WO2021223378A1 - 反应分区可调的两级缺/好氧生物膜污水处理系统 - Google Patents

反应分区可调的两级缺/好氧生物膜污水处理系统 Download PDF

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WO2021223378A1
WO2021223378A1 PCT/CN2020/124103 CN2020124103W WO2021223378A1 WO 2021223378 A1 WO2021223378 A1 WO 2021223378A1 CN 2020124103 W CN2020124103 W CN 2020124103W WO 2021223378 A1 WO2021223378 A1 WO 2021223378A1
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reactor
anoxic
aerobic
stage
aerobic reactor
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PCT/CN2020/124103
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French (fr)
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毕学军
周小琳
樊星
王晓东
陈珊珊
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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
    • 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
    • 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

Definitions

  • the invention relates to a system for sewage treatment through anoxic/aerobic biofilm, and belongs to the technical field of sewage treatment.
  • 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 kind of activated sludge method system cannot realize the functional design of partition, the biological denitrification efficiency is low, and the investment and operation cost are high.
  • the present invention proposes a two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones. Through automatic control and adjustment of reaction space and operating conditions, different The most economical sewage treatment under seasonal changes.
  • the two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones of the present invention adopts the following technical schemes.
  • the system includes a first-stage A/O unit and a second-stage A/O unit connected in sequence;
  • the first-stage A/O unit includes a first anoxic reactor, a second anoxic/aerobic reactor, and a second Three aerobic reactors, fourth aerobic reactors and fifth aerobic reactors;
  • the second-stage A/O unit includes the sixth anoxic reactor, the seventh anoxic reactor and the eighth aerobic reactor connected in sequence
  • Each reactor is filled with suspended biofilm carriers;
  • the first anoxic reactor, the sixth anoxic reactor, the seventh anoxic reactor and the second anoxic/aerobic reactor are provided with Stirring device;
  • the third aerobic reactor, the fourth aerobic reactor, the fifth aerobic reactor, the eighth aerobic reactor and the second anoxic/aerobic reactor are provided with aeration devices.
  • the filling rate of the suspended biofilm carrier is not more than 45%, and the second anoxic/aerobic reactor and the first anoxic reactor are not more than 45%.
  • the filling rate in the five aerobic reactor is not more than 40%, and the filling rate in the third aerobic reactor, the fourth aerobic reactor and the eighth aerobic reactor is not more than 55%.
  • the stirring device adopts a spiral or hyperboloid stirrer, and the stirring input power is not less than 25W/m 3 .
  • the aeration device adopts a single-sided arrangement of perforated pipes for aeration, and the ventilation rate of the aeration orifices is 1.60-1.75m 3 /h.
  • Each reactor is provided with an outflow suspended biofilm carrier interception screen, the maximum sieving flow rate of the interception screen is not more than 60m/h, the opening rate of the interception screen is not more than 60%, and the screen aperture is a suspended biofilm carrier 60% of the diameter.
  • the inlet end of the first-stage A/O unit is provided with an online flow analyzer and an online COD analyzer; the outlet end of the first anoxic reactor is provided with an online nitrate nitrogen analyzer; the fifth aerobic reactor An online ammonia nitrogen analyzer, an online nitrate nitrogen analyzer and an online dissolved oxygen analyzer are installed at the water outlet.
  • the second anoxic/aerobic reactor is controlled and adjusted according to the following process:
  • the second anoxic/aerobic reactor When the second anoxic/aerobic reactor is turned on with stirring and the aeration is closed, it is used as an anoxic denitrification reactor for denitrification and denitrification; when the concentration of nitrate nitrogen in the effluent of the first anoxic reactor is lower than or equal to the setting When the constant value C 1 is set and the maintenance time exceeds the set value T 1 , the second anoxic/aerobic reactor will automatically turn off stirring and turn on aeration, that is, change from anoxic state to aerobic state, and the reactor will be regarded as aerobic The reactor undergoes organic degradation; when the nitrate nitrogen concentration in the effluent of the first anoxic reactor is higher than the set value C 1 and the maintenance time exceeds the set value T 2 , the aeration of the second anoxic/aerobic reactor is closed And the stirring is started, and the aerobic state is changed to the hypoxic state.
  • the fifth aerobic reactor performs aeration adjustment according to the following process:
  • a nitrification liquid reflux pump is arranged between the fifth aerobic reactor and the first anoxic reactor, and the nitrification liquid outflow from the fifth aerobic reactor is returned to the first anoxic reactor through a pipe (channel).
  • the total amount of COD entering the first anoxic reactor is obtained by online monitoring the first anoxic reactor water intake and the influent COD concentration. According to the set value ⁇ 1 of the carbon to nitrogen ratio (C/N), it is determined that it needs to enter the first
  • the total amount of nitrate nitrogen in the anoxic reactor is determined by the concentration of nitrate nitrogen in the effluent of the fifth aerobic reactor. At this time, if the reflux ratio is greater than 200%, the reflux ratio will be 200%, and if it is less than 50%, it will be refluxed. The ratio is 50%.
  • the sixth anoxic reactor is equipped with a carbon source dosing device, and the total amount of nitrate entering the sixth anoxic reactor is calculated according to the nitrate nitrogen concentration in the effluent of the fifth aerobic reactor, and the total amount of nitrate entering the sixth anoxic reactor is calculated according to the carbon to nitrogen ratio (C/ The set value ⁇ 2 of N) determines the amount of carbon source to be added.
  • Each of the reactors adopts a cylindrical or rectangular tank body, the diameter-to-depth ratio of the cylindrical tank body is 2:1 to 0.5:1, the effective depth is 4 to 10 m; the length to width ratio of the rectangular tank body is 0.5:1 to 1.5:1 , The effective depth is 4-10m, and the maximum flow velocity of the flow section is not higher than 35m/h.
  • Each of the reactors is provided with an inlet water distribution device and an outlet water collection device.
  • the inlet water distribution device adopts the upper part of the weir to distribute water or the submerged type close to the bottom of the side of the reactor.
  • the corresponding outlet water collection device is close to the reactor after intercepting the screen.
  • the water is collected at the bottom of the side or close to the top of the side of the reactor.
  • the water in and out of each reactor adopts the mode of top in and bottom out or bottom in and top out to control the hydraulic flow pattern to avoid the short flow phenomenon of the reactor.
  • the first anoxic reactor is the pre-anoxic denitrification zone, which uses the electron donor matrix provided by the organic carbon source in the raw water to perform denitrification to remove nitrate nitrogen.
  • the effluent from the five aerobic reactor carries nitrate nitrogen back to the first anoxic reactor; the second anoxic/aerobic reactor serves as an anoxic denitrification/aerobic organic degradation adjustment zone, and uses raw water when it is in anoxic state
  • the electron donor matrix provided by the organic carbon source performs denitrification to remove nitrate nitrogen, as a supplement to the first anoxic reactor, to ensure that the pre-denitrification reaction is fully and thoroughly, and when in aerobic state, it is used as an aerobic degradation zone for organic matter, and the degradation and removal enters Organic matter in the sewage in the reactor to ensure that the subsequent aerobic reaction zone is in a low organic load state; when the second anoxic/aerobic reactor is in anoxic state, the third aerobic reactor serves
  • the third aerobic reactor serves as a good
  • the oxygen organic matter degradation and nitrification reaction zone removes the organic matter, organic nitrogen and ammonia nitrogen entering the reactor;
  • the fourth aerobic reactor serves as the aerobic nitrification reaction zone to remove organic nitrogen and ammonia nitrogen entering the reactor;
  • the fifth aerobic reactor serves as The aerobic nitration reaction zone, which can adjust the aeration to control the dissolved oxygen level, is used as a supplement to the fourth reactor to ensure that the nitration reaction is fully and thoroughly.
  • the sixth anoxic reactor and the seventh anoxic reactor are used as the post-denitrification zone, and the added exogenous carbon source is used as the electron donor substrate for denitrification for denitrification removal Nitrate nitrogen, in this reaction process, in accordance with the total nitrogen emission target requirements of the final treated effluent, the amount of nitrate nitrogen removed is controlled by adjusting the amount of external carbon source; the eighth aerobic reactor is used for degradation and removal of the seventh anoxic reaction The residual organic matter out of the reactor is also used as a supplement to the nitrification reaction of the first-stage A/O unit to ensure that the final effluent is controlled in accordance with the design requirements, so that the organic matter, total nitrogen and ammonia nitrogen meet the water quality index requirements.
  • the pretreated sewage is lifted into the first anoxic reactor, the second anoxic/aerobic reactor, the third aerobic reactor, and the fourth aerobic reactor of the first-stage A/O unit.
  • the present invention has the following beneficial features:
  • the present invention adopts the setting of front and post denitrification to improve the high-efficiency utilization and denitrification efficiency of the internal carbon source in the raw water, and at the same time pass the external source in the post denitrification and denitrification.
  • reaction space and operating conditions can be automatically controlled and adjusted. Under the conditions of water quality, water volume, and water temperature fluctuations, the economic operation of sewage treatment can be realized through partial reactor function adjustments and dissolved oxygen control methods;
  • Biofilm is used instead of activated sludge.
  • the effluent suspended solids concentration (SS) of the two-stage A/O reaction unit is only 50-200mg/L, and the biofilm microbial yield and system sludge output are significantly reduced.
  • An air flotation tank can be used.
  • High-density sedimentation tank, magnetic flocculation separation, screen filtration, multi-media filtration and other efficient sludge water clarification and separation technologies replace the traditional secondary sedimentation tank and MBR membrane filtration technology used in the activated sludge method;
  • Fig. 1 is a schematic diagram of a sewage treatment system with a two-stage anoxic/aerobic combined reaction zone biofilm according to the present invention.
  • the first anoxic reactor 2. The second anoxic/aerobic reactor, 3. The third aerobic reactor, 4. The fourth aerobic reactor, 5. The fifth aerobic reactor, 6. The sixth anoxic reactor, 7. The seventh anoxic reactor, 8. The eighth aerobic reactor, 9. Mud-water clarification and separation unit, 10. Suspended biofilm carrier, 11. Stirring device, 12. Aeration Device, 13. Suspended biofilm carrier interception screen, 14. Carbon source dosing device, 15. Nitration liquid reflux pump, 16. Controller, 17. Controller, 18. Controller, 19. Controller.
  • the two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones of the present invention includes a first-stage A/O unit, a second-stage A/O unit, and a muddy water clarification and separation unit connected in sequence. .
  • the first-stage A/O unit includes the first anoxic reactor 1, the second anoxic/aerobic reactor 2, the third aerobic reactor 3, the fourth aerobic reactor 4, and the fifth aerobic reactor connected in sequence ⁇ 5.
  • the second-stage A/O unit includes a sixth anoxic reactor 6, a seventh anoxic reactor 7, and an eighth aerobic reactor 8, which are connected in sequence.
  • Each reactor (1-8) adopts a cylindrical or rectangular tank body, the diameter-to-depth ratio of the cylindrical tank body is 2:1 ⁇ 0.5:1, and the effective depth is 4 ⁇ 10m; the length-to-width ratio of the rectangular tank body is 0.5:1 ⁇ 1.5:1, the effective depth is 4-10m, and the maximum flow velocity of the flow section is not higher than 35m/h.
  • Each reactor (1-8) is 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, and the corresponding outlet water collection device is behind the interception screen
  • the water is collected near the bottom of the reactor side or near the top of the side of the reactor.
  • the water inlet and outlet modes of each reactor adopt the mode of top in and bottom out or bottom in and top out to control the hydraulic flow pattern to avoid the short flow phenomenon of the reactor.
  • Each reactor (1-8) is filled with a suspended biofilm carrier 10.
  • the filling rate in the first, sixth, and seventh anoxic reactors (1, 2, 6, 7) is not more than 45%, and the second anoxic/aerobic reactor 2 and the fifth aerobic reactor 5
  • the filling rate of the third, fourth and eighth aerobic reactor (3, 4, 8) is not more than 55%.
  • the first, sixth, and seventh anoxic reactors (1, 2, 7) and the second anoxic/aerobic reactor 2 are provided with a stirring device 11.
  • the stirring device 11 adopts a spiral or hyperboloid stirrer, and the stirring input power is not less than 25W/m 3 .
  • the third, fourth, fifth and eighth aerobic reactors (3, 4, 5, 8) and the second anoxic/aerobic reactor 2 are provided with aeration devices 12.
  • the aeration device 12 adopts a single-sided arrangement of perforated pipes for aeration.
  • a perforated pipe is arranged at the bottom of the 2/3 pool on the side close to the water outlet.
  • the perforated pipe aeration holes are arranged in a dense arrangement near the water outlet.
  • the aeration hole diameter It is 3 ⁇ 6mm
  • the ventilation rate of the aeration orifice is 1.60 ⁇ 1.75m 3 /h
  • the horizontal error of the perforated pipe installation is not more than 6.5mm.
  • Each reactor (1-8) is equipped with an outflow suspended biofilm carrier interception screen 13, the maximum sieving flow rate of the interception screen is not more than 60m/h, the opening rate of the interception screen is not more than 60%, and the screen aperture is 60% of the diameter of the suspended biofilm carrier.
  • the intercepting screen 13 can be a vertical vertical or horizontal cylindrical screen; when a vertical vertical screen is used, the opening surface of the screen is located at 35%-65% of the effective water depth of the pool; a horizontal horizontal cylindrical screen is adopted. In the case of a cylindrical screen, the installation height of the cylindrical screen is located at the position of 35% to 65% of the effective water depth of the pool body.
  • the water inlet end of the system (the water inlet end of the first anoxic reactor 1) is provided with an online flow analyzer and an online COD analyzer to obtain the inlet water flow rate and the COD concentration of the inlet water.
  • An online nitrate nitrogen analyzer is installed at the outlet end of the first anoxic reactor 1 to obtain the nitrate nitrogen concentration of the effluent.
  • the outlet end of the fifth aerobic reactor 5 is provided with an online ammonia nitrogen analyzer, an online nitrate nitrogen analyzer, and an online dissolved oxygen analyzer to obtain the ammonia nitrogen concentration, nitrate nitrogen concentration and dissolved oxygen concentration of the effluent.
  • the second anoxic/aerobic reactor 2 has an adjustable function, and the stirring device and aeration device in it are controlled by the controller 16, and it operates according to the following process:
  • the reactor 2 When the second anoxic/aerobic reactor 2 is in the state where the stirring device is turned on and the aeration device is turned off, the reactor 2 is used as an anoxic denitrification reactor for denitrification and denitrification; when the first anoxic reactor 1 effluents nitric acid When the salt nitrogen concentration is lower than or equal to the set value C 1 , and the maintenance time exceeds the set value T 1 , the second anoxic/aerobic reactor 2 automatically closes the stirring device and turns on the aeration device, that is, it changes from anoxic state In an aerobic state, the reactor 2 serves as an aerobic reactor for organic matter degradation.
  • the second anoxic/aerobic reactor 2 When the nitrate nitrogen concentration in the effluent of the first anoxic reactor 1 is higher than the set value C 1 and the maintenance time exceeds a set value T 2 , the second anoxic/aerobic reactor 2 will automatically close the aeration system and Turn on the stirring system, that is, change from aerobic state to anoxic state.
  • the fifth aerobic reactor 5 has aeration adjustment function, and the stirring device and aeration device in it are controlled by the controller 17, and it runs according to the following process:
  • the setting value C 1 , setting value C 2 , setting value C 3 , setting value T 1 and setting value T 2 need to be determined according to the final effluent ammonia nitrogen requirements and final effluent total nitrogen requirements to meet the final effluent requirements Request for adjustment.
  • a nitration liquid reflux pump 15 is provided between the fifth aerobic reactor 5 and the first anoxic reactor 1, the reflux pump 15 is connected to the controller 18, and the reflux pump 15 adopts a low-lift large-flow axial flow pump.
  • the controller 18 for the reflux of the nitrification liquid controls the reflux pump 15 to return the nitrification liquid from the fifth aerobic reactor 5 to the first anoxic reactor 1 through a pipe (drain).
  • the total amount of COD entering the first anoxic reactor 1 is obtained by on-line monitoring of the first anoxic reactor 1 water intake and the influent COD concentration, and the amount of COD entering the first anoxic reactor 1 is determined according to the set value ⁇ 1 of the carbon to nitrogen ratio (C/N).
  • 50% means the reflux ratio is 50%.
  • the sixth anoxic reactor 6 is provided with a carbon source dosing device 14, the carbon source dosing device 14 is connected to the controller 19, and the controller 19 controls the dosing amount of the carbon source dosing device 14. According to the nitrate nitrogen concentration in the effluent of the fifth aerobic reactor 5, the total amount of nitrate entering the sixth anoxic reactor 6 is obtained, and the carbon source dosage is determined according to the set value ⁇ 2 of the carbon to nitrogen ratio (C/N) .
  • the setting values ( ⁇ 1 and ⁇ 2 ) of the carbon to nitrogen ratio (C/N) can be determined according to empirical values.
  • ⁇ 1 and ⁇ 2 are respectively related to the types of raw water and carbon sources, and each type of raw water and carbon source has experience The value is an existing technology.
  • the first anoxic reactor 1 is the pre-anoxic denitrification zone, which uses the electron donor matrix provided by the organic carbon source in the raw water to perform denitrification to remove nitrate nitrogen.
  • the effluent from the fifth aerobic reactor 5 flows back the nitrate nitrogen to the first anoxic reactor 1 through the nitration liquid reflux pump 15.
  • the second anoxic/aerobic reactor 2 is an anoxic denitrification/aerobic organic degradation adjustment zone.
  • the reactor 2 When the reactor 2 is in anoxic state, it uses the electron donor matrix provided by the organic carbon source in the raw water for denitrification to remove nitric acid Salt nitrogen is used as a supplement to the first anoxic reactor 1 to ensure that the pre-denitrification reaction is fully and thoroughly; when the reactor 2 is in aerobic state, it is used as an aerobic degradation zone for organic matter, degraded and removed into the sewage in the reactor In order to ensure that the subsequent aerobic reaction zone is in a low organic load state; when the second anoxic/aerobic reactor 2 is in an anoxic state, the third aerobic reactor 3 serves as the aerobic degradation zone of organic matter, and the degradation and removal enters this Organic matter in the sewage in the reactor to ensure that the subsequent aerobic reaction zone is in a low organic load state.
  • the third aerobic reactor 3 When the second anoxic/aerobic reactor 2 is in aerobic state, the third aerobic reactor 3 is used as aerobic organic matter to degrade
  • the nitrification reaction zone removes organic matter, organic nitrogen and ammonia nitrogen entering the reactor;
  • the fourth aerobic reactor 4 serves as an aerobic nitration reaction zone to remove organic nitrogen and ammonia nitrogen entering the reactor.
  • the fifth aerobic reactor 5 serves as an aerobic nitration reaction zone with adjustable aeration to control the level of dissolved oxygen, and serves as a supplement to the fourth reactor 4 to ensure that the nitration reaction is fully complete.
  • the sixth anoxic reactor 6 and the seventh anoxic reactor 7 are used as post-denitrification zones, which use the added exogenous carbon source as the electron donor substrate for denitrification.
  • Denitrification removes nitrate nitrogen.
  • the eighth aerobic reactor 8 mainly degrades and removes the residual organic matter in the outflow of the seventh anoxic reactor 7, and can also perform nitrification as a supplement to the nitration reaction of the first-stage A/O unit (also can be understood as the second-stage A/O unit).
  • the nitrification reaction of the /O unit but it is only a supplement, not the main nitrification reaction) to ensure that the final treated water quality indicators such as organic matter, total nitrogen and ammonia nitrogen are controlled in accordance with the design requirements.
  • the mud water clarification and separation unit 9, the carbon source dosing device 14, and each controller all adopt the existing technology.
  • the system is used to treat the primary effluent of the actual sewage treatment plant.
  • the specific implementation method is completed according to the following steps:
  • the dosing and filling rate is 55%; after adding raw water to the above-mentioned reactors to the normal reaction control liquid level of the reactor, turn on the aeration device 12 of each reactor for oxygenation and aeration, and control the aeration and supply
  • the strength is not more than 55m 3 /(m 2 ⁇ h), and the dissolved oxygen is 4 ⁇ 5mg/L for biofilm culture and membrane formation.
  • the sewage in the reactor is updated once a day for the first 5 days; the reactor is updated every day for the 5th to 10th days Sewage twice; after the 10th day, monitor the main water quality indicators of COD and ammonia nitrogen for the mixed solution of the above-mentioned reactor water and different reaction periods, and observe the state of biofilm formation, until the COD removal rate of the effluent reaches 80% in each treatment cycle After forming an effective biofilm coating, the coating culture of the suspended biofilm carrier is completed.
  • the suspended biofilm carrier 10 that has completed the film-hanging culture shall not exceed 45% in the first, sixth, and seventh hypoxic reactors (1, 6, 7), the second hypoxic/aerobic reactor 2 and the fifth aerobic reactor 2
  • the filling rate of reactor 5 not exceeding 40%, the third, fourth, and eighth aerobic reactor (3, 4, 8) not exceeding 55% is distributed to each reactor (1-8).
  • the continuous water inlet and outlet operation mode is adopted, and the inlet water flow is controlled to be 20-50% of the design flow.
  • the stirring device 11 Turn on the stirring device 11 to fully fluidize the suspended biofilm carrier 10 in the first, sixth, and seventh anoxic reactors (1, 6, 7) and the second anoxic/aerobic reactor 2.
  • the aeration device 12 is turned on to fully fluidize the suspended biofilm carrier in the third, fourth, and eighth aerobic reactors (3, 4, 8) and the fifth aerobic reactor 5.
  • the reflux pump 15 is turned on, and the outflow of the fifth aerobic reactor 5 is raised and refluxed to the first anoxic reactor 1 through the pipe (drain), and the reflux ratio is controlled to be 100%.
  • the carbon source dosing device 14 and the controller 19 are turned on, for example, sodium acetate is used as an external carbon source, and ⁇ 1 is set to 4.0:1 to automatically control the amount of carbon source dosing.
  • ⁇ 1 is set to 4.0:1 to automatically control the amount of carbon source dosing.
  • pay attention to the COD, ammonia nitrogen, and nitrate nitrogen of the influent water of the system and the effluent of the eighth reactor and observe the state of biofilm formation.
  • the final removal rate of COD, ammonia nitrogen and total nitrogen in the final effluent to be treated will reach about 80%, and form an effective After the biofilm is mounted, gradually increase the water flow and load of the system until the processing load of the system reaches the specified processing load condition.
  • the nitrate nitrogen concentration C 1 , the ammonia nitrogen concentration C 2 and the ammonia nitrogen concentration C 3 can be set to 2 mg/L and 4 mg/L respectively.
  • the T 1 and T 2 values can be set to 5 minutes.
  • the quality of the incoming and outgoing water in this case is as follows: at the reaction temperature of 8 ⁇ 25°C, the COD concentration of the influent is in the range of 76 ⁇ 284mg/L, and the average effluent concentration is 29.3 ⁇ 10.6mg/L; the concentration of ammonia nitrogen in the influent is in the range of 21.8 ⁇ 85.1mg /L, the effluent ammonia nitrogen concentration is 0.14 ⁇ 0.33mg/L; the influent total nitrogen concentration ranges from 25.7 to 87.8mg/L, and the average effluent concentration is 2.7 ⁇ 3.4mg/L. Under the conditions of fluctuating reaction conditions, the system achieves a stable pollutant removal effect.

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Abstract

一种反应分区可调的两级缺/好氧生物膜污水处理系统，包括依次连接的第一级A/O单元和第二级A/O单元；第一级A/O单元包括依次连接的第一缺氧反应器（1）、第二缺/好氧反应器（2）、第三好氧反应器（3）、第四好氧反应器（4）和第五好氧反应器（5）；第二级A/O单元包括依次连接的第六缺氧反应器（6）、第七缺氧反应器（7）和第八好氧反应器（8）。上述系统通过前置与后置反硝化的设置，在提高原水内碳源高效利用与脱氮效率的同时，在后置反硝化脱氮中通过对外源性碳源投加的精确控制，实现按照处理目标要求对系统脱氮能力的有效控制，达到污水脱氮处理的最经济性与稳定性，适用于高排放标准的污水处理，同时可通过反应空间与反应条件的自动控制调节。

Description

反应分区可调的两级缺/好氧生物膜污水处理系统 技术领域
本发明涉及通过缺/好氧生物膜进行污水处理的系统，属于污水处理技术领域。
背景技术
随着对污水处理厂水污染物排放标准的提高，尤其在氮元素相关的水质指标方面趋于更为严格的要求，传统的以活性污泥为主的A 2/O及其变形工艺，显然已经不能满足要求，且其为了提高城镇污水脱氮效率，需设置较长的污泥龄与水力停留时间，同时需控制较高的曝气量，由此导致的高投资与高能耗与国家倡导的绿色发展方式相违背。
水质、水量、水温的波动直接影响污水处理系统的效率与稳定性，并由此导致污水处理工程建设投资与运行成本高。因此，在保证达到高排放标准的前提下，降低水质、水量与水温波动影响与处理工程建设投资及其运行成本成为提高城镇污水处理经济性的关键。
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，生物脱氮效率低，投资与运行成本高。
因此，亟需一种经济、高效的城镇污水生物脱氮处理技术。
发明内容
本发明针对城镇污水处理高效脱氮技术需求与提高污水处理经济性目标，提出反应分区可调的两级缺/好氧生物膜污水处理系统，通过反应空间与运行条件的自动控制调节，达到不同季节变化下污水处理的最经济性。
本发明的反应分区可调的两级缺/好氧生物膜污水处理系统，采用以下技术方案。
该系统包括依次连接的第一级A/O单元和第二级A/O单元；第一级A/O单元包括依次连接的第一缺氧反应器、第二缺/好氧反应器、第三好氧反应器、第四好氧反应器和第五好氧反应器；第二级A/O单元包括依次连接的第六缺氧反应器、第七缺氧反应器和第八好氧反应器；所述各个反应器内均填充悬浮生物膜载体；所述第一缺氧反应器、第六缺氧反应器、第七缺氧反应器内和第二缺/好氧反应器内设置有搅拌装置；所述第三好氧反应器、第四好氧反应器、第五好氧反应器、第八好氧反应器与第二缺/好氧反应器内设置有曝气装置。
所述悬浮生物膜载体的填充率为：第一缺氧反应器、第六缺氧反应器和第七缺氧反应器内的填充率不大于45％，第二缺/好氧反应器与第五好氧反应器内的填充率不大于40％， 第三好氧反应器、第四好氧反应器和第八好氧反应器的填充率为不大于55％。
所述搅拌装置采用螺旋式或双曲面搅拌器，搅拌输入功率不小于25W/m 3。
所述曝气装置采用单侧布置穿孔管曝气的方式，曝气孔口通气量为1.60～1.75m 3/h。
所述各个反应器内均设置出流悬浮生物膜载体拦截筛网，拦截筛网最大过筛流速不大于60m/h，拦截筛网开孔率不大于60％，筛网孔径为悬浮生物膜载体直径的60％。
所述第一级A/O单元的进水端设置在线流量分析仪、在线COD分析仪；所述第一缺氧反应器出水端设置在线硝酸盐氮分析仪；所述第五好氧反应器出水端设置在线氨氮分析仪、在线硝酸盐氮分析仪与在线溶解氧分析仪。
所述第二缺/好氧反应器按以下过程进行控制调节：
当第二缺/好氧反应器处于搅拌开启且曝气关闭的状态时，作为缺氧反硝化反应器进行反硝化脱氮；当第一缺氧反应器出水硝酸盐氮浓度低于或等于设定值C 1，且维持时间超过设定值T 1时，则第二缺/好氧反应器自动关闭搅拌并开启曝气，即由缺氧状态转为好氧状态，该反应器作为好氧反应器进行有机物降解；当第一缺氧反应器出水硝酸盐氮浓度高于设定值C 1，且维持时间超过设定值T 2时，则第二缺/好氧反应器的曝气关闭且搅拌启动，由好氧状态转为缺氧状态。
所述第五好氧反应器按以下过程进行曝气调节：
当第五好氧反应器出水端氨氮浓度高于或等于设定值C 2时，则调大曝气量直至溶解氧水平达到并维持在6～8mg/L；当第五好氧反应器出水端氨氮浓度低于或等于设定值C 3(C 3＜C 2)时，则将曝气量逐渐调小直至出水氨氮浓度高于设定值C 3且低于设定值C 2，控制最小曝气量为10m 3/(m 2·h)。
所述第五好氧反应器与第一缺氧反应器之间设置硝化液回流泵，通过管(渠)道将第五好氧反应器出流硝化液回流到第一缺氧反应器内。通过在线监测第一缺氧反应器进水量与进水COD浓度得到进入第一缺氧反应器内的COD总量，根据碳氮比(C/N)的设定值θ 1确定需要进入第一缺氧反应器内的硝酸盐氮总量，进而根据第五好氧反应器出水硝酸盐氮浓度确定回流量，此时回流比若大于200％则回流比取200％，若小于50％则回流比取50％。
所述第六缺氧反应器内设置碳源投加装置，根据第五好氧反应器出水硝酸盐氮浓度计算进入第六缺氧反应器内的硝酸盐总量，按照碳氮比(C/N)的设定值θ 2确定碳源投加量。
所述各个反应器采用圆柱形或长方形池体，圆柱形池体径深比为2:1～0.5:1，有效深度为4～10m；长方形池体长宽比为0.5:1～1.5:1，有效深度为4～10m，过流断面最大流速不高于35m/h。
所述各个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，各反应器进出水方式采用上进下出或下进上出方式，控制水力流态避免反应器短流现象的发生。
第一级A/O单元内，第一缺氧反应器为前置缺氧反硝化区，利用原水中有机物碳源提供的电子供体基质进行反硝化去除硝酸盐氮，在此反应过程中第五好氧反应器出流液携带硝酸盐氮回流至第一缺氧反应器；第二缺/好氧反应器作为缺氧反硝化/好氧有机物降解调节区，处于缺氧状态时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，作为第一缺氧反应器的补充保证前置反硝化反应充分彻底，处于好氧状态时作为有机物好氧降解区，降解去除进入该反应器内的污水中的有机物，以保证后续好氧反应区处于低有机负荷状态；当第二缺/好氧反应器处于缺氧状态时，第三好氧反应器作为有机物好氧降解区，降解去除进入该反应器内的污水中的有机物，以保证后续好氧反应区处于低有机负荷状态，当第二缺/好氧反应器处于好氧状态时，第三好氧反应器作为好氧有机物降解与硝化反应区去除进入该反应器的有机物、有机氮和氨氮；第四好氧反应器作为好氧硝化反应区去除进入该反应器的有机氮和氨氮；第五好氧反应器作为可调节曝气控制溶解氧水平的好氧硝化反应区，作为第四反应器的补充以保证硝化反应充分彻底。
第二级A/O单元内，第六缺氧反应器与第七缺氧反应器作为后置反硝化区，利用投加的外源性碳源作为反硝化的电子供体基质进行反硝化去除硝酸盐氮，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；第八好氧反应器用于降解去除第七缺氧反应器出流残留的有机物，同时也作为第一级A/O单元硝化反应的补充，以保证按照设计要求控制最终出水，使有机物、总氮与氨氮等满足水质指标要求。
上述系统处理污水的运行过程如下所述：
采用连续流运行方式，经过预处理的污水经提升依次进入第一级A/O单元的第一缺氧反应器、第二缺/好氧反应器、第三好氧反应器、第四好氧反应器和第五好氧反应器，第二级A/O单元的第六缺氧反应器、第七缺氧反应器、第八好氧反应器，最后通过泥水澄清分离出水。
本发明具有以下有益特点：
(1)针对城镇污水处理高排放标准，本发明通过前置与后置反硝化的设置，在提高原水内碳源高效利用与脱氮效率的同时，在后置反硝化脱氮中通过对外源性碳源投加的精确控制，实现按照处理目标要求对系统脱氮能力的有效控制，达到污水脱氮处理的最经济性与 稳定性；
(2)反应空间与运行条件可自动控制调节，在水质、水量、水温波动条件下，通过部分反应器功能调节与溶解氧控制方式，实现污水处理的经济运行；
(3)反应器串联结构，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；
(4)将生物膜代替活性污泥，两级A/O反应单元出水悬浮物浓度(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；
(5)解决了冬季低温条件下城镇污水普遍存在低温硝化限制性瓶颈以及原水碳氮比低无法满足生物脱氮需求等问题；
(6)解决了现有以悬浮生长活性污泥为主的A 2/O工艺及其变形工艺所需较长理论水力停留时间及较高的污泥与硝化液回流比导致的工程投资大、运行能耗高等问题。
附图说明
图1是本发明两级缺/好氧结合反应分区生物膜的污水处理系统示意图。
图中：1.第一缺氧反应器，2.第二缺/好氧反应器，3.第三好氧反应器，4.第四好氧反应器，5.第五好氧反应器，6.第六缺氧反应器，7.第七缺氧反应器，8.第八好氧反应器，9.泥水澄清分离单元，10.悬浮生物膜载体，11.搅拌装置，12.曝气装置，13.悬浮生物膜载体拦截筛网，14.碳源投加装置，15.硝化液回流泵，16.控制器，17.控制器，18.控制器，19.控制器。
具体实施方式
如图1所示，本发明反应分区可调的两级缺/好氧生物膜污水处理系统，包括依次连接的第一级A/O单元、第二级A/O单元和泥水澄清分离单元9。
第一级A/O单元包括依次连接的第一缺氧反应器1、第二缺/好氧反应器2、第三好氧反应器3、第四好氧反应器4、第五好氧反应器5。第二级A/O单元包括依次连接的第六缺氧反应器6、第七缺氧反应器7和第八好氧反应器8。各个反应器(1～8)采用圆柱形或长方形池体，圆柱形池体径深比为2:1～0.5:1，有效深度为4～10m；长方形池体长宽比为0.5:1～1.5:1，有效深度为4～10m，过流断面最大流速不高于35m/h。
各个反应器(1～8)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，各反应器进出水方式采用上进下出或下进上出方式，控制水力流态避免反应器短流现象的发生。
各个反应器(1～8)内均填充悬浮生物膜载体10。其中，第一、第六、第七缺氧反应器(1、2、6、7)内的填充率不大于45％，第二缺/好氧反应器2与第五好氧反应器5内的填充率不大于40％，第三、第四、第八好氧反应器(3、4、8)的填充率为不大于55％。
第一、第六、第七缺氧反应器(1、2、7)与第二缺/好氧反应器2内设置有搅拌装置11。搅拌装置11采用螺旋式或双曲面搅拌器，搅拌输入功率不小于25W/m 3。
第三、第四、第五、第八好氧反应器(3、4、5、8)与第二缺/好氧反应器2内设置有曝气装置12。曝气装置12采用单侧布置穿孔管曝气的方式，在靠近出水口一侧的2/3池底部布置穿孔管，穿孔管曝气孔布置采用近出水端加密排布方式，曝气孔孔径为3～6mm，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。
各个反应器(1～8)内均设置出流悬浮生物膜载体拦截筛网13，拦截筛网最大过筛流速不大于60m/h，拦截筛网开孔率不大于60％，筛网孔径为悬浮生物膜载体直径的60％。所述拦截筛网13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。
系统的进水端(第一缺氧反应器1的进水端)设置在线流量分析仪和在线COD分析仪，用于获取进水流量和进水的COD浓度。第一缺氧反应器1出水端设置在线硝酸盐氮分析仪，以获取出水硝酸盐氮浓度。第五好氧反应器5出水端设置在线氨氮分析仪、在线硝酸盐氮分析仪与在线溶解氧分析仪，用于获取出水的氨氮浓度、硝酸盐氮浓度和溶解氧浓度。这些分析仪均为现有技术。
第二缺/好氧反应器2具有可调节功能，通过控制器16控制其内的搅拌装置和曝气装置，按以下过程运行：
当第二缺/好氧反应器2处于搅拌装置开启且曝气装置关闭的状态时，该反应器2作为缺氧反硝化反应器进行反硝化脱氮；当第一缺氧反应器1出水硝酸盐氮浓度低于或等于设定值C 1，且维持时间超过设定值T 1时，则第二缺/好氧反应器2自动关闭搅拌装置并开启曝气装置，即由缺氧状态转为好氧状态，该反应器2作为好氧反应器进行有机物降解。当第一缺氧反应器1出水硝酸盐氮浓度高于设定值C 1，且维持时间超过某设定值T 2时，则将第二缺/好氧反应器2自动关闭曝气系统并开启搅拌系统，即由好氧状态转为缺氧状态。
第五好氧反应器5具有曝气调节功能，通过控制器17控制其内的搅拌装置和曝气装置，按以下过程运行：
当第五好氧反应器5出水端氨氮浓度高于或等于设定值C 2时，则调大曝气量直至溶解氧水平达到并维持在6～8mg/L；当第五好氧反应器5出水端氨氮浓度低于或等于设定值C 3(C 3＜C 2)时，则将曝气量逐渐调小直至出水氨氮浓度高于设定值C 3且低于设定值C 2，控制最小曝气量为10m 3/(m 2·h)。
设定值C 1、设定值C 2、设定值C 3、设定值T 1和设定值T 2的确定需要根据最终出水氨氮要求和最终出水总氮要求具体确定，以满足最终出水要求进行调整。
第五好氧反应器5与第一缺氧反应器1之间设置有硝化液回流泵15，回流泵15与控制器18连接，回流泵15采用低扬程大流量轴流泵。硝化液回流的控制器18控制回流泵15通过管(渠)道将第五好氧反应器5的出流硝化液回流到第一缺氧反应器1内。通过在线监测第一缺氧反应器1进水量与进水COD浓度得到进入第一缺氧反应器1内的COD总量，根据碳氮比(C/N)的设定值θ 1确定需要进入第一缺氧反应器1内的硝酸盐氮总量，进而根据第五好氧反应器5出水硝酸盐氮浓度确定回流量，此时回流比若大于200％则回流比取200％，若小于50％则回流比取50％。
第六缺氧反应器6内设置碳源投加装置14，碳源投加装置14与控制器19连接，控制器19控制碳源投加装置14的投加量。根据第五好氧反应器5出水硝酸盐氮浓度得到进入第六缺氧反应器6内的硝酸盐总量，按照碳氮比(C/N)的设定值θ 2确定碳源投加量。
碳氮比(C/N)的设定值(θ 1和θ 2)均可按经验值确定，θ 1和θ 2分别与原水和碳源种类有关，每种原水和碳源种类都有经验值，为现有技术。
第一级A/O单元内，第一缺氧反应器1为前置缺氧反硝化区，利用原水中有机物碳源提供的电子供体基质进行反硝化去除硝酸盐氮，在此反应过程中第五好氧反应器5出流液通过硝化液回流泵15将硝酸盐氮回流至第一缺氧反应器1。第二缺/好氧反应器2为缺氧反硝化/好氧有机物降解调节区，当反应器2处于缺氧状态时，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去除硝酸盐氮，作为第一缺氧反应器1的补充保证前置反硝化反应充分彻底；当反应器2处于好氧状态时，其作为有机物好氧降解区，降解去除进入该反应器内的污水中的有机物，以保证后续好氧反应区处于低有机负荷状态；当第二缺/好氧反应器2处于缺氧状态时，第三好氧反应器3作为有机物好氧降解区，降解去除进入该反应器内的污水中的有机物，以保证后续好氧反应区处于低有机负荷状态，当第二缺/好氧反应器2处于好氧状态时，第三好氧反应器3作为好氧有机物降解与硝化反应区去除进入该反应器的有机物、有机氮和氨氮；第四好氧反应器4作为好氧硝化反应区去除进入该反应器的有机氮和氨氮。第五好氧反应器5作为可调节曝气控制溶解氧水平的好氧硝化反应区，作为第四反应器4的补充以保证硝化反应充分彻底。
第二级A/O单元内，第六缺氧反应器6与第七缺氧反应器7作为后置反硝化区，其利用投加的外源性碳源作为反硝化的电子供体基质进行反硝化去除硝酸盐氮，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。第八好氧反应器8主要降解去除第七缺氧反应器7出流残留的有机物，还能进行硝化作用，作为第一级A/O单元硝化反应的补充(也可以理解为第二级A/O单元的硝化反应，但它只是个补充，不是主要进行硝化反应)，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。
泥水澄清分离单元9、碳源投加装置14以及各控制器均采用现有技术。
采用该系统处理实际污水处理厂的一级出水，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
取一定量悬浮生物载体10，分别投入第三、第四、第八好氧反应器(3、4、8)与第二缺/好氧反应器2内，控制上述反应器(2、3、4、5、8)投加填充率为55％；向上述各反应器加入原水至反应器正常反应控制液位后，开启各反应器曝气装置12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进行生物膜的培养挂膜，前5天每天更新反应器内污水一次；第5～10天每天更新反应器内污水两次；第10天后对上述反应器进水及不同反应时段的混合液进行COD与氨氮主要水质指标的监测，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，且形成有效的生物膜挂膜后，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10按照第一、第六、第七缺氧反应器(1、6、7)不超过45％、第二缺/好氧反应器2与第五好氧反应器5不超过40％、第三、第四、第八好氧反应器(3、4、8)不超过55％的填充率分配到各个反应器(1～8)中。
采用连续进出水运行方式，控制进水流量为设计流量的20～50％。
开启搅拌装置11，使第一、第六、第七缺氧反应器(1、6、7)与第二缺/好氧反应器2内悬浮生物膜载体10充分流化。开启曝气装置12，使第三、第四、第八好氧反应器(3、4、8)与第五好氧反应器5内悬浮生物膜载体充分流化。开启回流泵15，通过管(渠)道将第五好氧反应器5出流提升回流至第一缺氧反应器1，控制回流比例为100％。
开启碳源投加装置14与控制器19，例如以乙酸钠作为外加碳源，设定θ 1为4.0:1自动控制碳源量投加。同时，关注系统进水及第八反应器出水的COD、氨氮、硝酸盐氮，并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，且形成有效的生物膜挂膜后，逐步提高系统进水流量与负荷，直至系统处理负荷达到规定的处理负荷 条件。
(3)正式运行
达到规定的处理负荷条件后，对整个系统进行优化控制。
调整第一、第六、第七缺氧反应器(1、6、7)与第二缺/好氧反应器2的搅拌强度，在保证悬浮生物膜载体充分流化的前提下尽量降低搅拌强度；调整第三、第四、第五、第八反应器(3、4、5、8)的曝气强度，在保证悬浮生物膜载体充分流化的前提下，控制溶解氧水平在5～7mg/L之间。
开启硝化液回流控制器18，按照θ 2设定值为6.5:1控制回流量；保持碳源投加装置14与控制器19处于开启状态，按照θ 1设定值为4.0:1控制碳源投加量。
开启第二缺/好氧反应器的控制器16，按照C 1设定值、T 1设定值与T 2设定值，自动控制第二缺/好氧反应器2处于缺氧状态或好氧状态。开启第五好氧反应器的控制器17，按照C 2设定值和C 3设定值，自动调节第五反应器5的曝气强度，在悬浮生物膜载体10充分流化的前提下，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。例如，最终出水氨氮要求为2mg/L、最终出水总氮要求为5mg/L时，可设置硝酸盐氮浓度C 1、氨氮浓度C 2与氨氮浓度C 3值分别为2mg/L、4mg/L与2mg/L，可设置T 1与T 2值均为5分钟。
本实施案例进出水水质如下：在反应温度8～25℃条件下，进水COD浓度范围在76～284mg/L，平均出水浓度29.3±10.6mg/L；进水氨氮浓度范围在21.8～85.1mg/L，出水氨氮浓度0.14±0.33mg/L；进水总氮浓度范围在25.7～87.8mg/L，平均出水浓度2.7±3.4mg/L。在反应条件波动的条件下，系统达到了稳定的污染物去除效果。

Claims (10)

  1. 一种反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：包括依次连接的第一级A/O单元和第二级A/O单元；第一级A/O单元包括依次连接的第一缺氧反应器、第二缺/好氧反应器、第三好氧反应器、第四好氧反应器和第五好氧反应器；第二级A/O单元包括依次连接的第六缺氧反应器、第七缺氧反应器和第八好氧反应器；所述各个反应器内均填充悬浮生物膜载体；所述第一缺氧反应器、第六缺氧反应器、第七缺氧反应器内和第二缺/好氧反应器内设置有搅拌装置；所述第三好氧反应器、第四好氧反应器、第五好氧反应器、第八好氧反应器与第二缺/好氧反应器内设置有曝气装置。
  2. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述悬浮生物膜载体的填充率为：第一缺氧反应器、第六缺氧反应器和第七缺氧反应器内的填充率不大于45％，第二缺/好氧反应器与第五好氧反应器内的填充率不大于40％，第三好氧反应器、第四好氧反应器和第八好氧反应器的填充率为不大于55％。
  3. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述搅拌装置的搅拌输入功率不小于25W/m 3。
  4. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述曝气装置采用单侧布置穿孔管曝气的方式，曝气孔口通气量为1.60～1.75m 3/h。
  5. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述各个反应器内均设置出流悬浮生物膜载体拦截筛网，拦截筛网最大过筛流速不大于60m/h，拦截筛网开孔率不大于60％，筛网孔径为悬浮生物膜载体直径的60％。
  6. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述第一级A/O单元的进水端设置在线流量分析仪、在线COD分析仪；所述第一缺氧反应器出水端设置在线硝酸盐氮分析仪；所述第五好氧反应器出水端设置在线氨氮分析仪、在线硝酸盐氮分析仪与在线溶解氧分析仪。
  7. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述第二缺/好氧反应器按以下过程进行控制调节：
    当第二缺/好氧反应器处于搅拌开启且曝气关闭的状态时，作为缺氧反硝化反应器进行反硝化脱氮；当第一缺氧反应器出水硝酸盐氮浓度低于或等于设定值C 1，且维持时间超过设定值T 1时，则第二缺/好氧反应器自动关闭搅拌并开启曝气，即由缺氧状态转为好氧状态，该反应器作为好氧反应器进行有机物降解；当第一缺氧反应器出水硝酸盐氮浓度高于设定值C 1，且维持时间超过设定值T 2时，则第二缺/好氧反应器的曝气关闭且搅拌启动，由好氧状态转为缺氧状态。
  8. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述第五好氧反应器按以下过程进行曝气调节：
    当第五好氧反应器出水端氨氮浓度高于或等于设定值C 2时，则调大曝气量直至溶解氧水平达到并维持在6～8mg/L；当第五好氧反应器出水端氨氮浓度低于或等于设定值C 3时，C 3＜C 2，则将曝气量逐渐调小直至出水氨氮浓度高于设定值C 3且低于设定值C 2，控制最小曝气量为10m 3/(m 2·h)。
  9. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述第五好氧反应器与第一缺氧反应器之间设置硝化液回流泵，将第五好氧反应器出流硝化液回流到第一缺氧反应器内。通过在线监测第一缺氧反应器进水量与进水COD浓度得到进入第一缺氧反应器内的COD总量，根据碳氮比的设定值θ 1确定需要进入第一缺氧反应器内的硝酸盐氮总量，进而根据第五好氧反应器出水硝酸盐氮浓度确定回流量，此时回流比若大于200％则回流比取200％，若小于50％则回流比取50％。
  10. 根据权利要求1所述的反应分区可调的两级缺/好氧生物膜污水处理系统，其特征是：所述第六缺氧反应器内设置碳源投加装置，根据第五好氧反应器出水硝酸盐氮浓度计算进入第六缺氧反应器内的硝酸盐总量，按照碳氮比的设定值θ 2确定碳源投加量。
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CN114735820A (zh) * 2022-03-09 2022-07-12 安徽中环环保科技股份有限公司 多级a/o串联分批进水式低碳源污水脱氮装置及方法
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CN114604966A (zh) * 2022-03-11 2022-06-10 青岛思普润水处理股份有限公司 基于微动力的mbbr强化aoa和aao双模式系统与运行方法
CN114604967B (zh) * 2022-03-11 2023-06-23 青岛思普润水处理股份有限公司 一种基于循环流动的mbbr强化aoa和aao双模式运行方法
CN114890545A (zh) * 2022-04-24 2022-08-12 陕西锦科环保工程有限公司 一种低温污水脱氮处理系统及方法
CN115159681A (zh) * 2022-07-29 2022-10-11 江苏河马井股份有限公司 多级好厌氧污水处理系统
CN115215438A (zh) * 2022-08-03 2022-10-21 中持水务股份有限公司 用于多级ao生化池的精准曝气及加药联合控制方法及系统
CN115215438B (zh) * 2022-08-03 2024-05-03 中持水务股份有限公司 用于多级ao生化池的精准曝气及加药联合控制方法及系统

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