WO2023123145A1 - Nouvel appareil de réaction de processus d'oxydation anaérobie de l'ammonium à grand cycle et à écoulement continu et procédé de commande en temps réel - Google Patents

Nouvel appareil de réaction de processus d'oxydation anaérobie de l'ammonium à grand cycle et à écoulement continu et procédé de commande en temps réel Download PDF

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Publication number
WO2023123145A1
WO2023123145A1 PCT/CN2021/142782 CN2021142782W WO2023123145A1 WO 2023123145 A1 WO2023123145 A1 WO 2023123145A1 CN 2021142782 W CN2021142782 W CN 2021142782W WO 2023123145 A1 WO2023123145 A1 WO 2023123145A1
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reaction tank
pna
tank
monitor
water distribution
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PCT/CN2021/142782
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English (en)
Chinese (zh)
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彭永臻
王聪
张树军
戚伟康
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北京工业大学
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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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • 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
    • C02F2209/14—NH3-N
    • 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
    • C02F2209/15—N03-N
    • 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
    • C02F2209/22—O2
    • 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
    • C02F2209/38—Gas flow rate
    • 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
    • C02F2209/44—Time
    • 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
    • C02F2303/14—Maintenance of water treatment installations

Definitions

  • the invention relates to a sewage biochemical treatment device and method, belonging to the technical field of sewage biological treatment, in particular to a novel continuous flow large cycle anaerobic ammonium oxidation process reaction device and a real-time control method.
  • the application of the anammox process is mainly in the form of carrier biofilm and granular sludge.
  • the carrier biofilm can achieve a good film-hanging effect and realize the retention of anammox bacteria in the reaction device, but Its main application is the integrated anammox process. Its application in the two-stage anammox process is limited by the lack of a better stirring form, resulting in the pollutants in the sewage and the carrier biofilm.
  • the granular sludge anammox oxidation process does not require a carrier, and the granular sludge-like anammox bacteria have good settling properties, can be effectively retained in the reactor, and have high impact load resistance. They can be used as the preferred sludge for project start-up inoculation, but Its cultivation is difficult, and the world's first granular sludge anaerobic ammonium oxidation project has been started for as long as 2.5 years; in the current granular sludge anaerobic ammonium oxidation process, the formation of granular sludge is mainly by aeration And the backflow of a large proportion of liquid provides shear force, consumes a lot of electric energy, and the control conditions are difficult.
  • Anammox process is currently recognized as the most economical and efficient wastewater denitrification technology, but the above two problems: (1) It is difficult to obtain a good mixed mass transfer effect in biofilm process, and the engineering inoculation is difficult and costly, (2) ) Granular sludge is difficult to start quickly, the power consumption is large, and the control conditions are difficult, which seriously restricts the engineering process of the anammox process.
  • the purpose of the present invention is to solve the above technical problems, and propose a novel continuous-flow large-circulation anaerobic ammonium oxidation process reaction device and a real-time control method.
  • the reaction device of the present invention can realize continuous operation, simple structure, convenient operation, no stirring and mixing equipment, and maintenance
  • the cost is low, the circulation volume in the system is as high as 20-200 times, and the rising flow rate is 5-30m/h, which effectively realizes the full mixing and mass transfer of the anaerobic ammonium oxidation carrier biofilm and sewage, and promotes the rapid growth of suspended microorganisms in the pool. of granulation.
  • the first aspect of the present invention provides a novel continuous flow large cycle anaerobic ammonium oxidation process reaction device, its structure is shown in accompanying drawing 1, it is characterized in that:
  • the reaction device includes a PDA reaction tank, an aeration tank, a PNA reaction tank, an online DO monitor I, an online DO monitor II, an online DO monitor III, an online ammonia nitrogen monitor, an online nitrate nitrogen monitor, a blower, and a gas regulator.
  • the PDA reaction tank, aeration tank, and PNA reaction tank are arranged in sequence, and water distribution pipes are arranged at the bottom; the PDA reaction tank and the aeration tank are connected through the connecting pipe I, and the aeration tank and the PNA reaction tank are connected through the connecting pipe II;
  • the PNA reaction tank is connected to the water inlet pipe at the front end of the PDA reaction tank through the connecting pipe III; the aeration tank is connected to the blower, and the aeration tank is adjusted through the aerator and the gas volume adjustment flowmeter; the PNA reaction tank is connected to the outlet pipe.
  • the sewage in the water inlet pipe is mixed with the liquid returned in the connecting pipe III, and enters the bottom area of the PDA reaction tank together through the water distribution pipe;
  • the water from the upper part of the PDA reaction tank flows through the connecting pipe I, passes through the water distribution pipe, and enters the aeration tank together
  • the upper part of the aeration tank flows through the connecting pipe II through the water distribution pipe, and enters the bottom area of the PNA reaction tank together;
  • the upper circulating liquid of the PNA reaction tank flows through the connecting pipe III to mix with the sewage in the inlet pipe, and the outlet water is passed through the outlet pipe emission;
  • the reaction device is equipped with a real-time control system, and the PNA reaction pool is equipped with an online DO monitor I, an online DO monitor II, an online DO monitor III, an online ammonia nitrogen monitor, and an online nitrate nitrogen monitor.
  • the data of the monitor is fed back to the gas regulating flow meter according to the control program to realize the adjustment of the aeration volume.
  • the shape of the PDA reaction tank, aeration tank, and PNA reaction tank can be a cube, a cylinder or an elliptical cylinder, etc., and other shapes that are improved according to the method described in the patent of the present invention are also included.
  • the water distribution pipe is provided with one or more main water distribution pipes and branch pipes, with the middle plane of the pipe as the reference, only on the same horizontal plane on one side of the pipe, uniform water distribution pipes with an angle of 40 to 50 degrees are uniformly opened. Holes, the aperture and quantity of water distribution holes should be set according to the actual situation.
  • the on-line DO monitor I, on-line DO monitor II, and on-line DO monitor III are respectively located in the lower, middle and upper parts of the side wall of the PNA reaction tank, and their setting points are respectively located at 1/6-6 of the longitudinal height of the tank body. 1/4, 1/2 and 3/4.
  • the second aspect of the present invention provides a novel continuous-flow large-cycle anammox process real-time control method, the method adopts the described novel continuous-flow large-cycle anammox reaction device, comprising the following steps:
  • Inoculation sludge PDA reaction tank is inoculated with short-range denitrification floc sludge with stable performance and cultivated anaerobic ammonium oxidation floc sludge or carrier biofilm, the volume ratio is 1:1, so that the concentration of mixed sludge in the tank At 4-8g/L; the PNA reaction tank is inoculated with short-range nitrification floc sludge with stable performance and cultivated anaerobic ammonium oxidation floc sludge or carrier biofilm, the volume ratio is 1:1, so that the mixed sludge concentration in the tank At 4 ⁇ 8g/L;
  • the sewage in the water inlet pipe is mixed with the backflow liquid in the connecting pipe III, and enters the bottom area of the PDA reaction tank evenly through the water distribution pipe installed downward in the direction of the water distribution hole, with an average sludge concentration of 4-8g/L;
  • the short-range denitrifying bacteria use the organic matter in the sewage to reduce the nitrate nitrogen in the backflow liquid in the connecting pipe III to nitrite nitrogen, and the newly formed nitrite nitrogen and ammonia nitrogen in the sewage are under the action of anammox bacteria
  • the reaction generates nitrogen, which is discharged into the air;
  • the water from the upper part of the aeration tank flows through the connecting pipe II through the water distribution pipe installed downwards through the water distribution hole, and enters the bottom area of the PNA reaction tank together; the average sludge concentration is 4-8g/L;
  • the pollutant ammonia nitrogen is partially oxidized to nitrite nitrogen, and the newly formed nitrite nitrogen and the remaining ammonia nitrogen in the sewage react to form nitrogen gas under the action of anammox bacteria, which is discharged into the air;
  • the circulation ratio of the circulating liquid in the upper part of the PNA reaction pool is 20-200 times.
  • the flow rate of the water distribution hole on the water distribution pipe is controlled at 60-300m/h; the liquid ascending flow rate in the PDA reaction tank and the PNA reaction tank is 5-30m/h, and the median diameter of the suspended microorganisms in the tank is 50-800 ⁇ m.
  • the dissolved oxygen in the PNA reaction tank is 0.1-0.5 mg/L.
  • the volume ratio of the PDA reaction tank, aeration tank and PNA reaction tank is 1:0.1-1:0.5-1.5, and the hydraulic retention time is 0.5-16h.
  • control box collects the data of the online monitor, and feeds back to the gas regulating flow meter according to the control program to realize the regulation of the aeration amount.
  • control program settings are as follows:
  • Short-range denitrification/anammox can be combined with short-range nitrification/anammox and realized in the same system, which can give full play to the advantages of anammox process, achieve higher nitrogen removal efficiency, save exposure Reduce gas energy consumption, reduce greenhouse gas emissions, reduce sludge production, and reduce chemical consumption;
  • Short-range denitrifying bacteria and anammox bacteria are the dominant species in the PDA reaction tank.
  • the short-range denitrifying bacteria can use the carbon source in the raw water to reduce the nitrate nitrogen produced by anammox to nitrite nitrogen. Then improve the theoretical denitrification efficiency of the anammox process;
  • the present invention can achieve up to 20-200 times the circulation rate and 5-30m/h ascending flow rate, can solve the problem of poor mixed mass transfer effect of the carrier biofilm anaerobic ammonium oxidation process, and can realize the anaerobic ammonium oxidation carrier biological Fully mixed mass transfer of membrane and sewage; it can solve the problems of long start-up period, large power consumption and difficult control of granular sludge anaerobic ammonium oxidation process, and can promote the rapid granulation of suspended microorganisms in the tank;
  • the microorganisms in the reaction device of the present invention are mainly granular sludge, which has strong resistance to water quality and water volume impact loads, good settling performance, and can be effectively retained in the reactor without the need for subsequent mud-water separation units, reducing the pool capacity and infrastructure costs of structures .
  • the reaction device of the present invention can realize continuous operation, has a simple structure, is convenient to operate, has no stirring and mixing equipment, and has low maintenance cost.
  • the invention is environmentally friendly, economical and efficient, and provides a new implementation scheme for the engineering of the anaerobic ammonium oxidation process.
  • Fig. 1 is the structural representation of the novel continuous flow large cycle anaerobic ammonium oxidation process reaction device of the present invention
  • Fig. 1 is the schematic diagram of the structure and principle of the embodiment of the novel continuous flow large cycle anaerobic ammonium oxidation process reaction device provided by the present invention
  • the reaction device comprises a PDA reaction tank 1, an aeration tank 2, a PNA reaction tank 3, and an online DO monitor I3.1, online DO monitor II3.2, online DO monitor III3.3, online ammonia nitrogen monitor 3.4, online nitrate nitrogen monitor 3.5, blower 4, gas regulating flowmeter 4.1, aerator 4.2, water distribution pipe 5 , water inlet pipe 6, connecting pipe I7, connecting pipe II8, connecting pipe III9, outlet pipe 10 and control box 11.
  • PDA reaction tank 1, aeration tank 2, and PNA reaction tank 3 are arranged in sequence, and water distribution pipes 5 are arranged at the bottom; PDA reaction tank 1 and aeration tank 2 are connected through connecting pipe I7, and aeration tank 2 reacts with PNA
  • the pools 3 are connected through the connecting pipe II8; the PNA reaction pool 3 is connected with the water inlet pipe 6 at the front end of the PDA reaction pool 1 through the connecting pipe III9;
  • the aeration tank 2 is used for aeration adjustment; the PNA reaction tank 3 is connected with the outlet pipe 10 .
  • the sewage in the water inlet pipe 6 is mixed with the liquid returned in the connecting pipe III9, and enters the bottom area of the PDA reaction tank 1 together through the water distribution pipe 5; , and enter the bottom area of the aeration tank 2 together; the water from the upper part of the aeration tank 2 flows through the connecting pipe II8 through the water distribution pipe 5, and enters the bottom area of the PNA reaction tank 3 together; the circulating liquid in the upper part of the PNA reaction tank 3 flows through the connecting pipe III9 is mixed with the sewage in the inlet pipe 6, and the outlet water is discharged from the outlet pipe 10;
  • the reaction device is provided with a real-time control system
  • the PNA reaction pool 3 is provided with an online DO monitor I 3.1, an online DO monitor II 3.2, an online DO monitor III 3.3, an online ammonia nitrogen monitor 3.4, and an online nitrate nitrogen monitor.
  • the monitoring instrument 3.5 collects the data of the online monitoring instrument by the control box 11, and feeds back to the gas regulating flowmeter 4.1 according to the control program to realize the adjustment of the aeration volume.
  • the shape of the PDA reaction tank 1, the aeration tank 2, and the PNA reaction tank 3 can be cube, cylinder or elliptical cylinder, etc., and other shapes improved according to the method described in the patent of the present invention are also included.
  • the water distribution pipe 5 is provided with one or more main water distribution pipes and branch pipes, with the middle plane of the pipe as the reference, only on the same horizontal plane on one side of the pipe, there are uniform water distribution holes with an oblique direction of 40-50 degrees.
  • the aperture and quantity of the water distribution holes should be set according to the actual situation.
  • the on-line DO monitor I3.1, on-line DO monitor II3.2, and on-line DO monitor III3.3 are respectively located in the lower, middle and upper parts of the side walls of the PNA reaction tank 3, and their setting points are respectively at the longitudinal height of the tank body. 1/6 ⁇ 1/4, 1/2 and 3/4.
  • the method of using the above device to treat low carbon nitrogen ratio sewage is as follows:
  • a real-time control method for the reaction of a novel continuous-flow large-circulation anaerobic ammonium oxidation process adopts the described novel continuous-flow large-circulation anaerobic ammonium oxidation process reaction device, comprising the following steps:
  • Inoculation sludge PDA reaction tank 1 is inoculated with short-range denitrification floc sludge with stable performance and cultivated anaerobic ammonium oxidation floc sludge or carrier biofilm, the volume ratio is 1:1, so that the sludge mixed in the tank The concentration is 4-8g/L; PNA reaction tank 3 is inoculated with short-range nitrification floc sludge with stable performance and cultivated anammox floc sludge or carrier biofilm, the volume ratio is 1:1, so that the mixed sewage in the tank The mud concentration is 4 ⁇ 8g/L;
  • the outlet water from the upper part of the aeration tank 2 flows through the connecting pipe II8 through the water distribution pipe 5 installed downwards through the water distribution hole, and enters the bottom area of the PNA reaction tank 3 together; the average sludge concentration is 4-8g/L; short-range nitrifying bacteria
  • the pollutant ammonia nitrogen in the sewage is partially oxidized to nitrite nitrogen, and the newly formed nitrite nitrogen and the remaining ammonia nitrogen in the sewage react to form nitrogen gas under the action of anammox bacteria, which is discharged into the air;
  • the circulation ratio of the circulating liquid in the upper part of the PNA reaction pool 3 is 20-200 times.
  • the flow rate of the water distribution holes on the water distribution pipe 5 is controlled at 60-300m/h; the liquid ascending flow rate in the PDA reaction tank 1 and the PNA reaction tank 3 is 5-30m/h, and the suspended microorganisms in the tanks are at a median
  • the diameter is 50-800 ⁇ m.
  • the dissolved oxygen in the PNA reaction tank 3 is 0.1-0.5 mg/L.
  • the volume ratio of the PDA reaction tank 1, the aeration tank 2 and the PNA reaction tank 3 is 1:0.1-1:0.5-1.5, and the hydraulic retention time is 0.5-16h.
  • the control box 11 collects the data of the on-line monitor, and feeds back to the gas regulating flow meter 4.1 according to the control program to realize the regulation of the aeration rate.
  • the specific control program settings are as follows:
  • the sludge in the PDA reaction tank and the PNA reaction tank is uniformly mixed, the sludge concentration is maintained at 6-7g/L, the rising flow rate is 6m/h, and the median diameter of microorganisms is 80 ⁇ m; the PDA reaction tank, aeration tank and PNA reaction tank The volume ratio is 1:0.8:1; the hydraulic retention time is 12h; the sludge is not actively discharged; the initial aeration volume of the aeration tank is set to 9L/(m 2 ⁇ s), and the circulation multiple of the circulating liquid is 30 times in the PNA reaction tank Dissolved oxygen is controlled at 0.2-0.5mg/L, and the aeration rate is adjusted according to the set procedure according to the dissolved oxygen in the PNA reaction tank and the readings of the on-line monitor.
  • the effluent COD is within 50mg/L
  • the effluent NH 4 + -N is within 2mg/L
  • the effluent TN is within

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  • Biodiversity & Conservation Biology (AREA)
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  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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Abstract

L'invention concerne un appareil de réaction de processus d'oxydation anaérobie de l'ammonium à grand cycle et à écoulement continu, qui comprend un réservoir de réaction PDA (1), un réservoir d'aération (2) et un réservoir de réaction ANP (3) disposés en séquence, qui peut fonctionner en continu et dont la structure est simple, le fonctionnement pratique, exempt de dispositif d'agitation et de mélange, et dont le coût d'entretien est peu élevé. En utilisant le procédé de commande en temps réel de l'appareil, la circulation peut être multipliée par 20 à 200 et la vitesse d'écoulement ascendante peut atteindre 5 à 30 m/h ; la difficulté liée aux mauvais effets de mélange et de transfert de masse d'un processus d'oxydation anaérobie de l'ammoniac pour une membrane biologique de support peut être résolue, et un mélange et un transfert de masse complets de la membrane biologique de support soumise à l'oxydation anaérobie de l'ammoniac et des eaux usées peuvent être réalisés ; les micro-organismes en suspension dans le réservoir sont rapidement granulés, et les micro-organismes dans l'appareil de réaction sont principalement des boues granuleuses, dont la qualité de l'eau et la résistance à la charge d'impact de la quantité d'eau sont élevées et dont la performance de décantation est bonne, et qui peuvent être efficacement retenues dans le réacteur. La dénitrification rapide/oxydation anaérobie de l'ammoniac et la nitrification rapide/oxydation anaérobie de l'ammoniac sont combinées et réalisées dans un même système, les avantages du processus d'oxydation anaérobie de l'ammoniac sont pleinement exploités, et une nouvelle solution de mise en œuvre est fournie pour l'ingénierie du processus d'oxydation anaérobie de l'ammoniac.
PCT/CN2021/142782 2021-12-29 2021-12-30 Nouvel appareil de réaction de processus d'oxydation anaérobie de l'ammonium à grand cycle et à écoulement continu et procédé de commande en temps réel WO2023123145A1 (fr)

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CN202111624902.9A CN114180722A (zh) 2021-12-29 2021-12-29 新型连续流大循环厌氧氨氧化工艺反应装置及实时控制方法
CN202111624902.9 2021-12-29

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CN109160606A (zh) * 2018-08-21 2019-01-08 海南大学 一种城市污水产甲烷及高效深度脱氮的方法
CN112299560A (zh) * 2020-11-12 2021-02-02 北京城市排水集团有限责任公司 连续流反硝化除磷串联厌氧氨氧化耦合内源反硝化的污水处理系统与方法

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103922540A (zh) * 2014-04-11 2014-07-16 北京工业大学 Apo/生物接触氧化短程硝化耦合厌氧氨氧化自养脱氮三污泥装置及方法
JP2016016347A (ja) * 2014-07-07 2016-02-01 新日鐵住金株式会社 生物学的窒素除去方法
CN104556376A (zh) * 2014-11-29 2015-04-29 北京工业大学 基于短程反硝化提供亚硝酸盐的城市污水生物除磷自养脱氮方法
CN105461178A (zh) * 2016-01-09 2016-04-06 北京工业大学 短程硝化-厌氧氨氧化后接短程反硝化-厌氧氨氧化处理城市污水的系统和方法
CN105836885A (zh) * 2016-06-04 2016-08-10 北京工业大学 一种低碳源城市污水深度脱氮的方法
CN106115915A (zh) * 2016-07-10 2016-11-16 北京工业大学 低c/n比城市生活污水短程反硝化/短程硝化厌氧氨氧化生物膜工艺的装置与方法
CN108640279A (zh) * 2018-05-25 2018-10-12 北京工业大学 一种连续流短程硝化-厌氧氨氧化工艺的实时调控装置及方法
CN109160606A (zh) * 2018-08-21 2019-01-08 海南大学 一种城市污水产甲烷及高效深度脱氮的方法
CN112299560A (zh) * 2020-11-12 2021-02-02 北京城市排水集团有限责任公司 连续流反硝化除磷串联厌氧氨氧化耦合内源反硝化的污水处理系统与方法

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