3)使厌氧氨氧水处理技术能够在低温度条件下进行。
(4)与传统活性污泥工艺脱氮不同的是，本工艺发明能够显著地减少所需的硝酸盐内循环。同时，厌氧氨氧化工艺中所需的污泥回流量也明显缩减。
附图说明
图1为本发明的一种厌氧氨氧化污水处理工艺的流程图。
图中：1、粗格栅及除砂装置，2、带搅拌器的混凝反应器，3、无机盐絮凝剂，4、高分子聚合物絮凝剂，5、预处理细格栅单元，6、预处理细格栅，7、栅渣，8、细筛过的污水，9、硝化池，10、曝气器，11、厌氧氨氧化反应器，12、回流混合液悬浮固体，13、活性污泥液，14、搅拌器，15、混合液悬浮固体，16、膜擦洗气，17、MBR膜池，18、MBR膜组，19、滤后液，20、活性污泥，21、工艺运行条件控制模块，22、剩余污泥，23、回流细格栅单元，24、回流细格栅，25、污泥回流，26、污泥栅渣。
具体实施方式
为了使本发明实现的技术手段、创作特征、达成目的与功效易于明白了解，下面结合具体图示进一步阐述本发明。
参照图1，本发明提供了一种结合MBR的厌氧氨氧化污水处理工艺按照如下步骤进行：
步骤a：将粗格栅及除砂装置1预处理过的污水，输入到带搅拌器的混凝反应器2内，向所述混凝反应器2中投加无机盐絮凝剂3和高分子聚合物絮凝剂4作为化学絮凝剂，启动搅拌器进行机械搅拌，对未溶解的无机和有机固体物质进行脱稳和絮凝。
步骤b：经絮凝的污水通过预处理细格栅单元5去除固体，所述预处理细格栅单元5内的预处理细格栅6采用转鼓式格栅或平面格栅，且所述格栅的穿孔或网眼的尺寸大小在0.1mm～2.0mm之间。被拦截下来的栅渣7被输送到污泥处理系统中进行处理。预处理细格栅还可以选用阶梯式格栅、内进流式格栅。
步骤c：经过预处理工序处理细筛过的污水8内，未溶解的固体和有机物浓度较低，将其输入到硝化池9内，硝化池9连通有曝气器10。为了适应自养菌生化反应的需求，需要将氨氮不完全地氧化为亚硝酸盐，且避免氨氮的完全硝化。因此，曝气器10通入到硝化池9中的曝气量应小于氨氮氧化成硝酸盐的临界值。
同时，所述硝化池9内的活性污泥浓度，通过自厌氧氨氧化反应器11中的回流混合液悬浮固体12浓度进行调节。
步骤d：含有亚硝酸盐和残余氨氮的活性污泥液13，由所述硝化池9输入到厌氧氨氧化反应器11中，所述厌氧氨氧化反应器11内优选地为厌氧环境，不充氧，通过搅拌器14使之机械搅拌均匀，其中厌氧自养菌Anammox，以亚硝酸盐为电子受体，进行生化脱氮反应，反应温度为10℃～35℃，直接将所述活性污泥13中的氨氮和亚硝态氮转化成氮气释放出去，实现氮的去除。本步骤中的厌氧自养菌Anammox反应可以水温低至10℃的低温，使本发明可以适用于在冬天低水温环境下进行脱氮处理。
步骤e：污水随着混合液悬浮固体15进入到MBR膜池17内，所述MBR膜池17将膜分离技术和生化处理技术相结合，通过膜组18对池中的含泥污水进行过滤，实现泥水分离，并截留污泥微生物，使池中活性污泥浓度显著增加，同时通过膜片的过滤作用，保证了良好的出水水质。
所述MBR膜池17内通过曝气器产生的膜擦洗气16对膜组18进行擦洗，同时将所述混合液悬浮固体15中的过量亚硝酸盐氧化为硝酸盐。
步骤f：将所述MBR膜池17排出的活性污泥20回流至厌氧氨氧化反应器11中，回流比的大小由所述MBR膜池17内的混合液悬浮固体浓度值和反硝化反应比率进行控制。
活性污泥20中含有呈颗粒状的厌氧自养菌菌体，这部分污泥经过工艺运行条件控制模块21注入回所述厌氧氨氧化反应器11内。根据生化系统物质平衡理论，为了维持系统中的混合液悬浮固体浓度，需要排出剩余污泥22，剩余污泥22先通过回流细格栅单元23处理，再部分回流至厌氧氨氧化反应器11中，所述回流细格栅单元23内回流细格栅24的类型及结构尺寸与预处理细格栅6一致，其中穿孔或网眼尺寸也可以小于预处理细格栅6中穿孔或 网眼的尺寸。
通过所述污泥细格栅单元23筛离出的厌氧自养菌菌体菌体颗粒，经污泥回流25至厌氧氨氧化反应器11内，残余的污泥栅渣26则排放到污泥处理系统中。
步骤g：在所述MBR膜池17内处理后的水即为滤后液19，由抽吸泵从膜组18中抽吸到清水池备用。
以上显示和描述了本发明的基本原理、主要特征和本发明的优点。本行业的技术人员应该了解，本发明不受上述实施例的限制，上述实施例和说明书中描述的只是说明本发明的原理，在不脱离本发明精神和范围的前提下，本发明还会有各种变化和改进，这些变化和改进都落入要求保护的本发明范围内。本发明要求保护范围由所附的权利要求书及其等效物界定。

Claims (10)

  1. 一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，包括如下步骤：
    (1)污水预处理：污水经粗格栅和除砂装置去除大颗粒物后，通入到混凝反应器中进行絮凝，经预处理细格栅单元对固体颗粒物进行分离，使预处理后的污水中，固体颗粒尺寸不大于脱氮处理步骤中厌氧氨氧化菌体微粒的尺寸；
    (2)脱氮处理：预处理后的污水通入到硝化池进行硝化，所述硝化池内配有曝气器，使氨氮不完全氧化为亚硝酸盐，并产生含有残存氨氮的活性污泥液；将含有亚硝酸盐和残存氨氮的活性污泥液投入到厌氧氨氧化反应器内进行脱氮反应；
    (3)固液分离处理：将脱氮处理后的污水投入到MBR膜反应器中进行固液分离，所述MBR膜反应器配有曝气器，将亚硝酸盐氧化成硝酸盐；并将MBR膜分离出的富含厌氧氨氧化菌体颗粒和硝酸盐的活性污泥回流到厌氧氨氧化反应器中，作为下次脱氮处理的反应物。
  2. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述固液分离步骤还包括在富含厌氧氨氧化菌体颗粒和硝酸盐的污泥回流到厌氧氨氧化反应器的路径上，设置一回流细格栅单元，其用于控制厌氧氨氧化菌体在厌氧氨氧化反应器中的浓度。
  3. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述混凝反应器内设有搅拌器，其内投放有具有絮凝效果的高分子聚合物和无机盐。
  4. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述预处理步骤的预处理细格栅单元采用转鼓式或者平面格栅；所述预处理细格栅的穿孔或网眼的尺寸为0.1mm～2.0mm。
  5. 根据权利要求2所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述回流细格栅单元采用转鼓式、平面格栅、阶梯式格栅或内进流式格栅中的一种或多种；所述回流细格栅的穿孔或网眼的尺寸为0.1mm～2.0mm。
  6. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述厌氧氨氧化反应器内的脱氮反应将硝化池内输送来的亚硝酸盐和残余氨氮转化为氮气；所述厌氧氨氧化反应器内还进行将回流的含硝酸盐污泥，进行反硝化反应的工序。
  7. 根据权利要求1至6任一项所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述厌氧氨氧化反应器的反应温度≥10℃。
  8. 根据权利要求7所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述厌氧氨氧化反应器的反应温度为10℃～35℃。
  9. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，所述MBR膜池内的活性污泥回流至厌氧氨氧化反应器比率，由厌氧氨氧化反应器内混合液悬浮固体浓度控制。
  10. 根据权利要求1所述的一种结合MBR的厌氧氨氧化污水处理工艺，其特征在于，污水预处理、脱氮处理和固液分离处理步骤同步连续进行，所述MBR膜反应器的出水口连续出水。
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111115973A (zh) * 2020-01-16 2020-05-08 乐山市净源水处理设备有限公司 一种多级兼氧膜生物污水处理装置
CN111533363A (zh) * 2020-04-03 2020-08-14 北京博泰至淳生物科技有限公司 一种实现原位提高处理规模的污水处理方法及系统
CN112093983A (zh) * 2020-09-14 2020-12-18 陕西新泓水艺环境科技有限公司 污水处理装置和污水处理方法
CN112142204A (zh) * 2020-09-23 2020-12-29 沈阳大学 一种富集培养厌氧氨氧化菌处理污水的方法
CN112321081A (zh) * 2020-10-29 2021-02-05 李同霞 一种工业污水处理工艺
CN113264586A (zh) * 2021-06-02 2021-08-17 知和环保科技有限公司 一种处理硝酸盐废水的mbr工艺
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CN114262038A (zh) * 2021-11-15 2022-04-01 中国电建集团北京勘测设计研究院有限公司 一种用于网格絮凝池的自动冲洗与排泥装置

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2900509Y (zh) * 2006-06-08 2007-05-16 浙江大学 膜－厌氧氨氧化生物反应器
US20110207061A1 (en) * 2009-04-28 2011-08-25 Cantwell Brian J Microbial production of nitrous oxide coupled with chemical reaction of gaseous nitrous oxide
CN103539319A (zh) * 2013-10-31 2014-01-29 华北电力大学 一种垃圾渗滤液处理装置
CN203545786U (zh) * 2013-10-22 2014-04-16 黎明兴技术顾问股份有限公司 含氨氮废水处理设备
CN106430576A (zh) * 2016-09-07 2017-02-22 北京化工大学 一种高效脱氮的厌氧氨氧化膜生物反应系统及方法
CN107739094A (zh) * 2017-10-13 2018-02-27 中联环股份有限公司 一种高效脱氮反应系统及方法
CN208327522U (zh) * 2018-03-09 2019-01-04 上海世浦泰膜科技有限公司 一种结合mbr的厌氧氨氧化污水处理系统

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2542507A4 (en) * 2010-03-03 2013-11-20 Liquid Waste Treat Systems Ltd ADJUSTMENT OF A REACTOR
WO2012019310A1 (en) * 2010-08-13 2012-02-16 Anaergia Inc. Treatment of municipal wastewater with anaerobic digestion
CN103693807B (zh) * 2013-12-13 2015-05-13 重庆大学 一种基于厌氧氨氧化处理榨菜废水的组合方法
CN106365373A (zh) * 2015-07-24 2017-02-01 王玮 处理市政污泥厌氧消化液的方法及其设备
CN107555600A (zh) * 2017-09-28 2018-01-09 樊忠芳 一种污水处理系统

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2900509Y (zh) * 2006-06-08 2007-05-16 浙江大学 膜－厌氧氨氧化生物反应器
US20110207061A1 (en) * 2009-04-28 2011-08-25 Cantwell Brian J Microbial production of nitrous oxide coupled with chemical reaction of gaseous nitrous oxide
CN203545786U (zh) * 2013-10-22 2014-04-16 黎明兴技术顾问股份有限公司 含氨氮废水处理设备
CN103539319A (zh) * 2013-10-31 2014-01-29 华北电力大学 一种垃圾渗滤液处理装置
CN106430576A (zh) * 2016-09-07 2017-02-22 北京化工大学 一种高效脱氮的厌氧氨氧化膜生物反应系统及方法
CN107739094A (zh) * 2017-10-13 2018-02-27 中联环股份有限公司 一种高效脱氮反应系统及方法
CN208327522U (zh) * 2018-03-09 2019-01-04 上海世浦泰膜科技有限公司 一种结合mbr的厌氧氨氧化污水处理系统

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3747836A4 *

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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