WO2021223377A1 - 低温下分段进水多级缺/好氧的污水生物脱氮处理方法 - Google Patents

低温下分段进水多级缺/好氧的污水生物脱氮处理方法 Download PDF

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WO2021223377A1
WO2021223377A1 PCT/CN2020/124101 CN2020124101W WO2021223377A1 WO 2021223377 A1 WO2021223377 A1 WO 2021223377A1 CN 2020124101 W CN2020124101 W CN 2020124101W WO 2021223377 A1 WO2021223377 A1 WO 2021223377A1
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stage
reactor
aerobic
anoxic
reaction unit
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French (fr)
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毕学军
周小琳
宋鹏
王晓东
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青岛理工大学
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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
    • C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
    • 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
    • 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
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic 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
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen
    • 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
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/043—Treatment of partial or bypass streams
    • 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
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • 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
    • C02F2301/10—Temperature conditions for biological treatment
    • 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
    • C02F3/08—Aerobic processes using moving contact bodies

Definitions

  • the invention relates to a method for sewage treatment through the functionalization of biofilms in sub-intake multi-stage anoxic/aerobic combined reaction zones, and belongs to the technical field of sewage treatment.
  • the traditional single-stage or multi-stage anoxic/aerobic (A/O) process based on activated sludge requires a longer sludge age and theoretical hydraulic retention time to ensure
  • the number of nitrifying bacteria in the activated sludge needs to be increased by increasing the aeration rate to maintain a high level of dissolved oxygen to maintain the activity of the nitrifying bacteria, which not only requires a large biochemical reactor tank capacity, which leads to large investment in civil engineering, but also high
  • the amount of aeration and long hydraulic retention time lead to high energy consumption for the operation of the sewage treatment system, and its high investment and high energy consumption are contrary to the current state of the country's green production and living development mode.
  • the existing activated sludge method single-stage or multi-stage A/O process is the cycle operation reaction of activated sludge in an anoxic and aerobic alternate environment.
  • This activated sludge process system cannot realize the functional design of partitions.
  • the traditional single-stage or multi-stage A/O process wastewater biological denitrification method based on activated sludge faces technical problems such as the restrictive bottleneck of low-temperature nitrification and low biological denitrification efficiency.
  • the present invention proposes a multi-stage anoxic/aerobic sewage biological denitrification treatment method under low temperature, which can solve the low temperature in winter Under conditions (6 ⁇ 15°C), urban sewage treatment generally has the problems of low-temperature nitrification restrictive bottleneck and low denitrification utilization efficiency of biodegradable organic matter in raw water, which can meet the high-standard discharge requirements of different regions, especially under low-temperature conditions.
  • the multi-stage anoxic/aerobic sewage biological denitrification treatment method of the present invention adopts the following technical schemes.
  • Continuous flow operation mode is adopted. After primary treatment (the effluent from the sedimentation tank), the raw water enters the first-stage A/O reaction unit and the second-stage A/O reaction unit from two locations respectively; the first-stage A/O reaction unit The outflow from the water outlet returns to the water inlet of the unit with a reflux ratio of 50% to 200%; the outflow from the water outlet of the second-stage A/O reaction unit returns to the water inlet of the unit with a reflux ratio of 50% to 200%; The effluent from the water outlet end of the third-stage A/O reaction unit is clarified and separated and the water is effluent;
  • the first-stage A/O reaction unit includes A1 anoxic raw water carbon source denitrification functional reactor, A2 anoxic raw water carbon source denitrification functional reactor, and O3 aerobic organics degradation functional reactor connected in sequence Four biofilm reactors with O4 aerobic nitrification functional reactor;
  • the second-stage A/O reaction unit includes an A5 anoxic raw water carbon source denitrification functionalized reactor, an A6 anoxic raw water carbon source denitrification functionalized reactor, and an O7 aerobic organics degradation functionalized reactor connected in sequence Four biofilm reactors with O8 aerobic nitrification functional reactor;
  • the third-stage A/O reaction unit includes two biofilm reactors, which are connected in turn, A9 anoxic exogenous carbon source denitrification functionalized reactor and O10 aerobic residual organics degradation and nitrification functionalized reactor; A9 lacks A carbon source dosing device is installed in the denitrification functionalized reactor with an oxygen external carbon source;
  • the facultative heterotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier uses the raw water carbon source to denitrify to remove nitrate nitrogen; in the first stage In the reaction unit and the second-stage reaction unit, the aerobic heterotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the aerobic reactor that mainly degrades organic matter removes the organic matter in the sewage; The aerobic autotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the oxygen reactor removes organic nitrogen and ammonia nitrogen in the sewage; in the third-stage reaction unit in accordance with the final treatment effluent total nitrogen emission target requirements, through the addition of external sources The natural carbon source removes nitrate nitrogen, so that the organic matter, total nitrogen and ammonia nitrogen of the final treated water can reach the water quality index.
  • the reflux ratio of the outflow from the water outlet end of the first-stage A/O reaction unit and the second-stage A/O reaction unit to the water inlet end of the unit is 50% to 200%.
  • the total hydraulic residence time of the three-stage A/O reaction unit is 6-12 hours (h), and the maximum flow velocity of the flow section of each reactor is not higher than 35 meters/hour (m/h).
  • An agitator is provided in each of the anoxic reactors (A1, A2, A5, A6, A9), and the filling rate of the suspended biofilm carrier suitable for the attachment and growth of microorganisms in an anoxic environment is not more than 55%.
  • Each aerobic reactor (O3, O4, O7, O8, O10) is equipped with an aeration device, and the filling rate of the suspended biofilm carrier suitable for the attachment and growth of microorganisms is not more than 66%.
  • All the reactors are equipped with an inlet water distribution device and an outlet water collection device.
  • the inlet water distribution device adopts the upper part of the weir or the submerged type near the bottom of the reactor side to distribute water.
  • the corresponding outlet water collection device is intercepted by the filler After the screen, the water is collected close to the bottom of the side of the reactor or close to the top of the side of the reactor.
  • the suspended biofilm carrier interception device can adopt a vertical vertical or horizontal cylindrical screen; when a vertical vertical screen is used, the opening surface of the screen is located at the position of 35%-65% of the effective water depth of the pool; adopts horizontal In the case of horizontal cylindrical screens, the installation height of the cylindrical screens is at 35%-65% of the effective water depth of the pool body.
  • the maximum intercepting screen sieving flow rate is not more than 60m/h, and the opening rate of the intercepting screen is not more than 50%; the screen aperture of the intercepting screen is 50% to 60% of the diameter of the suspended biofilm carrier.
  • the A1 anoxic raw water carbon source denitrification functionalized reactor and the A2 anoxic raw water carbon source denitrification functionalized reactor are the pre-denitrification zone, which uses the organic carbon source in the raw water to provide
  • the electron donor matrix of the A2 is used for denitrification
  • the facultative heterotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the reactor is used to remove nitrate nitrogen.
  • A2 anoxic raw water carbon source denitrification functionalized reactor is used as A1 anoxic
  • the original water carbon source denitrification functional reactor is supplemented to ensure that the pre-denitrification reaction is fully and thoroughly; during this reaction, the nitrate nitrogen carried by the O4 aerobic nitrification functional reactor refluxed nitrification liquid is removed; O3 aerobic organic matter is degraded
  • the aerobic heterotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the functionalized reactor removes the organic matter in the sewage entering the reactor to ensure that the subsequent aerobic reaction zone is in a low organic load state; O4 aerobic nitrification function
  • the aerobic autotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the chemical reactor removes the organic nitrogen and ammonia nitrogen in the sewage entering the reactor and improves the efficiency of the nitrification reaction.
  • the A5 anoxic raw water carbon source denitrification functional reactor and the A6 anoxic raw water carbon source denitrification functional reactor are also pre-denitrification zones, which also use organic carbon in the raw water
  • the electron donor substrate provided by the source performs denitrification to remove nitrate nitrogen
  • the A6 anoxic raw water carbon source denitrification functional reactor is also used as a supplement to the A5 anoxic raw water carbon source denitrification functional reactor to ensure pre-denitrification
  • the reaction is complete and complete.
  • the nitrate nitrogen carried by the O8 aerobic nitrification functionalized reactor and the nitrate nitrogen carried by the nitrification liquid in the backflow of the O4 aerobic nitration functionalized reactor in the first-stage A/O reaction unit is carried by the nitrate Salt and nitrogen are removed together;
  • O7 aerobic organic matter degradation functionalized reactor The aerobic heterotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the functionalized reactor removes the organic matter in the sewage entering the reactor to ensure subsequent O8 aerobic nitrification
  • the functionalized reactor is in a low organic load state;
  • the aerobic autotrophic functionalized biofilm attached to the surface of the suspended biofilm carrier in the O8 aerobic nitrification functionalized reactor removes the organic nitrogen and ammonia nitrogen in the sewage entering the reactor;
  • the strong hydraulic shearing effect caused by the increase of hydraulic load of the reaction unit strengthens the biofilm renewal and improves the biofilm metabolic activity, improves the mass transfer efficiency of oxygen and substrate, in the O7 aerobic organic
  • the A9 anoxic exogenous carbon source denitrification functionalized reactor by adding exogenous carbon source as the electron donor substrate for denitrification, in the reaction process according to the final treatment
  • the effluent total nitrogen emission target requires that the amount of nitrate nitrogen removed is controlled by adjusting the amount of external carbon source; the main function of the O10 aerobic residual organic degradation and nitrification functionalized reactor is to degrade and remove the residual anoxic exogenous carbon in A9
  • the exogenous carbon source organics added in the functionalized reactor for denitrification are also used as a supplement to the first two stages of nitrification to ensure that the final treated water quality indicators such as organics, total nitrogen and ammonia nitrogen are controlled in accordance with the design requirements.
  • the present invention combines the multi-stage anoxic/aerobic process of water inflow in stages and the functionalized technology of biofilm in reaction zone.
  • the divisional functional operation is realized, and the operation of the multi-stage A/O process is combined with the divisional functionalization of the biofilm method, and the post-denitrification anoxic reactor is added.
  • the external carbon source realizes the optimal control of the total nitrogen in the effluent and achieves the target demand for high-efficiency nitrogen removal.
  • the present invention has the following outstanding features:
  • the two-stage water inlet method and the structure of the reactor in series have realized the optimal spatial distribution of the organic load and the ammonia nitrogen load, which created favorable conditions for the efficient removal of organic matter and system nitrification, and at the same time improved the utilization of the system's front denitrification carbon source Efficiency and denitrification capacity of carbon sources in the system;
  • the reflux ratio of the aerobic nitrification liquid in the first two stages is 100% (using the sewage flow meter entering each reaction unit section), that is, the reflux ratio of the total aerobic nitrification liquid is only 100% (according to the total water intake of the treatment system).
  • the total nitrogen removal rate reaches 82.49 ⁇ 2.36%, and the denitrification efficiency of pre-denitrification can reach about 66%.
  • the single-stage A/O sewage treatment mode under the condition that the reflux ratio of the aerobic nitrification solution is 100% (according to the total flow meter of the treatment system), the theoretical total nitrogen removal rate can reach 50%.
  • the nitrogen removal rate reaches the requirement of 82%, and the minimum aerobic nitrification liquid reflux ratio must reach 456%.
  • the data shows that the two-stage influent three-stage anoxic/aerobic sewage denitrification treatment method of the present invention can achieve 99.51 ⁇ 0.41% of ammonia nitrogen removal rate under low temperature conditions and without sludge return, which is a good solution
  • the utilization rate of sewage carbon source and pre-denitrification efficiency are significantly improved, and the energy consumption of the system aerobic nitrification liquid reflux is greatly reduced, and the high-efficiency biological denitrification of urban sewage is realized. Nitrogen target.
  • Fig. 1 is a schematic diagram of a system for realizing the multi-stage anoxic/aerobic sewage biological denitrification treatment method of the present invention.
  • the first-stage nitrification liquid reflux pump 15.
  • the second-stage nitrification liquid reflux pump 16.
  • Stirrer 17.
  • Aeration device 18.
  • Suspended biofilm carrier interception device 19.
  • Suspended biofilm carrier 20.
  • Carbon source dosing device
  • the present invention adopts sub-inflow three-stage anoxic/aerobic combined reaction zone biofilm for high-efficiency denitrification treatment of sewage.
  • the system used is shown in FIG. composition.
  • the first-stage A/O reaction unit consists of A1 anoxic raw water carbon source denitrification functional reactor 1, A2 anoxic raw water carbon source denitrification functional reactor 2, O3 aerobic organic matter degradation functional reactor 3 and O4.
  • the functionalized oxynitrification reactor 4 consists of four biofilm reactors.
  • the first-stage nitration liquid reflux pump 14 is installed in the outlet well (or pipe channel) behind the outflow screen at the end of the first-stage A/O reaction unit to return the aerobic nitrification functional reactor O4 outflow mixture to A1 In the anoxic raw water carbon source denitrification functionalized reactor 1, the reflux ratio is 50% to 200%.
  • the second-stage A/O reaction unit consists of A5 anoxic raw water carbon source denitrification functional reactor 5, A6 anoxic raw water carbon source denitrification functional reactor 6, O7 aerobic organic degradation functional reactor 7 and O8.
  • the functionalized oxynitrification reactor 8 consists of four biofilm reactors.
  • a second-stage nitration liquid reflux pump 15 is installed in the outlet well (or pipe channel) behind the outlet screen at the end of the second-stage A/O reaction unit to return the outflow mixed liquid of the O8 aerobic nitrification functionalized reactor 8 to A5 Anoxic raw water carbon source denitrification functional reactor 5, the reflux ratio is 50% to 200% (to enter the raw water flowmeter of the reaction unit section).
  • the third-stage A/O unit section consists of two biofilm reactors, A9 anoxic exogenous carbon source denitrification functional reactor 9 and O10 aerobic residual organics degradation and nitrification functional reactor 10.
  • A9 Anoxic exogenous carbon source denitrification functionalized reactor 9 is provided with a carbon source dosing device 20.
  • the O8 aerobic nitrification functionalized reactor 8 is equipped with a nitrate nitrogen monitoring instrument, and according to the monitored nitrate nitrogen concentration, the carbon source dosing of the anoxic external carbon source denitrification functionalized reactor A9 is automatically controlled.
  • All reactors (A1 ⁇ O10) can adopt cylindrical tank body or rectangular tank body, the effective depth is 4-10m, the diameter-to-depth ratio of the cylindrical tank body is 2:1 ⁇ 0.5:1, and the length-to-width ratio of the rectangular tank body is 0.5: 1 ⁇ 1.5:1.
  • All (A1 ⁇ O10) reactors are equipped with an inlet water distribution device and an outlet water collection device.
  • the inlet water distribution device adopts the upper part of the weir or the submerged type near the bottom of the reactor side to distribute water.
  • the corresponding outlet water collection device is suspended in the biofilm carrier. After the interception net 18, the water is collected near the bottom of the side of the reactor or near the top of the side of the reactor.
  • All (A1 ⁇ O10) reactors are equipped with an outflow suspended biofilm carrier interception device 18, which can adopt a vertical vertical or horizontal cylindrical screen; when a vertical vertical screen is used, the opening surface of the screen is located in the tank body The effective water depth is 35%-65%; when the horizontal cylindrical screen is used, the installation height of the cylindrical screen is at the position of 35%-65% of the effective water depth of the pool body; The opening rate of the sieve is not more than 50%, and the aperture of the sieve is 50%-60% of the diameter of the suspended biofilm carrier (suspended filler).
  • All anoxic reactors (A1, A2, A5, A6, A9) are equipped with a stirrer 16 and a suspended biofilm carrier (suspended filler) 19 suitable for the growth of microorganisms, and the filler filling rate is not more than 55%.
  • the stirrer 16 should adopt a spiral or hyperboloid stirrer, and the stirring input power should not be less than 25W/m 3 .
  • All aerobic reactors (O3, O4, O7, O8, O10) are equipped with aeration devices 17, and are equipped with suspended biofilm carriers suitable for the growth of microorganisms, and the filling rate of the filler is not more than 66%.
  • the aeration device 17 should adopt perforated pipe aeration, and the arrangement adopts the dense arrangement method near the water outlet.
  • the aperture of the perforated pipe aeration hole is 3-4mm
  • the aeration orifice ventilation rate is 1.60 ⁇ 1.75m 3 /h
  • the perforated pipe is installed.
  • the horizontal error is not more than 6.5mm.
  • Mud water clarification and separation unit 11 can choose air flotation tanks, high-density sedimentation tanks, magnetic flocculation separation, screen filtration, multi-media filtration and other high-efficiency mud-water clarification and separation technologies.
  • the discharge of phosphorus from treated effluent requires chemical phosphorus removal through chemical addition.
  • the total theoretical residence time of the three-stage A/O unit is 6-12h, and the maximum flow velocity of the flow section of each reactor is not higher than 35m/h.
  • the invention adopts a continuous flow operation mode, and the sewage passes through the existing primary treatment such as the grille, the aeration grit chamber, and the primary sedimentation tank, and then enters the secondary treatment of the invention.
  • the two points of the effluent water after the primary treatment of the raw water enter the A1 reactor 1 at the front end of the first-stage A/O reaction unit section and the A5 reactor 5 at the front end of the second-stage A/O reaction unit section respectively;
  • the outflow from the reactor at the end of the A/O reaction unit section is lifted to the water inlet end of the unit by the first-stage nitration liquid reflux pump 14, that is, the reactor O4 outflow mixture is refluxed to the A1 reactor 1;
  • the second-stage A/O reaction The effluent from the reactor at the end of the unit section is raised to the water inlet end of the unit by the second-stage nitration liquid reflux pump 15, that is, the effluent mixture from the O8 reactor 8 is returned to the A5 reactor
  • the microorganisms attached and growing on the surface of the suspended biofilm carrier 19 in each reactor are in a rapid renewal state, and a functionalized biofilm compatible with the function of the reaction zone is naturally formed, namely
  • the biofilm is always in the aerobic zone or in the hypoxic zone, and through operation, a functionalized biofilm suitable for the environment of the aerobic zone or hypoxic zone will be formed.
  • A1 Reactor 1 and A2 Reactor 2 are the pre-denitrification zones.
  • the electron donor matrix provided by the organic carbon source in the raw water is used for denitrification, and the biofilm carrier is suspended in the reactor.
  • Microorganisms attached to the surface naturally form a facultative heterotrophic functionalized biofilm that is compatible with the reaction environment and substrate conditions. It has high denitrification ability and removes nitrate nitrogen with a high denitrification loading rate on the surface of the biofilm, which is beneficial to the combination Significantly improve the efficiency of the pre-denitrification reaction, while the A2 reactor 2 is used as a supplement to the A1 reactor 1 to ensure that the pre-denitrification reaction is fully and thoroughly.
  • the nitrate nitrogen carried by the refluxing nitrification liquid of the O4 reactor 4 is removed At the same time, part of the organic matter in the sewage is degraded and removed as an electron donor matrix.
  • the microorganisms attached to the surface of the suspended biofilm carrier in the O3 reactor 3 naturally form an aerobic heterotrophic functionalized biofilm that is compatible with the organic load of the reaction zone and has the ability to efficiently degrade organic matter, with a high organic matter loading rate on the surface of the biofilm Remove the organic matter in the sewage entering the reactor to ensure that the subsequent aerobic reaction zone (O4 reactor) is in a low organic load state, which is beneficial to the natural formation of microorganisms attached to the surface of the suspended biofilm carrier in the O4 reactor 4 and the reaction
  • the zone organic load is compatible with the aerobic autotrophic functional biofilm with the ability to efficiently degrade ammonia nitrogen, and the organic nitrogen and ammonia nitrogen in the sewage entering the reactor are removed with a higher ammonia nitrogen loading rate on the surface of the biofilm,
  • the anoxic A5 reactor 5 and A6 reactor 6 are also pre-denitrification zones.
  • the electron donor matrix provided by the organic carbon source in the raw water is used for denitrification and compared with The high biofilm surface denitrification load rate removes nitrate nitrogen, and the A6 reactor 6 is also used as a supplement to the A5 reactor 5 to ensure that the pre-denitrification reaction is fully and thoroughly; it is different from the first-stage A/O reaction unit.
  • the nitrate nitrogen carried by the O8 reactor 8 backflow nitrification liquid and the nitrate nitrogen carried by the O4 reactor 4 nitrification liquid are removed together, and the raw water carbon source is fully utilized, making the denitrification reaction more thorough. Further improve the denitrification efficiency.
  • the O7 reactor 7 removes the organic matter in the sewage entering the reactor with a high biofilm surface organic matter loading rate, so as to ensure that the subsequent O8 aerobic reactor 8 is in a low organic loading state, and with a high biofilm surface ammonia nitrogen loading
  • the organic nitrogen and ammonia nitrogen in the sewage entering the reactor are removed at a high rate; the strong hydraulic shear effect caused by the increase of the hydraulic load of the reaction unit strengthens the renewal of the biofilm and improves the metabolic activity of the biofilm, and improves the mass transfer efficiency of oxygen and the substrate ,
  • a highly active biofilm is formed on the surface of the suspended biological carrier in the O7 reactor 7 and the O8 reactor 8, which improves the stability of the system's nitrification operation.
  • the anoxic A9 reactor 9 is fed with an exogenous carbon source as an electron donor substrate for denitrification through the carbon source dosing system.
  • the effluent can be treated as the final treatment.
  • the total nitrogen emission target requires that the amount of nitrate nitrogen removed be controlled by adjusting the amount of external carbon source added.
  • the main function of the O10 reactor 10 is to degrade and remove the exogenous carbon source organics that may remain in the post-denitrification zone (A9 reactor 9).
  • the O10 reactor 10 also serves as a supplement to the first two stages of nitrification. In order to ensure that the final treatment effluent organic matter, total nitrogen and ammonia nitrogen and other water quality indicators are controlled in accordance with the design requirements.
  • each aerobic reactor Take a certain amount of new suspended biofilm carrier 19 and put them into each aerobic reactor to control the filling rate of 60% of the filler; add sewage to the above-mentioned aerobic reactor to reach the normal reaction control level of the reactor, and then turn it on
  • the aeration device of each reactor carries out oxygenation and aeration, and the intensity of aeration supply is controlled not to exceed 55m 3 /(m 2 ⁇ h), and the dissolved oxygen is 4 ⁇ 5mg/L;
  • the main water quality indicators of COD and ammonia nitrogen in the inlet and outlet water of the above reactor were detected, and the state of biofilm formation was observed at the same time.
  • the removal rate of COD in the effluent reached about 80%, and the amount of biofilm reached 10-15gVSS/ After m 2 , the membrane culture of the suspended biofilm carrier is completed.
  • the suspended biofilm carrier 19 that has completed the film-hanging culture is distributed to 10 reactors (A1, A2, O3, O4, O5, A5) at a filling rate of no more than 55% for anoxic reactors and no more than 66% for aerobic reactors. , A6, O7, O8, A9, O10).
  • the continuous water inlet and outlet operation mode is adopted, and the inlet water flow rate of the control system is 20-50% of the design flow rate, and it enters the A1 reactor 1 and the A5 reactor 5 according to the ratio of 1:1.
  • the amount of carbon source to be added is determined according to the total nitrogen emission requirements of the treated effluent, the type of carbon source and its denitrification C/N, such as sodium acetate as the external carbon source, according to the total nitrogen emission requirements Calculate the amount of nitrate nitrogen to be removed, and control the dosage of sodium acetate according to the ratio (C/N) of the added external carbon source to the amount of nitrate nitrogen to be removed is about 4:1.
  • the main water quality indicators of COD, ammonia nitrogen and nitrate nitrogen in the inlet and outlet water of the above-mentioned reactors are regularly tested, and the state of biofilm formation is observed at the same time.
  • the final removal rate of COD, ammonia nitrogen and total nitrogen in the final effluent to be treated will reach about 80%.
  • the system is optimized and regulated. Adjust the stirring intensity in each anoxic denitrification functionalized reactor, and reduce the stirring intensity as much as possible on the premise of ensuring that the suspended biofilm carrier 19 is fully fluidized; adjust the aeration intensity of each aerobic functionalized reactor to ensure that the suspended biofilm carrier 19 Under the premise of full fluidization, control the dissolved oxygen level between 5 and 6 mg/L;
  • Adjust the return flow of the inlet pump and the nitrification liquid reflux pump control the fractional inlet water ratio and the corresponding reflux ratio, so that the amount of dissolved COD entering the A1 reactor 1 and the amount of nitrate nitrogen carried by the reflux nitrification liquid of the O4 reactor 4
  • the ratio of is about 5:1, so that the ratio of the amount of dissolved COD entering the A5 reactor 5 to the sum of the amount of nitrate nitrogen carried by the nitrification liquid from the O4 reactor 4 and the reflux nitrification liquid from the O8 reactor 8 is Around 5:1;
  • the quality of the incoming and outgoing water in this case is as follows: Under the reaction temperature of 8 ⁇ 15°C, the removal rates of COD, ammonia nitrogen and total nitrogen are 78.60 ⁇ 1.43%, 99.51 ⁇ 0.41%, 82.49 ⁇ 2.36%, and the effluent concentration is 20.97 ⁇ 1.51. mg/L, 0.73 ⁇ 0.34mg/L, 6.24 ⁇ 0.57mg/L, with good pollutant removal effect.
  • the theoretical total nitrogen removal rate can reach 50%, in order to achieve total nitrogen removal The rate reaches the requirement of 82%, and the minimum reflux ratio of the aerobic nitrification solution must reach 456%.
  • the reflux ratio of the first two stages of aerobic nitrification liquid is 100% (using the raw water flowmeter entering each reaction unit section), that is, the reflux ratio of the total aerobic nitrification liquid is only 100% (according to the processing system).
  • the total nitrogen removal rate reaches 82.49 ⁇ 2.36%, and the pre-denitrification denitrification efficiency can reach about 66%.

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Abstract

一种低温下分段进水多级缺/好氧的污水生物脱氮处理方法，采用连续流运行方式，污水经过一级处理后由两处位置点分别进入第一级A/O反应单元与第二级A/O反应单元；第一级A/O反应单元出水端的出流提升回流至该单元进水端；第二级A/O反应单元出水端的出流提升回流至该单元进水端；第三级A/O反应单元出水端的出流经澄清分离后最终出水。该方法采用两段进水、三级缺氧/好氧结合反应分区生物膜功能化的污水处理模式，可根据原水中反硝化可利用有机物量，优化控制各区段回流比，在保证反硝化脱氮的同时降低功能化反应器内可能存在的断面水力负荷影响问题，实现低温下对有机物与含氮污染物的高效去除。

Description

低温下分段进水多级缺/好氧的污水生物脱氮处理方法 技术领域
本发明涉及一种用于通过分段进水多级缺/好氧结合反应分区生物膜功能化进行污水处理的方法，属于污水处理技术领域。
背景技术
目前，随着对城镇污水处理厂水污染物排放标准提出更高要求，尤其在有机物与氨氮、总氮等水质指标上趋于更为严格，特别在低温下传统的污水生物脱氮处理工艺显然已经不能满足要求。为提高低温下城镇污水生物脱氮效率，传统以活性污泥为主的单级或多级缺/好氧(A/O)工艺均需设置较长的污泥龄与理论水力停留时间以保证活性污泥中硝化细菌的数量，同时需通过提高曝气量保持较高的溶解氧水平以维持硝化细菌的活性，由此不仅需要较大的生化反应器池容导致土建工程投资大，而且高曝气量与长水力停留时间导致污水处理系统运行能耗大，其高投资和高能耗与现阶段国家推动的绿色生产生活发展方式相违背。
虽然缺/好氧工艺以及生物膜技术都是现有技术，但是现有活性污泥法单级或多级A/O工艺是活性污泥在缺氧与好氧交替环境下循环运行反应，这种活性污泥法系统是无法实现分区功能化设计的。传统以活性污泥为主的单级或多级A/O工艺污水生物脱氮方法面临着低温硝化限制性瓶颈以及生物脱氮效率低等技术问题。
因此，亟需一种可达到更高水质要求的城镇污水高效生物脱氮技术。
发明内容
本发明针对现有污水生物脱氮除磷技术存在的不足以及城镇污水处理高效脱氮技术需求，提出一种低温下分段进水多级缺/好氧的污水生物脱氮处理方法，可解决冬季低温条件下(6～15℃)城镇污水处理普遍存在低温硝化限制性瓶颈以及原水中可生物降解有机物反硝化利用效率低等问题，可满足不同地区尤其是低温条件下的高标准排放要求。
本发明低温下分段进水多级缺/好氧的污水生物脱氮处理方法，采用以下技术方案。
采用连续流运行方式，原水经过一级处理后(沉淀池出水)由两处位置点分别进入第一级A/O反应单元与第二级A/O反应单元；第一级A/O反应单元出水端的出流回流至该单元进水端，回流比为50％～200％；第二级A/O反应单元出水端的出流回流至该单元进水端，回流比为50％～200％；第三级A/O反应单元出水端的出流经澄清分离后出水；
所述第一级A/O反应单元，包括依次连接的A1缺氧原水碳源反硝化功能化反应器、 A2缺氧原水碳源反硝化功能化反应器、O3好氧有机物降解功能化反应器和O4好氧硝化功能化反应器四个生物膜反应器；
所述第二级A/O反应单元，包括依次连接的A5缺氧原水碳源反硝化功能化反应器、A6缺氧原水碳源反硝化功能化反应器、O7好氧有机物降解功能化反应器和O8好氧硝化功能化反应器四个生物膜反应器；
所述第三级A/O反应单元，包括依次连接的A9缺氧外源碳源反硝化功能化反应器和O10好氧残留有机物降解与硝化功能化反应器两个生物膜反应器；A9缺氧外源碳源反硝化功能化反应器内设置碳源投加装置；
所有反应器内均设置悬浮生物膜载体(悬浮填料)；
在第一级反应单元和第二级反应单元的缺氧反应器内，悬浮生物膜载体表面附着的兼氧异养型功能化生物膜利用原水碳源反硝化去除硝酸盐氮；在第一级反应单元和第二级反应单元内，以有机物降解为主的好氧反应器内悬浮生物膜载体表面附着的好氧异养型功能化生物膜去除污水中的有机物；以氨氮硝化为主的好氧反应器内悬浮生物膜载体表面附着的好氧自养型功能化生物膜去除污水中的有机氮和氨氮；在第三级反应单元按照最终处理出水总氮排放目标要求，通过投加外源性碳源去除硝酸盐氮，使最终处理出水的有机物、总氮与氨氮达到水质指标。
所述第一级A/O反应单元和第二级A/O反应单元出水端的出流回流至该单元进水端的回流比为50％～200％。
所述三级A/O反应单元的水力总停留时间为6～12小时(h)，各反应器过流断面最大流速不高于35米/小时(m/h)。
所述各个缺氧反应器(A1、A2、A5、A6、A9)内均设置搅拌器，其内适合缺氧环境微生物附着生长的悬浮生物膜载体填充率不大于55％。
所述各个好氧反应器(O3、O4、O7、O8、O10)内均设置曝气装置，其内适合微生物附着生长的悬浮生物膜载体填充率不大于66％。
所述全部反应器(A1～O10)均设置有进水配水装置与出水集水装置，进水配水装置采用堰口上部配水或淹没式靠近反应器侧面底部配水，对应出水集水装置则在填料拦截筛网后靠近反应器侧面底部集水或靠近反应器侧面顶部集水，采用上进下出或下进上出方式。
所述全部反应器(A1～O10)均设置出流悬浮生物膜载体拦截装置。所述悬浮生物膜载体拦截装置，可采用垂直竖式或水平横式圆柱状筛网；采用垂直竖式筛网时，筛网开孔面位于池体有效水深35％～65％位置；采用水平横式圆柱状筛网时，圆柱状筛网安装高度位于 池体有效水深35％～65％位置。最大拦截筛网过筛流速不大于60m/h，拦截筛网开孔率不大于50％；拦截筛网的筛网孔径为悬浮生物膜载体直径的50％～60％。
第一级A/O反应单元内，A1缺氧原水碳源反硝化功能化反应器和A2缺氧原水碳源反硝化功能化反应器为前置反硝化区，其利用原水中有机物碳源提供的电子供体基质进行反硝化，通过反应器内悬浮生物膜载体表面附着的兼氧异养型功能化生物膜去除硝酸盐氮，A2缺氧原水碳源反硝化功能化反应器作为A1缺氧原水碳源反硝化功能化反应器的补充以保证前置反硝化反应充分彻底；在此反应过程中O4好氧硝化功能化反应器回流硝化液携带的硝酸盐氮被去除；O3好氧有机物降解功能化反应器内悬浮生物膜载体表面附着的好氧异养型功能化生物膜去除进入该反应器的污水中的有机物，以保证后续好氧反应区处于低有机负荷状态；O4好氧硝化功能化反应器内悬浮生物膜载体表面附着的好氧自养型功能化生物膜，去除进入该反应器的污水中的有机氮和氨氮，提高硝化反应效率。
第二级A/O反应单元内，A5缺氧原水碳源反硝化功能化反应器和A6缺氧原水碳源反硝化功能化反应器亦为前置反硝化区，其同样利用原水中有机物碳源提供的电子供体基质进行反硝化去除硝酸盐氮，且A6缺氧原水碳源反硝化功能化反应器亦作为A5缺氧原水碳源反硝化功能化反应器的补充以保证前置反硝化反应充分彻底，在此反应过程中O8好氧硝化功能化反应器回流硝化液携带的硝酸盐氮与第一级A/O反应单元内O4好氧硝化功能化反应器出流硝化液携带的硝酸盐氮一起被去除；O7好氧有机物降解功能化反应器内悬浮生物膜载体表面附着的好氧异养型功能化生物膜去除进入该反应器的污水中的有机物，以保证后续O8好氧硝化功能化反应器处于低有机负荷状态；O8好氧硝化功能化反应器内悬浮生物膜载体表面附着的好氧自养型功能化生物膜，去除进入该反应器的污水中的有机氮和氨氮；该反应单元水力负荷增加导致的强水力剪切作用，强化了生物膜更新并提高生物膜代谢活性，提高了氧气和基质的传质效率，在O7好氧有机物降解功能化反应器和O8好氧硝化功能化反应器内悬浮生物载体表面形成了高活性生物膜，提高了系统硝化运行的稳定性。
在第三级A/O反应单元段内，A9缺氧外源碳源反硝化功能化反应器通过投加外源性碳源作为反硝化的电子供体基质，在此反应过程中按照最终处理出水总氮排放目标要求，通过调节外源性碳源投加量控制硝酸盐氮去除量；O10好氧残留有机物降解与硝化功能化反应器主要功能为降解去除残留的在A9缺氧外源碳源反硝化功能化反应器内投加的外源性碳源有机物，同时也作为前两段硝化反应的补充，以保证按照设计要求控制最终处理出水有机物、总氮与氨氮等水质指标。
本发明将分段进水多级缺/好氧工艺与反应分区生物膜功能化技术相结合。通过每个单元中多个反应器的设计，实现了分区功能化运行，使多级A/O工艺的运行与生物膜法分区功能化相结合，通过后置反硝化缺氧反应器内投加外源性碳源，实现了对出水总氮的优化控制，达到高效脱氮的目标需求。
本发明具有如下突出特点：
1.两段进水、三级缺氧/好氧结合反应分区生物膜功能化的污水处理模式，可根据原水中反硝化可利用有机物量，优化控制各区段回流比，在保证反硝化脱氮的同时降低功能化反应器内可能存在的断面水力负荷影响问题；
2.采用两段进水方式及反应器串联的结构，实现了有机负荷与氨氮负荷在空间上的优化分配，为有机物高效去除与系统硝化创造了有利条件，同时提高了系统前置反硝化碳源利用效率与系统内碳源脱氮能力；
3.通过反应分区与反应条件控制，可形成与对应反应区去除对象及其目标相适应的功能性生物膜，使系统具有较高的生物硝化与反硝化脱氮能力；
4.通过后置反硝化缺氧反应器内投加外源性碳源，可以实现对系统出水总氮的优化控制，达到高效脱氮的目标需求；
5.将功能化生物膜代替活性污泥，三级A/O反应器出水悬浮物浓度(SS)仅为50～200mg/L，生物膜微生物产率与系统污泥产量显著降低，可选用气浮池、高密度沉淀池、磁絮凝分离、筛网过滤、多介质过滤等高效的泥水澄清分离技术替代活性污泥法所采用的传统二沉池与MBR膜过滤技术；
6.尤其适用于低温条件下高标准排放的污水处理，可实现对有机物与含氮污染物的高效去除。
本发明在前两级好氧硝化液回流比均为100％(以进入各反应单元段的污水流量计)，即总的好氧硝化液的回流比仅为100％(按照处理系统进水总流量计)的条件下，其总氮去除率达82.49±2.36％，其中前置反硝化脱氮效率即可达到66％左右。如果使用单级A/O污水处理模式，在好氧硝化液的回流比为100％(按照处理系统进水总流量计)的条件下，其理论总氮去除率可达50％，为实现总氮去除率达到82％的要求，其好氧硝化液回流比最小需达到456％。
数据表明，本发明中两段进水三级缺/好氧的污水脱氮处理方法在低温条件下，在未设置污泥回流的情况下，氨氮去除率即可达99.51±0.41％，较好地解决了低温硝化问题；同时在较低好氧硝化回流比条件下，显著提高污水碳源利用率与前置反硝化效率，大大降低 了系统好氧硝化液回流能耗，实现了城镇污水高效生物脱氮的目标。
附图说明
图1为实现本发明分段进水多级缺/好氧的污水生物脱氮处理方法的系统示意图。
图中：1.A1缺氧原水碳源反硝化功能化反应器，2.A2缺氧原水碳源反硝化功能化反应器，3.O3好氧有机物降解功能化反应器，4.O4好氧硝化功能化反应器，5.A5缺氧原水碳源反硝化功能化反应器，6.A6缺氧原水碳源反硝化功能化反应器，7.O7好氧有机物降解功能化反应器，8.O8好氧硝化功能化反应器，9.A9缺氧外源碳源反硝化功能化反应器，10.O10好氧残留有机物降解与硝化功能化反应器，11.泥水澄清分离单元，12.第一级进水提升泵，13.第二级进水提升泵，14.第一级硝化液回流泵，15.第二级硝化液回流泵，16.搅拌器，17.曝气装置，18.悬浮生物膜载体拦截装置，19.悬浮生物膜载体，20.碳源投加装置。
具体实施方式
本发明采用分段进水三级缺氧/好氧结合反应分区生物膜进行污水的高效脱氮处理，所用系统如图1所示，由依次连接的三级A/O反应单元与泥水澄清分离单元11组成。
第一级A/O反应单元由A1缺氧原水碳源反硝化功能化反应器1、A2缺氧原水碳源反硝化功能化反应器2、O3好氧有机物降解功能化反应器3和O4好氧硝化功能化反应器4四个生物膜反应器组成。第一级A/O反应单元末端的出流筛网后的出水井(或管渠道)内设置第一级硝化液回流泵14，将好氧硝化功能化反应器O4出流混合液回流到A1缺氧原水碳源反硝化功能化反应器1内，回流比为50％～200％。
第二级A/O反应单元由A5缺氧原水碳源反硝化功能化反应器5、A6缺氧原水碳源反硝化功能化反应器6、O7好氧有机物降解功能化反应器7和O8好氧硝化功能化反应器8四个生物膜反应器组成。第二级A/O反应单元末端的出流筛网后的出水井(或管渠道)内设置第二级硝化液回流泵15，将O8好氧硝化功能化反应器8出流混合液回流到A5缺氧原水碳源反硝化功能化反应器5内，回流比为50％～200％(以进入该反应单元段的原水流量计)。
第三级A/O单元段由A9缺氧外源碳源反硝化功能化反应器9和O10好氧残留有机物降解与硝化功能化反应器10两个生物膜反应器组成。A9缺氧外源碳源反硝化功能化反应器9内设置碳源投加装置20。O8好氧硝化功能化反应器8内设置硝酸盐氮监测仪表，根据监测的硝酸盐氮浓度，自动控制缺氧外源碳源反硝化功能化反应器A9的碳源投加。
全部反应器(A1～O10)可采用圆柱池体或长方池体，有效深度为4～10m，圆柱池体径深比为2:1～0.5:1，长方形池体长宽比为0.5:1～1.5:1。全部(A1～O10)反应器均设置有进水 配水装置与出水集水装置，进水配水装置采用堰口上部配水或淹没式靠近反应器侧面底部配水，对应出水集水装置则在悬浮生物膜载体拦截网18后靠近反应器侧面底部集水或靠近反应器侧面顶部集水，采用上进下出或下进上出方式。全部(A1～O10)反应器均设置出流悬浮生物膜载体拦截装置18，可采用垂直竖式或水平横式圆柱状筛网；采用垂直竖式筛网时，筛网开孔面位于池体有效水深35％～65％位置；采用水平横式圆柱状筛网时，圆柱状筛网安装高度位于池体有效水深35％～65％位置；最大拦截网过筛流速不大于60m/h，拦截筛网开孔率不大于50％，筛网孔径为悬浮生物膜载体(悬浮填料)直径的50％～60％。
所有缺氧反应器(A1、A2、A5、A6、A9)内均设置搅拌器16，并设有适合微生物附着生长的悬浮生物膜载体(悬浮填料)19，填料填充率不大于55％。搅拌器16宜采用螺旋式或双曲面搅拌器，搅拌输入功率不小于25W/m 3。
所有好氧反应器(O3、O4、O7、O8、O10)内均设置曝气装置17，并设有适合微生物附着生长的悬浮生物膜载体，填料填充率不大于66％。曝气装置17宜采用穿孔管曝气，布置采用近出水端加密排布方式，穿孔管曝气孔孔径为3～4mm，曝气孔口通气量为1.60～1.75m 3/h，穿孔管安装水平误差不大于6.5mm。
泥水澄清分离单元11，可选用气浮池、高密度沉淀池、磁絮凝分离、筛网过滤、多介质过滤等高效的泥水澄清分离技术，主要作用为去除脱落的生物膜等悬浮固体，并根据最终处理出水磷的排放要求通过加药进行化学除磷。
三级A/O单元的总理论停留时间为6～12h，各反应器过流断面最大流速不高于35m/h。
本发明采用连续流运行方式，污水经过格栅、曝气沉砂池、初沉池之类的现有一级处理，再进入到本发明的二级处理。原水一级处理后的出水分两个位置点分别进入第一级A/O反应单元段的前端的A1反应器1与第二级A/O反应单元段前端的A5反应器5；第一级A/O反应单元段末端反应器出流通过第一级硝化液回流泵14提升至该单元进水端，即将反应器O4出流混合液回流到A1反应器1；第二级A/O反应单元段末端反应器出流通过第二级硝化液回流泵15提升至该单元进水端，即将O8反应器8出流混合液回流到A5反应器5；第三级A/O反应单元的末端反应器出流经由O10反应器10进入泥水澄清分离单元11，经澄清分离后最终出水。
通过拦截筛网18对悬浮生物膜载体19的拦截，使得各反应器内悬浮生物膜载体19表面附着生长的微生物处于快速更新状态，并自然形成与反应区功能相适应的功能化生物膜，即生物膜始终处于好氧区或者始终处于缺氧区，通过运行就会形成与好氧区或者缺氧区环境相适应的功能化生物膜。
第一级A/O反应单元段内，A1反应器1和A2反应器2为前置反硝化区，利用原水中有机物碳源提供的电子供体基质进行反硝化，反应器内悬浮生物膜载体表面附着生长的微生物自然形成与反应环境及基质条件相适应具有高效反硝化能力的兼氧异养型功能化生物膜，以较高的生物膜表面反硝化负荷率去除硝酸盐氮，有利于并显著提高前置反硝化反应效率，同时A2反应器2作为A1反应器1的补充以保证前置反硝化反应充分彻底，在此反应过程中O4反应器4回流硝化液携带的硝酸盐氮被去除，同时污水中的部分有机物作为电子供体基质得到降解去除。O3反应器3内悬浮生物膜载体表面附着生长的微生物自然形成与该反应区有机负荷相适应具有高效降解有机物能力的好氧异养型功能化生物膜，以较高的生物膜表面有机物负荷率去除进入该反应器的污水中的有机物，以保证后续好氧反应区(O4反应器)处于低有机负荷状态，有利于O4反应器4内悬浮生物膜载体表面附着生长的微生物自然形成与该反应区有机负荷相适应具有高效降解氨氮能力的好氧自养型功能化生物膜，以较高的生物膜表面氨氮负荷率去除进入该反应器的污水中的有机氮和氨氮，提高硝化反应效率。
第二级A/O反应单元段内，缺氧的A5反应器5与A6反应器6亦为前置反硝化区，利用原水中有机物碳源提供的电子供体基质进行反硝化，并以较高的生物膜表面反硝化负荷率去除硝酸盐氮，且A6反应器6亦作为A5反应器5的补充以保证前置反硝化反应充分彻底；与第一级A/O反应单元不同，在此反应过程中O8反应器8回流硝化液携带的硝酸盐氮与O4反应器4出流硝化液携带的硝酸盐氮一起被去除，原水碳源得到充分利用，使反硝化反应进行的更为彻底，进一步提高脱氮效率。O7反应器7以较高的生物膜表面有机物负荷率去除进入该反应器的污水中的有机物，以保证后续O8好氧反应器8处于低有机负荷状态，并以较高的生物膜表面氨氮负荷率去除进入该反应器的污水中的有机氮和氨氮；该反应单元水力负荷增加导致的强水力剪切作用，强化了生物膜更新并提高生物膜代谢活性，提高了氧气和基质的传质效率，在O7反应器7和O8反应器8内悬浮生物载体表面形成了高活性生物膜，提高了系统硝化运行的稳定性。
在第三级A/O反应单元段内，缺氧A9反应器9通过碳源投加系统投加外源性碳源作为反硝化的电子供体基质，在此反应过程中可按照最终处理出水总氮排放目标要求，通过调节外源性碳源投加量控制硝酸盐氮去除量。O10反应器10主要功能为降解去除可能残留的在后置反硝化区(A9反应器9)内投加的外源性碳源有机物，同时O10反应器10也作为前两段硝化反应的补充，以保证按照设计要求控制最终处理出水有机物、总氮与氨氮等水质指标。
以生活污水为主的某城镇污水，具体实施方式是按照以下步骤完成的：
(1)悬浮生物膜载体挂膜培养
取一定量新的悬浮生物膜载体19，分别投入各好氧反应器内，控制填料投加填充率为60％；向上述各好氧反应器加入污水至反应器正常反应控制液位后，开启各反应器曝气装置进行充氧曝气，控制曝气供气强度不大于55m 3/(m 2·h)，溶解氧在4～5mg/L；
在上述反应条件下进行生物膜的培养挂膜，前5天每天更新各反应器内污水一次，即上述各好氧反应器按照每天1个周期的运行方式进行生物膜培养挂膜；第5～10天每天更新反应器内污水两次，即上述各好氧反应器按照每天2个周期的运行方式进行生物膜培养挂膜；
第10天后对上述反应器进出水的COD与氨氮主要水质指标进行检测，同时观察生物膜挂膜状态，待每个处理周期出水COD去除率达到80％左右，且生物膜量达到10～15gVSS/m 2后，即完成悬浮生物膜载体的挂膜培养。
(2)初期启动
将完成挂膜培养的悬浮生物膜载体19按照缺氧反应器不超过55％、好氧反应器不超过66％的填充率分配到10个反应器(A1、A2、O3、O4、O5、A5、A6、O7、O8、A9、O10)中。
采用连续进出水运行方式，控制系统进水流量为设计流量的20～50％，按照1:1的比例分点进入A1反应器1与A5反应器5。
开启缺氧反应器中的搅拌器11，使缺氧反硝化功能化反应器(A1、A2、A5、A6)内悬浮生物膜载体充分流化；开启好氧反应器中的曝气装置17，使好氧功能化反应器内悬浮生物膜载体充分流化；
开启第一级硝化液回流泵14和第二级硝化液回流泵15，O4反应器4出流提升回流至A1反应器1并控制回流比例为100％，O8反应器8出流提升回流至A5反应器5，控制回流比例为100％(以进入该段的污水流量计)；
开启碳源投加装置20，碳源投加量根据处理出水总氮排放要求、碳源种类及其反硝化C/N而定，如以乙酸钠作为外源性碳源，根据总氮排放要求计算需去除的硝酸盐氮量，按照投加的外源性碳源与需去除硝酸盐氮量的比值(C/N)约为4:1控制乙酸钠的投加量。
同时，对上述各反应器进水及出水的COD与氨氮、硝酸盐氮主要水质指标进行定期检测，同时观察生物膜挂膜状态，待处理最终出水COD、氨氮与总氮去除率达到80％左右，逐步提高系统进水流量与负荷，直至处理系统达到规定的处理负荷条件。
(3)正式运行
处理系统达到规定的处理负荷条件后，对系统进行优化调控。调整各缺氧反硝化功能化反应器内搅拌强度，在保证悬浮生物膜载体19充分流化的前提下尽量降低搅拌强度；调整各好氧功能化反应器曝气强度，在保证悬浮生物膜载体19充分流化的前提下，控制溶解氧水平在5～6mg/L之间；
调整进水泵与硝化液回流泵回流量，控制分段进水比例与相应的回流比，使进入A1反应器1的进水溶解性COD的量与由O4反应器4的回流硝化液携带硝酸盐氮量的比值在5:1左右，使进入A5反应器5的进水溶解性COD量与O4反应器4出流硝化液和O8反应器8的回流硝化液携带的硝酸盐氮量之和的比值为5:1左右；
开启A9反应器9的碳源投加系统20，按照处理最终出水总氮要求控制碳源投加量，以乙酸钠为外加碳源为例，根据总氮排放要求计算需去除的硝酸盐氮量，按照投加的外源性碳源与需去除硝酸盐氮量的比值(C/N)约为4:1控制乙酸钠的投加量；根据最终出水水质指标结果，调节O10反应器曝气强度，在保证悬浮生物膜载体(悬浮填料)充分流化的前提下，控制溶解氧水平在3～4mg/L之间，以保证按照设计要求控制最终处理出水有机物、总氮与氨氮等水质指标。
本实施案例进出水水质如下：在反应温度8～15℃条件下，COD、氨氮、总氮去除率分别为78.60±1.43％、99.51±0.41％、82.49±2.36％，出水浓度分别为20.97±1.51mg/L、0.73±0.34mg/L、6.24±0.57mg/L，具有较好的污染物去除效果。
单级A/O污水处理模式，在好氧硝化液的回流比为100％(按照处理系统进水总流量计)的条件下，其理论总氮去除率可达50％，为实现总氮去除率达到82％的要求，其好氧硝化液回流比最小需达到456％。而本实施例在前两级好氧硝化液回流比均为100％(以进入各反应单元段的原水流量计)，即总的好氧硝化液的回流比仅为100％(按照处理系统进水总流量计)的条件下，其总氮去除率达82.49±2.36％，其中前置反硝化脱氮效率即可达到66％左右。
本实例表明，两段进水三级缺/好氧的污水脱氮处理方法在低温条件下，在未设置污泥回流的情况下，氨氮去除率即可达99.51±0.41％，较好地解决了低温硝化问题；同时在较低好氧硝化回流比条件下，显著提高污水碳源利用率与前置反硝化效率，大大降低了系统好氧硝化液回流能耗，实现了城镇污水高效生物脱氮的目标。

Claims (8)

  1. 一种低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：采用连续流运行方式，原水经过一级处理后由两处位置点分别进入第一级A/O反应单元与第二级A/O反应单元；第一级A/O反应单元出水端的出流回流至该单元进水端；第二级A/O反应单元出水端的出流回流至该单元进水端；第三级A/O反应单元出水端的出流经澄清分离后出水；
    所述第一级A/O反应单元，包括依次连接的A1缺氧原水碳源反硝化功能化反应器、A2缺氧原水碳源反硝化功能化反应器、O3好氧有机物降解功能化反应器和O4好氧硝化功能化反应器四个生物膜反应器；
    所述第二级A/O反应单元，包括依次连接的A5缺氧原水碳源反硝化功能化反应器、A6缺氧原水碳源反硝化功能化反应器、O7好氧有机物降解功能化反应器和O8好氧硝化功能化反应器四个生物膜反应器；
    所述第三级A/O反应单元，包括依次连接的A9缺氧外源碳源反硝化功能化反应器和O10好氧残留有机物降解与硝化功能化反应器两个生物膜反应器；A9缺氧外源碳源反硝化功能化反应器内设置碳源投加装置；
    所有反应器内均设置悬浮生物膜载体；
    在第一级反应单元和第二级反应单元的缺氧反应器内，悬浮生物膜载体表面附着的兼氧异养型功能化生物膜利用原水碳源反硝化去除硝酸盐氮；在第一级反应单元和第二级反应单元内，以有机物降解为主的好氧反应器内悬浮生物膜载体表面附着的好氧异养型功能化生物膜去除污水中的有机物；以氨氮硝化为主的好氧反应器内悬浮生物膜载体表面附着的好氧自养型功能化生物膜去除污水中的有机氮和氨氮；在第三级反应单元按照最终处理出水总氮排放目标要求，通过投加外源性碳源去除硝酸盐氮，使最终处理出水的有机物、总氮与氨氮达到水质指标。
  2. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：所述第一级A/O反应单元出水端的出流回流至该单元进水端的回流比为50％～200％。
  3. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：所述第二级A/O反应单元出水端的出流回流至该单元进水端的回流比为50％～200％。
  4. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：所述三级A/O反应单元总停留时间为6～12小时，各反应器过流断面最大流速不高于35米/小时。
  5. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：所述各个缺氧反应器内的悬浮生物膜载体的填充率不大于55％。
  6. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特 征是：所述各个好氧反应器内的悬浮生物膜载体填充率不大于66％。
  7. 根据权利要求1所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：所述全部反应器均设置出流悬浮生物膜载体拦截装置，所述悬浮生物膜载体拦截装置为拦截筛网。
  8. 根据权利要求4所述的低温下分段进水多级缺/好氧的污水生物脱氮处理方法，其特征是：拦截筛网过筛流速不大于60米/小时，拦截筛网开孔率不大于50％，拦截筛网的筛网孔径为悬浮生物膜载体直径的50％～60％。
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