WO2021017367A1 - 一种基于生物膜颗粒污泥反应器的废水处理装置及其方法 - Google Patents

一种基于生物膜颗粒污泥反应器的废水处理装置及其方法 Download PDF

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WO2021017367A1
WO2021017367A1 PCT/CN2019/124745 CN2019124745W WO2021017367A1 WO 2021017367 A1 WO2021017367 A1 WO 2021017367A1 CN 2019124745 W CN2019124745 W CN 2019124745W WO 2021017367 A1 WO2021017367 A1 WO 2021017367A1
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tank
wastewater
water
biofilm
granular sludge
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English (en)
French (fr)
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雷利荣
韩俊
李友明
李广胜
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South China University of Technology SCUT
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South China University of Technology SCUT
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/06—Nutrients for stimulating the growth of microorganisms
    • 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

Definitions

  • the invention relates to the technical field of wastewater treatment, in particular to a wastewater treatment device and a method based on a biofilm granular sludge reactor.
  • the main methods of industrial wastewater treatment include physical methods, chemical methods, physicochemical methods, and biological methods.
  • the existing biological wastewater treatment methods generally have the following disadvantages: the process flow is complex, requiring a large area and high infrastructure Investment; low microbial concentration, easy expansion of sludge; poor adaptability to changes in water quality and water volume; low oxygen transfer efficiency, high power consumption; difficult operation maintenance and management; low real-time online automation control and high energy consumption. How to better solve the problems existing in the traditional wastewater treatment process and improve the energy efficiency of the biological treatment process is the focus and trend of wastewater treatment technology research.
  • the present invention provides a wastewater treatment device and method based on a biofilm granular sludge reactor, which improves the efficiency of wastewater biological treatment and reduces treatment costs.
  • the invention provides a wastewater treatment device based on a biofilm granular sludge reactor, which includes: a grid tank, a grit tank, a regulating tank, a regulating tank pump, a first pipeline mixer, a second pipeline mixer, and coagulation sedimentation Tank, the first intermediate tank and the batch-type biofilm granular sludge expanded bed reactor;
  • the outlet of the grid tank is connected with the inlet of the grit tank, the outlet of the grit tank is connected with the inlet of the adjustment tank, the outlet of the adjustment tank is connected with the first pipeline mixer through the adjustment tank water pump, and the first pipeline mixer mixes
  • a coagulant and is connected to a second pipeline mixer, the second pipeline mixer is mixed with a flocculant and connected to the inlet of the coagulation sedimentation tank, and the outlet of the coagulation sedimentation tank is connected to the inlet of the first intermediate tank,
  • the outlet of the first intermediate pool is connected with a batch type biofilm granular sludge expanded bed reactor.
  • an anaerobic reactor and a second intermediate tank are also provided, the inlet of the anaerobic reactor is connected with the outlet of the first intermediate tank, and the outlet of the anaerobic reactor is connected with the inlet of the second intermediate tank, so The outlet of the second intermediate water tank is connected with a sequencing batch type biofilm granular sludge expanded bed reactor.
  • the sequencing batch biofilm granular sludge expanded bed reactor is provided with: water inlet, support plate, biological carrier bed, limit plate, water distribution system, air distribution system, water distribution device, aerator Air system, first blower, second blower, first water inlet pump and circulating water outlet;
  • the water inlet is connected with the water outlet of the second water inlet pump, the biological carrier bed is arranged on a support plate, the biological carrier bed is arranged with biological carriers, the biological carriers are arranged irregularly, and the biological carrier bed is
  • the spacing between the limit plates forms an expansion space
  • the air distribution system is connected to the second blower
  • the water distributor is installed on the support plate
  • the aeration system is connected to the first blower
  • the circulating water outlet is connected to the first blower.
  • the water inlet of the water inlet pump is connected, and the water distribution system is connected with the water outlet of the first water inlet pump.
  • the sequencing batch biofilm granular sludge reactor is also provided with a circulating aeration tank and a water outlet, the water outlet is provided with a circulating return port, and the circulating return port is connected to the circulating aeration tank ,
  • the aeration system is arranged in the circulating aeration tank, and the circulating water outlet is arranged on the circulating aeration tank.
  • the volume of the expansion space is set to 1/50-1/20 of the volume of the biological carrier bed 9.
  • the inner circle of the biological carrier is provided with granular sludge
  • the outer circle is provided with a biofilm
  • the inner circle is provided with partition bars.
  • the biological carrier adopts a hollow particle filler with a density of less than 1 g/cm 3 , a specific surface area greater than 500 m 2 /m 3 and a porosity between 60% and 85%.
  • the support plate adopts a perforated plate, and water distributors are evenly distributed on the through holes of the support plate, and the waste water is evenly distributed along the vertical cross section of the water flow after passing through the water distributor and reacts through the biofilm particle sludge. Area.
  • the limiting plate adopts a perforated plate, the waste water enters the circulation return zone from the biofilm particle sludge reaction zone through the through holes on the limiting plate, and the size of the through holes on the limiting plate is smaller than the biological carrier size of.
  • the invention also provides a wastewater treatment method based on the biofilm granular sludge reactor, which includes the following steps:
  • Pretreatment The production wastewater passes through the grille tank and grit tank to remove impurities, and then enters the adjustment tank for balanced adjustment of water quality and quantity;
  • Coagulation sedimentation treatment The pretreated wastewater is added with coagulant when passing through the first pipeline mixer, and when passing through the second pipeline mixer, flocculant is added and mixed, and then enters the coagulation sedimentation tank for coagulation reaction. After the coagulation reaction, the wastewater is separated from the coagulation sedimentation tank, and the supernatant is extracted and enters the first intermediate pool;
  • the wastewater from the first intermediate pool enters the circulating aeration tank, and the first water inlet pump is started at the same time.
  • the wastewater in the circulating aeration tank is transported to the water distribution system through the first water inlet pump, and enters the biofilm granular sludge reactor.
  • the membrane granular sludge reactor is filled with waste water and the waste water in the circulating aeration tank reaches the set water level and stops the water inflow;
  • the present invention has the following advantages and beneficial effects:
  • the sequencing batch type biofilm granular sludge expanded bed reactor of the present invention can constitute a wastewater secondary biological treatment unit alone, or can be combined with an anaerobic reactor to form a secondary biological treatment unit, which is highly efficient and flexible, and improves overall The efficiency of wastewater biological treatment reduces the floor space.
  • the biofilm granular sludge reactor of the present invention has a high sludge concentration, and the biological carrier bed sludge concentration (TSS) reaches 20-45g/L, which is higher than the sludge of the currently commonly used activated sludge method and biofilm method Concentration, to ensure good results in wastewater treatment, and low sludge yield.
  • the remaining sludge yield is less than 0.15kgTSS/kgCOD, which is more than 60% lower than that of the activated sludge method.
  • the biological carrier of the present invention is provided with granular sludge in the inner circle and biofilm on the outer circle.
  • the formation of granular sludge is the main reason for the high concentration of sludge in the reactor.
  • the high concentration of granular sludge and biological ensures a good wastewater treatment effect.
  • the biological treatment aeration system is set in a separate circulating aeration tank, which solves the problem that the biological treatment system is easy to block the aeration system, and the maintenance of the aeration system is convenient.
  • the circulating aeration system The pond has the function of diluting and equalizing water quality, which is beneficial to improve the efficiency of wastewater treatment.
  • the biofilm granular sludge reactor of the present invention is simple and compact, highly efficient and flexible, and has strong adaptability. After the wastewater passes through the biological carrier bed, the suspended matter in the wastewater is adsorbed and intercepted by microorganisms, and then decomposed and degraded. Therefore, After the wastewater is treated by the biofilm granular sludge reactor, the concentration of suspended matter is very low, the effluent quality is stable, and no secondary settling tank is required.
  • the sequencing batch type biofilm granular sludge expanded bed reactor of the present invention is equipped with an expansion space, so that the biological carrier in the biological carrier bed is in a micro-expansion state during the wastewater treatment process, which is beneficial to the wastewater in the biofilm granular sludge.
  • the uniform distribution of the reaction zone and uniform treatment can effectively improve the efficiency of wastewater treatment.
  • FIG. 1 is a schematic structural diagram of a wastewater treatment device based on a biofilm granular sludge reactor of Embodiment 1;
  • Figure 2 is a partial enlarged view of the biological carrier bed at I in Figure 1;
  • Example 3 is a schematic diagram of the structure of the biological carrier of Example 1;
  • FIG. 4 is a schematic structural diagram of a wastewater treatment device based on a biofilm granular sludge reactor of Embodiment 2;
  • Example 5 is a schematic diagram of the structure of the biofilm granular sludge reactor of Example 3.
  • 1-biofilm granular sludge reactor 2-circulation aeration tank, 3-first feed pump, 4-distribution system, 5-support plate, 6-distributor, 7-biological carrier bed, 8 -Expansion space, 9-limiting plate, 10-outlet tank, 11-second inlet pump, 12-first blower, 13-aeration system, 14-second blower, 15-air distribution system, 16-outlet , 17- grid tank, 18- grit tank, 19- regulation tank, 20- first pipeline mixer, 21- second pipeline mixer, 22- coagulation sedimentation tank, 23- first intermediate tank, 24- The third water pump, 25-anaerobic reactor, 26-the second intermediate tank, 27-granular sludge, 28-biofilm, 29-regulation tank water pump.
  • this embodiment provides a wastewater treatment device based on a biofilm granular sludge reactor, which includes: a grid tank 17, a grit tank 18, a regulating tank 19, a regulating tank pump 29, and a first pipeline mixing Reactor 20, the second pipeline mixer 21, the coagulation sedimentation tank 22, the first intermediate tank 23 and the biofilm granular sludge reactor 1, the waste water passes through the grid tank 17 to remove coarse impurities, and then enters the grit tank 18 to remove heavy impurities , And then enter the adjustment tank 19 for balanced adjustment of water quality and quantity, add coagulant when passing through the first pipeline mixer 20, add flocculant when passing through the second pipeline mixer 21, and perform coagulation reaction in the coagulation sedimentation tank.
  • the waste water is separated from the coagulation sedimentation tank.
  • the supernatant enters the first intermediate tank 23, supplements nutrients, and adjusts the pH value with lye and acid solution, and then enters through the second inlet pump 11 Sequencing batch type biofilm granular sludge expanded bed reactor, and at the same time starting the first water inlet pump 3, the wastewater is subjected to biochemical oxidation cycle treatment in the biofilm granular sludge reactor 1.
  • the biofilm granular sludge reactor 1 is provided with a water and gas distribution zone A, a biofilm granular sludge reaction zone B, and a circulation return zone C along the wastewater treatment direction;
  • the biofilm particle sludge reaction zone B includes the support plate 5 , The biological carrier bed 7, the limiting plate 9, and the expansion space 8 formed between the biological carrier bed 7 and the limiting plate 9 arranged on the supporting plate 5;
  • the circulating return zone C is provided with a water outlet groove 10, a water outlet groove 10 is provided with a circulating return port, which is connected to the circulating aeration tank 2 through a pipeline;
  • the support plate 5 adopts a perforated plate, and the through hole of the support plate 5 is provided with a water distributor 6 so that the waste water is evenly distributed along the vertical section of the water flow and passes through the biofilm particle sludge reaction zone;
  • the limit plate 9 adopts Perforated plate, the waste water enters the circulation return zone from the biofilm granular sludge reaction zone through the through holes on the limiting plate 9.
  • the size of the through holes on the limiting plate 9 is smaller than the size of the biological carrier in the biofilm granular sludge reaction zone;
  • the circulating aeration tank 2 is provided with an aeration system 13 and a circulating water outlet.
  • the aeration system is connected to the first blower 12 through a pipe, and the circulating water outlet is connected to the water inlet of the first water inlet pump 3 through a pipe.
  • the water outlet of the first water inlet pump 3 is connected with the water distribution system 4;
  • the biofilm granular sludge reactor 1 is also provided with a backwash drain;
  • the circulating aeration tank 2 is also provided with a water inlet and a drain 16;
  • the minimum volume of the expansion space 8 is 0, and the maximum volume of the expansion space 8 is 1/10 of the volume of the biological carrier bed 7; the volume of the expansion space 8 in this embodiment is preferably set to 1 of the volume of the biological carrier bed 7. /50-1/20;
  • a certain flow rate is maintained when the wastewater passes through the biological carrier bed 7, so that the biological carrier in the biological carrier bed 7 is in a micro-expanded state, and the biological carrier expands to fill the entire space including the biological carrier bed 7 and the expansion space 8.
  • the flow rate is 1.5-15mm/s
  • the biological carrier uses hollow particle fillers with a density less than 1g/cm 3 , a specific surface area greater than 500 m 2 /m 3 and a porosity between 60% and 85%.
  • the biological carrier is in a micro-expansion state during the wastewater treatment process and is irregularly distributed in the biofilm granular sludge reaction zone B; as shown in Figure 3, the biological carrier is surrounded by granular sludge 27.
  • a biofilm 28 is formed in the outer ring, and there are partitions in the inner ring.
  • the granular sludge and biofilm are formed at the same time in the reactor.
  • biofilm is formed on the surface of the carrier.
  • the formation of granular sludge is the main reason for the high concentration of sludge in the reactor.
  • the high concentration of granular sludge and biofilm in the reactor Ensure good wastewater treatment effect.
  • Pretreatment The production wastewater passes through the grille tank 17 to remove coarse impurities, then enters the grit tank 18 to remove heavy impurities, and then enters the adjustment tank 19 for balanced adjustment of water quality and quantity;
  • the wastewater in the first intermediate pool 23 enters the circulating aeration tank 2 from the water inlet through the second water inlet pump 11, and the first water inlet pump 3 is started at the same time, and the wastewater in the circulating aeration tank 2 passes through the first water inlet pump 3 through the circulating water outlet. It is transported to the water distribution system 4 and enters the biofilm granular sludge reactor 1. When the biofilm granular sludge reactor 1 is full of wastewater and the wastewater in the circulating aeration tank 2 reaches a certain level, the water will stop entering;
  • the wastewater is paper-making coating wastewater
  • the COD of the wastewater is 3250mg/L
  • the chromaticity is 2700C.U.
  • the SS is 280mg/L;
  • the wastewater in the circulating aeration tank 2 is transported to the water distribution system 4 of the water distribution area A of the biofilm granular sludge reactor 1 through the first water inlet pump 3 through the circulation outlet, and then enters the water distribution area A.
  • the wastewater in the water distribution zone A passes through the water distributor 6 on the support plate 5 and enters the biological carrier bed 7 of the biofilm granular sludge reactor 1.
  • the wastewater undergoes biochemical oxidation treatment on the biological carrier bed 7, and then passes through the limit plate 9 Enter the recirculation zone C;
  • the waste water in the circulating return zone C enters the circulating aeration tank 2 through the pipe through the circulating return port provided in the water outlet tank 10, and the waste water in the circulating aeration tank 2 again passes through the first water inlet pump 3 through the biofilm granular sludge reactor.
  • the water and air distribution zone A, the biofilm granular sludge reaction zone B and the circulation return zone C are for wastewater treatment and circulation;
  • the volume of the expansion space 8 of the biofilm granular sludge reactor 1 is 1/20 of the volume of the biological carrier bed 7, the flow rate of wastewater in the biofilm granular sludge reactor 1 is 15mm/s, and the wastewater treatment cycle is 8h, where The aeration operation time is 5h, the hypoxia operation time is 1h, and the dissolved oxygen concentration in the biofilm particle sludge reaction zone B is 4-5mg/L during the aeration operation;
  • the first blower 12 In the wastewater treatment process, stop the first blower 12 to supply air to the circulating aeration tank 2 for a period of time, so that the wastewater is treated and circulated in anoxic state. After the wastewater is treated for a certain period of time, the first inlet pump 3 and the first blower 12 are stopped In operation, 30% of the total wastewater in the biofilm granular sludge reactor 1 and the circulating aeration tank 2 is discharged from the reactor through the drainage port 16. After the treatment, the COD of the wastewater is 115mg/L, and the color is 25C.U., SS is 28mg/L.
  • the biological carrier can be backwashed through the second blower 14 and the air distribution system 15, and the backwashed wastewater is discharged from the reactor through the backwash drain port and transported to the regulating tank 19, and the pretreated The wastewater is treated with coagulation and sedimentation together.
  • the PAC addition amount is 200mg/L
  • CPAM addition amount is 4mg/L
  • the volume of the expansion space of the biofilm granular sludge reactor is 1/50 of the volume of the biological carrier bed
  • the flow rate of the wastewater in the biological carrier bed The wastewater treatment cycle is 8h, and the aeration operation time is 4h, the hypoxia operation time is 2h, and the dissolved oxygen concentration in the biofilm particle sludge reaction zone B is 4-5mg/L during aeration operation.
  • the COD of wastewater is 205mg/L
  • the color is 78C.U.
  • the SS is 34mg/L;
  • the PAC addition amount is 300mg/L
  • the CPAM addition amount is 5mg/L
  • the volume of the expansion space of the biofilm granular sludge reactor is 1/40 of the volume of the biological carrier bed
  • the flow rate of the wastewater in the biological carrier bed The wastewater treatment cycle is 8h
  • the aeration operation time is 5h
  • the hypoxia operation time is 1h
  • the dissolved oxygen concentration in the biofilm particle sludge reaction zone B is 4-5mg/L during aeration operation.
  • the COD of wastewater is 124mg/L
  • the chromaticity is 43C.U.
  • the SS is 36mg/L;
  • the wastewater used in this example is secondary fiber papermaking wastewater.
  • the COD of the wastewater is 4590 ⁇ 80mg/L, the chromaticity is 1070 ⁇ 50 C.U., and the SS is 160 ⁇ 15mg/L; based on the volume of the wastewater, the PAC addition amount is 400mg /L, the amount of CPAM added is 6mg/L, the volume of the expansion space is set to 1/40 of the volume of the biological carrier bed 7, the flow rate of wastewater in the biological carrier bed is 7mm/s, and the wastewater treatment cycle is 8h, where aeration The running time is 3h, the anoxic running time is 3h, the dissolved oxygen concentration in the biofilm granular sludge reaction zone B during aeration operation is 4-5mg/L, the treated wastewater COD is 220 ⁇ 40mg/L, the color is 25 ⁇ 5C.U., SS is 10 ⁇ 4mg/L.
  • this embodiment provides a wastewater treatment device based on a biofilm granular sludge reactor, including: a grid tank 17, a grit tank 18, a regulating tank 19, a first pipeline mixer 20, and a second Pipe mixer 21, coagulation sedimentation tank 22, first intermediate tank 23, third water pump 24, anaerobic reactor 25, second intermediate tank 26 and biofilm granular sludge reactor 1, waste water is removed through grid tank 17 Coarse impurities, then enter the grit chamber 18 to remove heavy impurities, and then enter the adjustment tank 19 for balanced adjustment of water quality and quantity.
  • the coagulation reaction is carried out in the coagulation sedimentation tank, the wastewater after the coagulation reaction for a period of time is separated from the coagulation sedimentation tank, the supernatant enters the first intermediate pool 23, supplemented with nutrients, and adjusted with lye and acid solution
  • the pH value then enters the anaerobic reactor 25 through the third water pump 24, enters the second intermediate water tank 26 after anaerobic reaction, adds nutrients again, and adjusts the pH value with lye and acid solution, and then passes through the second water inlet pump 11 Enter the sequencing batch biofilm granular sludge expanded bed reactor, and at the same time start the first water inlet pump 3, and the wastewater is subjected to biochemical oxidation cycle treatment in the biofilm granular sludge reactor 1.
  • the sequencing batch biofilm granular sludge expanded bed reactor can form a wastewater secondary biological treatment unit alone, or can be combined with an anaerobic reactor to form a secondary biological treatment unit, which is highly efficient and flexible, and improves overall The efficiency of wastewater biological treatment reduces the floor space.
  • the biofilm granular sludge reactor in Example 1 can also adopt an integrated structure, and the aeration system is separately arranged in the circulating return zone C, which can also achieve convenient maintenance and reduce floor space. purpose.
  • the biofilm granular sludge reactor of this embodiment is sequentially provided with a water and gas distribution zone, a biofilm granular sludge reaction zone and a circulation return zone along the wastewater treatment flow direction;
  • the biofilm granular sludge reaction zone includes a supporting plate 5, a biological carrier bed 7, a limiting plate 9 and an expansion space 8.
  • the biological carrier bed 7 is arranged on the supporting plate 5, and the distance between the biological carrier bed 7 and the limiting plate 9 An expansion space is formed;
  • the water distribution area is provided with a water distribution system 4, an air distribution system 15, a water distributor 6 and a second blower 14.
  • the air distribution system 15 is connected to the second blower 14, and the water distributor 6 is installed on the support plate 5 on;
  • the circulating return zone is provided with an aeration system 13, a first blower 12, a first water inlet pump 3 and a circulating water outlet.
  • the circulating water outlet is connected to the water inlet of the first water inlet pump 3, and the water distribution system 4 is connected to the first inlet
  • the water outlet of the water pump 3 is connected, and the aeration system 13 is connected to the first blower 12.
  • the sequencing batch type biofilm granular sludge expanded bed reactor of this embodiment is also provided with a water inlet, a drain 16 and a backwash drain.
  • the water inlet of this embodiment is set in the circulating return zone C.
  • the water inlet and the second inlet The water pump 11 is connected, the drain 16 is set in the biofilm particle sludge reaction zone B, and the backwash drain is set in the water and air distribution zone A.

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Abstract

本发明公开了一种基于生物膜颗粒污泥反应器的废水处理装置及其方法，该装置包括：格栅池、沉砂池、调节池、调节池水泵、第一管道混合器、第二管道混合器、混凝沉淀池、第一中间水池和序批式生物膜颗粒污泥膨胀床反应器；格栅池出口与沉砂池入口连接，沉砂池出口与调节池入口连接，调节池出口通过调节池水泵与第一管道混合器连接，第一管道混合器混合有混凝剂，并与第二管道混合器连接，第二管道混合器混合有絮凝剂，并与混凝沉淀池入口连接，混凝沉淀池出口与第一中间水池入口连接，第一中间水池出口与序批式生物膜颗粒污泥膨胀床反应器连接。本发明构成废水二级生物处理单元，提高了废水生物处理的效率、运行成本低、结构紧凑、减少了占地面积。

Description

一种基于生物膜颗粒污泥反应器的废水处理装置及其方法 技术领域
本发明涉及废水处理技术领域，具体涉及一种基于生物膜颗粒污泥反应器的废水处理装置及其方法。
背景技术
为了避免工业废水污染对人类健康和生态环境造成严重危害，为了改善人民生活和生态环境，工业废水须经过处理及检测达标后才能排放。当前，工业废水处理的主要方法有物理方法、化学方法、物化方法和生物方法等，现有的废水生物处理方法普遍存在如下弊端：工艺流程复杂，需要较大的占地面积和较高的基建投资；微生物浓度低，污泥易于膨胀；对水质、水量的变化适应性差；氧传递效率低，动力消耗量大；运行的维护和管理难度大；实时在线自动化控制程度低，能耗高。如何更好地解决传统废水处理工艺中存在的问题，提高生物处理工艺的能效，是废水处理技术研究的重点和趋势。
发明内容
为了克服现有技术存在的缺陷与不足，本发明提供一种基于生物膜颗粒污泥反应器的废水处理装置及其方法，提高了废水生物处理的效率，同时减少了处理成本。
为了达到上述目的，本发明采用以下技术方案：
本发明提供一种基于生物膜颗粒污泥反应器的废水处理装置，包括：格栅池、沉砂池、调节池、调节池水泵、第一管道混合器、第二管道混合器、混凝沉淀池、第一中间水池和序批式生物膜颗粒污泥膨胀床反应器；
所述格栅池出口与沉砂池入口连接，所述沉砂池出口与调节池入口连接，所述调节池出口通过调节池水泵与第一管道混合器连接，所述第一管道混合器混合有混凝剂，并与第二管道混合器连接，所述第二管道混合器混合有絮凝剂， 并与混凝沉淀池入口连接，所述混凝沉淀池出口与第一中间水池入口连接，所述第一中间水池出口与序批式生物膜颗粒污泥膨胀床反应器连接。
作为优选的技术方案，还设有厌氧反应器和第二中间水池，所述厌氧反应器入口与第一中间水池出口连接，所述厌氧反应器出口与第二中间水池入口连接，所述第二中间水池出口与序批式生物膜颗粒污泥膨胀床反应器连接。
作为优选的技术方案，所述序批式生物膜颗粒污泥膨胀床反应器设有：进水口、支撑板、生物载体床、限位板、布水系统、布气系统、布水器、曝气系统、第一鼓风机、第二鼓风机、第一进水泵和循环出水口；
所述进水口与第二进水泵的出水口连接，所述生物载体床设置在支撑板上，所述生物载体床设置有生物载体，所述生物载体无规律分散布置，所述生物载体床与限位板的间隔形成膨胀空间，所述布气系统与第二鼓风机连接，所述布水器安装在支撑板上，所述曝气系统与第一鼓风机连接，所述循环出水口与第一进水泵的进水口连接，所述布水系统与第一进水泵的出水口连接。
作为优选的技术方案，所述序批式生物膜颗粒污泥反应器还设有循环曝气池和出水槽，所述出水槽设置有循环回流口，所述循环回流口与循环曝气池连接，所述曝气系统设置在循环曝气池内，所述循环出水口设置在循环曝气池上。
作为优选的技术方案，所述膨胀空间的容积设置为生物载体床9容积的1/50-1/20。
作为优选的技术方案，所述生物载体内圈设有颗粒污泥，外圈设有生物膜，内圈内设有分隔条。
作为优选的技术方案，所述生物载体采用密度小于1g/cm 3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
作为优选的技术方案，所述支撑板采用多孔板，所述支撑板的通孔上均匀分布设置布水器，废水经布水器后沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区。
作为优选的技术方案，所述限位板采用多孔板，废水经限位板上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位板上的通孔尺寸小于所述生物载体的尺寸。
本发明还提供一种基于生物膜颗粒污泥反应器的废水处理方法，包括下述步骤：
S1：预处理：生产废水经过格栅池、沉砂池去除杂质，然后进入调节池，进行水质水量的均衡调节；
S2：混凝沉淀处理：经预处理后的废水经过第一管道混合器时加入混凝剂，经过第二管道混合器时加入絮凝剂，并进行混合，进入混凝沉淀池进行混凝反应，混凝反应后废水在混凝沉淀池内产生泥水分离，提取上清液进入第一中间水池；
S3：在第一中间水池内加入营养盐，并用碱液、酸溶液调节pH值，废水进入生物膜颗粒污泥反应器进行生物化学氧化处理：
S31：第一中间水池的废水进入循环曝气池，同时启动第一进水泵，循环曝气池中的废水经第一进水泵输送到布水系统，进入生物膜颗粒污泥反应器，当生物膜颗粒污泥反应器充满废水且循环曝气池中废水到达设定的水位后停止进水；
S32：进水完成后，启动第一鼓风机，通过曝气系统对循环曝气池中的废水进行曝气，循环曝气池中的废水输送到生物膜颗粒污泥反应器的布水布气区，接着废水进入生物载体床进行生物化学氧化处理，然后进入循环回流区，循环回流区的废水通过循环回流口进入循环曝气池；在废水处理的过程中，循环曝气池中的废水依次通过生物膜颗粒污泥反应器的布水布气区、生物膜颗粒污泥反应区和循环回流区，进行废水的循环处理；
S33：在废水的循环处理中，停止向循环曝气池供气一段时间，废水在缺氧状态下进行循环处理；进行循环处理一段时间后，停止第一进水泵和第一鼓风 机运行，通过排水口将一定比例废水排出反应器，返回执行步骤S31；
S4：通过第二鼓风机和布气系统对生物载体进行反冲洗，通过反冲洗排水口将反冲洗后的废水排出反应器，并输送到调节池，和经过预处理的废水一起进行混凝沉淀处理。
本发明与现有技术相比，具有如下优点和有益效果：
(1)本发明的序批式生物膜颗粒污泥膨胀床反应器可以单独构成废水二级生物处理单元，也可以和厌氧反应器联用组成二级生物处理单元，高效灵活，整体提高了废水生物处理的效率，减少了占地面积。
(2)本发明的生物膜颗粒污泥反应器污泥浓度高，生物载体床污泥浓度(TSS)达到20-45g/L，高于目前常用的活性污泥法和生物膜法的污泥浓度，保证废水处理获得良好的效果，并且污泥产率低，剩余污泥产率小于0.15kgTSS/kgCOD，比活性污泥法的剩余污泥产率低60％以上。
(3)本发明的生物载体内圈设有颗粒污泥，外圈设有生物膜，颗粒污泥的形成是反应器具有高污泥浓度的主要原因，反应器中高浓度的颗粒污泥和生物膜保证了良好的废水处理效果。
(4)本发明将生物处理的曝气系统设置在单独的循环曝气池中，解决了生物处理系统普遍存在的曝气系统容易堵塞的问题，且曝气系统维护方便，同时，循环曝气池具有稀释、均衡水质的作用，有利于提高废水处理效率。
(5)本发明的生物膜颗粒污泥反应器简洁紧凑、高效灵活、适应性强，废水在通过生物载体床后，废水中的悬浮物被微生物吸附、截留，然后被分解、降解，因此，废水经生物膜颗粒污泥反应器处理后悬浮物浓度很低，出水质量稳定，不需要二沉池。
(6)本发明的序批式生物膜颗粒污泥膨胀床反应器设置了膨胀空间，使废水处理过程中生物载体床中的生物载体处于微膨胀化状态，有利于废水在生物膜颗粒污泥反应区的均匀分布，受到均匀的处理，有效提高了废水处理的效率。
附图说明
图1为本实施例1的基于生物膜颗粒污泥反应器的废水处理装置的结构示意图；
图2为图1中I处生物载体床的局部放大图；
图3为本实施例1的生物载体结构示意图；
图4为本实施例2的基于生物膜颗粒污泥反应器的废水处理装置的结构示意图；
图5为本实施例3的生物膜颗粒污泥反应器的结构示意图。
其中，1-生物膜颗粒污泥反应器，2-循环曝气池，3-第一进水泵，4-布水系统，5-支撑板，6-布水器，7-生物载体床，8-膨胀空间，9-限位板，10-出水槽，11-第二进水泵，12-第一鼓风机，13-曝气系统，14-第二鼓风机，15-布气系统，16-排水口，17-格栅池，18-沉砂池，19-调节池，20-第一管道混合器，21-第二管道混合器，22-混凝沉淀池，23-第一中间水池，24-第三水泵，25-厌氧反应器，26-第二中间水池，27-颗粒污泥，28-生物膜，29-调节池水泵。
具体实施方式
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图及实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅仅用以解释本发明，并不用于限定本发明。
实施例1
如图1所示，本实施例提供一种基于生物膜颗粒污泥反应器的废水处理装置，包括：格栅池17、沉砂池18、调节池19、调节池水泵29、第一管道混合器20、第二管道混合器21、混凝沉淀池22、第一中间水池23和生物膜颗粒污泥反应器1，废水经过格栅池17去除粗大杂质，再进入沉砂池18去除重杂质，然后进入调节池19，进行水质水量的均衡调节，经过第一管道混合器20时添加混凝剂，经过第二管道混合器21时添加絮凝剂，在混凝沉淀池内进行混凝反应，混凝反应一段时间后的废水在混凝沉淀池内产生泥水分离，上清液进入第一中间水池23，补加营养盐，并用碱液、酸溶液调节PH值，然后通过第二进水泵11进入到序批式生物膜颗粒污泥膨胀床反应器，同时启动第一进水泵3，废水在生物膜颗粒污泥反应器1内进行生物化学氧化循环处理。
在本实施例中，生物膜颗粒污泥反应器1沿废水处理方向设置有布水布气区A、生物膜颗粒污泥反应区B和循环回流区C；布水布气区A设有布水系统4、布气系统15、安装在支撑板5上的布水器6，所述布气系统15通过管道和第二鼓风机14连接；所述生物膜颗粒污泥反应区B包括支撑板5、设置在支撑板5上面的生物载体床7、限位板9、以及生物载体床7与限位板9之间形成的膨胀空间8；所述循环回流区C设置有出水槽10，出水槽10设置有循环回流口，循环回流口通过管道与循环曝气池2连接；
在本实施例中，支撑板5采用多孔板，支撑板5的通孔上设置布水器6，使废水沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区；限位板9采用多孔板，废水经限位板9上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位板9上的通孔尺寸小于生物膜颗粒污泥反应区中的生物载体的尺寸；
在本实施例中，循环曝气池2设置有曝气系统13和循环出水口，曝气系统通过管道和第一鼓风机12连接，循环出水口通过管道与第一进水泵3的进水口 连接，第一进水泵3的出水口与布水系统4连接；
在本实施例中，生物膜颗粒污泥反应器1上还设置有反冲洗排水口；循环曝气池2上还设置有进水口和排水口16；
在本实施例中，膨胀空间8的最小容积为0，膨胀空间8的最大容积是生物载体床7容积的1/10；本实施例膨胀空间8的容积优选设置为生物载体床7容积的1/50-1/20；
在本实施例中，维持废水通过生物载体床7时一定的流速，使生物载体床7中的生物载体处于微膨胀化状态，生物载体膨胀充满了包括生物载体床7和膨胀空间8的整个空间，优选流速为1.5-15mm/s，生物载体采用密度小于1g/cm 3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
如图2所示，生物载体在废水处理过程中处于微膨胀化状态，无规律分布在生物膜颗粒污泥反应区B内；如图3所示，生物载体内圈设有颗粒污泥27，外圈形成生物膜28，内圈内设有分隔条，反应器同时形成了颗粒污泥和生物膜，颗粒污泥和生物膜同时存在好氧、兼氧和厌氧微生物群落；当反应器污泥驯化完成后，生物载体中产生了颗粒污泥，而载体表面形成了生物膜，颗粒污泥的形成是反应器具有高污泥浓度的主要原因，反应器中高浓度的颗粒污泥和生物膜保证了良好的废水处理效果。
本实施例具体的废水处理步骤如下所述：
S1：预处理：生产废水经过格栅池17去除粗大杂质，再进入沉砂池18去除重杂质，然后进入调节池19，进行水质水量的均衡调节；
S2：混凝沉淀处理：经预处理后的废水经过第一管道混合器20和第二管道混合器21，并先后依次加入400mg/L的聚合氯化铝(PAC)和6mg/L阳离子聚丙烯酰胺(CPAM)，搅拌使废水中的PAC和CPAM混合均匀，进入混凝沉淀池22 进行混凝反应，反应后废水在混凝沉淀池22内产生泥水分离，提取上清液进入第一中间水池23，沉淀在混凝沉淀池底部的污泥经脱水干化后外运，进行进一步的无害化、稳定化和资源化处理处置；
S3：废水在第一中间水池23中补加生物处理所需营养盐等，并用碱液、酸溶液调节pH值，废水进入生物膜颗粒污泥反应器1进行生物化学氧化处理：
1)进水
第一中间水池23中的废水通过第二进水泵11从进水口进入循环曝气池2，同时启动第一进水泵3，循环曝气池2中的废水通过循环出水口经第一进水泵3输送到布水系统4，进入生物膜颗粒污泥反应器1，当生物膜颗粒污泥反应器1充满废水且循环曝气池2中废水到达一定水位后停止进水；
本实施例中，废水采用造纸涂布废水，废水COD为3250mg/L，色度为2700C.U.，SS为280mg/L；
2)废水的处理和循环
进水完成后，启动第一鼓风机12通过曝气系统13对循环曝气池2中的废水进行曝气；
循环曝气池2中的废水通过循环出水口经第一进水泵3输送到生物膜颗粒污泥反应器1的布水布气区A的布水系统4，进入布水布气区A，布水布气区A的废水通过支撑板5上的布水器6，进入生物膜颗粒污泥反应器1的生物载体床7，废水在生物载体床7进行生物化学氧化处理，然后经过限位板9进入循环回流区C；
循环回流区C中的废水通过设置在出水槽10的循环回流口经管道进入循环曝气池2，循环曝气池2中的废水再次经第一进水泵3依次通过生物膜颗粒污泥反应器1的布水布气区A、生物膜颗粒污泥反应区B和循环回流区C，进行废水 的处理和循环；
生物膜颗粒污泥反应器1的膨胀空间8的容积为生物载体床7容积的1/20，废水在生物膜颗粒污泥反应器1的流速为15mm/s，废水一个处理周期为8h，其中曝气运行时间为5h，缺氧运行时间为1h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L；
3)排水
在废水处理过程中，停止第一鼓风机12向循环曝气池2供气一段时间，使废水在缺氧状态下处理和循环，废水处理一定时间后，停止第一进水泵3和第一鼓风机12运行，通过排水口16将生物膜颗粒污泥反应器1和循环曝气池2中废水总量的30％排出反应器，经处理后废水COD为115mg/L，色度为25C.U.，SS为28mg/L。
处理废水一段时间后，可以通过第二鼓风机14和布气系统15对生物载体进行反冲洗，通过反冲洗排水口将反冲洗后的废水排出反应器，并输送到调节池19，和经过预处理的废水一起进行混凝沉淀处理。
在本实施例中，通过改变PAC加入量、CPAM加入量、生物膜颗粒污泥反应器膨胀空间的容积、废水在生物膜颗粒污泥反应器的流速、曝气运行时间和缺氧运行时间等参数，可以得到不同的废水处理效果，具体如下所述：
以废水体积计，PAC加入量为200mg/L，CPAM加入量为4mg/L，生物膜颗粒污泥反应器的膨胀空间的容积为生物载体床容积的1/50，废水在生物载体床的流速为1.5mm/s，废水一个处理周期为8h，其中曝气运行时间为4h，缺氧运行时间为2h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后废水COD为205mg/L，色度为78C.U.，SS为34mg/L；
以废水体积计，PAC加入量为300mg/L，CPAM加入量为5mg/L，生物膜颗粒污泥反应器的膨胀空间的容积为生物载体床容积的1/40，废水在生物载体床的流速为8mm/s，废水一个处理周期为8h，其中曝气运行时间为5h，缺氧运行时间为1h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后废水COD为124mg/L，色度为43C.U.，SS为36mg/L；
本实施例采用的废水为二次纤维造纸废水，废水COD为4590±80mg/L，色度为1070±50C.U.，SS为160±15mg/L；以废水体积计，PAC加入量为400mg/L，CPAM加入量为6mg/L，将膨胀空间的容积设置为生物载体床7容积的1/40，废水在生物载体床的流速为7mm/s，废水一个处理周期为8h，其中曝气运行时间为3h，缺氧运行时间为3h，曝气运行时生物膜颗粒污泥反应区B溶解氧浓度为4-5mg/L，经处理后废水COD为220±40mg/L，色度为25±5C.U.，SS为10±4mg/L。
实施例2
本实施例2的技术方案除了下述技术特征外，其它技术方案与实施例1相同：
如图4所示，本实施例提供一种基于生物膜颗粒污泥反应器的废水处理装置，包括：格栅池17、沉砂池18、调节池19、第一管道混合器20、第二管道混合器21、混凝沉淀池22、第一中间水池23、第三水泵24、厌氧反应器25、第二中间水池26和生物膜颗粒污泥反应器1，废水经过格栅池17去除粗大杂质，再进入沉砂池18去除重杂质，然后进入调节池19，进行水质水量的均衡调节，经过第一管道混合器20时添加混凝剂，经过第二管道混合器21时添加絮凝剂，在混凝沉淀池内进行混凝反应，混凝反应一段时间后的废水在混凝沉淀池内产生泥水分离，上清液进入第一中间水池23，补加营养盐，并用碱液、酸溶液调 节pH值，然后经过第三水泵24进入到厌氧反应器25，进行厌氧反应后进入第二中间水池26，再次添加营养盐，并用碱液、酸溶液调节pH值，然后通过第二进水泵11进入序批式生物膜颗粒污泥膨胀床反应器，同时启动第一进水泵3，废水在生物膜颗粒污泥反应器1内进行生物化学氧化循环处理。
在本实施例中，序批式生物膜颗粒污泥膨胀床反应器可以单独构成废水二级生物处理单元，也可以和厌氧反应器联用组成二级生物处理单元，高效灵活，整体提高了废水生物处理的效率，减少了占地面积。
实施例3
本实施例3的技术方案除了下述技术特征外，其它技术方案与实施例1相同：
如图5所示，实施例1中的生物膜颗粒污泥反应器也可以采用一体式结构，并且将曝气系统单独设置在循环回流区C，也能达到方便维护、减少了占地面积的目的。
本实施例的生物膜颗粒污泥反应器沿废水处理流向上依次设置有布水布气区、生物膜颗粒污泥反应区和循环回流区；
其中，生物膜颗粒污泥反应区包括支撑板5、生物载体床7、限位板9和膨胀空间8，生物载体床7设置在支撑板5上，生物载体床7与限位板9的间隔形成膨胀空间；布水布气区设置有布水系统4、布气系统15、布水器6和第二鼓风机14，布气系统15与第二鼓风机14连接，布水器6安装在支撑板5上；循环回流区设置有曝气系统13、第一鼓风机12、第一进水泵3和循环出水口，循环出水口与第一进水泵3的进水口连接，布水系统4与第一进水泵3的出水口连接，曝气系统13与第一鼓风机12连接。
本实施例的序批式生物膜颗粒污泥膨胀床反应器上还设置有进水口、排水口16和反冲洗排水口，本实施例进水口设在循环回流区C，进水口与第二进水泵11连接，排水口16设在生物膜颗粒污泥反应区B，反冲洗排水口设在布水布气区A。
上述实施例为本发明较佳的实施方式，但本发明的实施方式并不受上述实施例的限制，其他的任何未背离本发明的精神实质与原理下所作的改变、修饰、替代、组合、简化，均应为等效的置换方式，都包含在本发明的保护范围之内。

Claims (10)

  1. 一种基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，包括：格栅池、沉砂池、调节池、调节池水泵、第一管道混合器、第二管道混合器、混凝沉淀池、第一中间水池和序批式生物膜颗粒污泥膨胀床反应器；
    所述格栅池出口与沉砂池入口连接，所述沉砂池出口与调节池入口连接，所述调节池出口通过调节池水泵与第一管道混合器连接，所述第一管道混合器混合有混凝剂，并与第二管道混合器连接，所述第二管道混合器混合有絮凝剂，并与混凝沉淀池入口连接，所述混凝沉淀池出口与第一中间水池入口连接，所述第一中间水池出口与序批式生物膜颗粒污泥膨胀床反应器连接。
  2. 根据权利要求1所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，还设有厌氧反应器和第二中间水池，所述厌氧反应器入口与第一中间水池出口连接，所述厌氧反应器出口与第二中间水池入口连接，所述第二中间水池出口与序批式生物膜颗粒污泥膨胀床反应器连接。
  3. 根据权利要求1或2所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述序批式生物膜颗粒污泥膨胀床反应器设有：进水口、支撑板、生物载体床、限位板、布水系统、布气系统、布水器、曝气系统、第一鼓风机、第二鼓风机、第一进水泵和循环出水口；
    所述进水口与第二进水泵的出水口连接，所述生物载体床设置在支撑板上，所述生物载体床设置有生物载体，所述生物载体无规律分散布置，所述生物载体床与限位板的间隔形成膨胀空间，所述布气系统与第二鼓风机连接，所述布水器安装在支撑板上，所述曝气系统与第一鼓风机连接，所述循环出水口与第一进水泵的进水口连接，所述布水系统与第一进水泵的出水口连接。
  4. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述序批式生物膜颗粒污泥反应器还设有循环曝气池和出水槽，所述出水槽设置有循环回流口，所述循环回流口与循环曝气池连接，所述曝气系统设置在循环曝气池内，所述循环出水口设置在循环曝气池上。
  5. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述膨胀空间的容积设置为生物载体床9容积的1/50-1/20。
  6. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述生物载体内圈设有颗粒污泥，外圈设有生物膜，内圈内设有分隔条。
  7. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述生物载体采用密度小于1g/cm 3、比表面积大于500m 2/m 3和孔隙率介于60％和85％之间的中空颗粒填料。
  8. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述支撑板采用多孔板，所述支撑板的通孔上均匀分布设置布水器，废水经布水器后沿水流垂直的截面均匀分布并通过生物膜颗粒污泥反应区。
  9. 根据权利要求3所述的基于生物膜颗粒污泥反应器的废水处理装置，其特征在于，所述限位板采用多孔板，废水经限位板上的通孔从生物膜颗粒污泥反应区进入循环回流区，限位板上的通孔尺寸小于所述生物载体的尺寸。
  10. 一种基于生物膜颗粒污泥反应器的废水处理方法，其特征在于，包括下述步骤：
    S1：预处理：生产废水经过格栅池、沉砂池去除杂质，然后进入调节池，进行水质水量的均衡调节；
    S2：混凝沉淀处理：经预处理后的废水经过第一管道混合器时加入混凝剂，经过第二管道混合器时加入絮凝剂，并进行混合，进入混凝沉淀池进行混凝反应，混凝反应后废水在混凝沉淀池内产生泥水分离，提取上清液进入第一中间水池；
    S3：在第一中间水池内加入营养盐，并用碱液、酸溶液调节pH值，废水进入生物膜颗粒污泥反应器进行生物化学氧化处理：
    S31：第一中间水池的废水进入循环曝气池，同时启动第一进水泵，循环曝 气池中的废水经第一进水泵输送到布水系统，进入生物膜颗粒污泥反应器，当生物膜颗粒污泥反应器充满废水且循环曝气池中废水到达设定的水位后停止进水；
    S32：进水完成后，启动第一鼓风机，通过曝气系统对循环曝气池中的废水进行曝气，循环曝气池中的废水输送到生物膜颗粒污泥反应器的布水布气区，接着废水进入生物载体床进行生物化学氧化处理，然后进入循环回流区，循环回流区的废水通过循环回流口进入循环曝气池；在废水处理的过程中，循环曝气池中的废水依次通过生物膜颗粒污泥反应器的布水布气区、生物膜颗粒污泥反应区和循环回流区，进行废水的循环处理；
    S33：在废水的循环处理中，停止向循环曝气池供气一段时间，废水在缺氧状态下进行循环处理；进行循环处理一段时间后，停止第一进水泵和第一鼓风机运行，通过排水口将一定比例废水排出反应器，返回执行步骤S31；
    S4：通过第二鼓风机和布气系统对生物载体进行反冲洗，通过反冲洗排水口将反冲洗后的废水排出反应器，并输送到调节池，和经过预处理的废水一起进行混凝沉淀处理。
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