WO2019128474A1 - 深度污水处理系统以及污水处理方法 - Google Patents

深度污水处理系统以及污水处理方法 Download PDF

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Publication number
WO2019128474A1
WO2019128474A1 PCT/CN2018/114153 CN2018114153W WO2019128474A1 WO 2019128474 A1 WO2019128474 A1 WO 2019128474A1 CN 2018114153 W CN2018114153 W CN 2018114153W WO 2019128474 A1 WO2019128474 A1 WO 2019128474A1
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WIPO (PCT)
Prior art keywords
sewage
water
ozone
sewage treatment
processing unit
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PCT/CN2018/114153
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English (en)
French (fr)
Inventor
张潇源
魏卡佳
黄霞
曹效鑫
梁鹏
Original Assignee
清华大学
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Priority claimed from CN201711477365.3A external-priority patent/CN108002660B/zh
Priority claimed from CN201721922235.1U external-priority patent/CN208022860U/zh
Application filed by 清华大学 filed Critical 清华大学
Publication of WO2019128474A1 publication Critical patent/WO2019128474A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present application relates to the field of sewage treatment, and in particular to a deep sewage treatment system and a sewage treatment method.
  • Ozone catalytic oxidation method utilizes hydroxyl radicals ( ⁇ OH) generated by ozonolysis to oxidize and decompose refractory organic matter in sewage. It has the advantages of strong oxidizing ability, weak selectivity and no secondary pollution. Ozone oxidation is an effective method. Advanced treatment of sewage.
  • the present application proposes a sewage treatment system.
  • the sewage treatment system includes: a water inlet tank; an ozone fluidized bed processing unit, the ozone fluidized bed processing unit is connected to the water inlet tank, and includes: a first casing; a ceramic membrane module, the ceramic membrane module Vertically disposed in the first housing, the ceramic membrane assembly includes one or more ceramic membranes, and the ceramic membrane assembly is reserved between a sidewall, a top surface, and a bottom surface of the first housing a first water flow passage communicating with each other; a first water inlet, the first water inlet is disposed at an upper portion of the first casing, and the first water inlet can utilize the ceramic membrane module and the first shell
  • the first water flow channel between the sidewalls of the body supplies sewage into the ceramic membrane module; a first water outlet, the first water outlet is disposed at an upper portion of the first casing, and The first water inlet is oppositely disposed; and the first aeration port is disposed at a bottom of the first casing
  • the sewage treatment system is not only simple and compact in structure, small in floor space, low in sludge expansion rate, high in mass transfer efficiency, high in quality and stable in effluent, but also capable of reducing membrane pollution, reducing energy consumption and sewage treatment cost, and
  • the sewage treatment system can flexibly select the sewage treatment unit according to the quality of the incoming water, which is convenient to operate and has strong applicability.
  • the ceramic membrane module further includes a membrane module housing having four side walls between the four side walls and a side wall of the first housing A first water flow channel is reserved.
  • the membrane module housing can further support and fix the ceramic membrane, and sewage can be circulated and flowed on the four sides between the membrane module housing and the first water flow passage, thereby further enhancing mass transfer and improving The mass transfer rate in the ozone fluidized bed processing unit.
  • the ceramic membrane module further includes: a baffle disposed between the plurality of the ceramic membranes.
  • the baffle plate can define a plurality of flow channels between the ceramic membranes, further enhancing mass transfer, improving the mass transfer rate in the ozone fluidized bed processing unit, and making the effluent more stable and stable.
  • the ozone fluidized bed processing unit further comprises: a first catalyst inlet, the first catalyst inlet being disposed on the first housing.
  • the first catalyst can be provided into the first casing through the first catalyst inlet to promote the catalytic oxidative decomposition of the organic matter in the sewage, so that the effluent is more excellent.
  • the ozone fluidized bed processing unit further comprises: a hydrogen peroxide inlet, the hydrogen peroxide inlet being disposed on the first housing.
  • hydrogen peroxide can be supplied into the first casing through the hydrogen peroxide inlet, and the organic matter in the sewage can be jointly oxidized by ozone and hydrogen peroxide, thereby further improving the oxidative decomposition efficiency of the organic matter in the sewage and improving the effluent water quality.
  • the ozone fluidized bed processing unit further comprises: an ultraviolet illumination device adapted to illuminate the ceramic membrane module with ultraviolet light.
  • the ultraviolet light can promote ozone to generate hydroxyl radicals, further improve the ozone oxidation decomposition efficiency of the organic matter in the sewage, and improve the effluent water quality.
  • the top of the separator is provided with a second water circulation hole.
  • the sewage treated through the membrane filtration space may be passed over the partition and flowed from the second water circulation hole into the biological reaction space, and then passed through the first water at the bottom of the partition
  • the flow holes are returned to the membrane filtration space to form an inner circulation flow.
  • the sewage flows upward from the bottom of the membrane filtration space, can wash the surface of the membrane module to reduce membrane fouling, and the internal circulation flow energy will fall off from the surface of the biological carrier filler and enter the membrane filtration through the first water circulation hole.
  • the free microorganisms in the space are returned to the biological reaction space and re-fixed, thereby reducing free microorganisms in the membrane filtration space, further reducing membrane fouling, and reducing the water discharge pressure and operating cost.
  • the bioreaction space has a first partition, the first partition is vertically disposed in the biological reaction space, and the first partition a second water flow channel is reserved between the top of the second housing and the second housing, or between the bottom of the first partition and the second housing, the second housing, the first Between the partition and the partition, a rising flow region and a downflow region are sequentially arranged.
  • the sewage can be flow-flowed in the biological reaction space, which increases the contact area between the sewage and the bio-carrier filler, thereby improving the sewage treatment efficiency.
  • the biofilm assembly processing unit further comprises a plurality of the first spacers arranged in parallel.
  • the biological reaction space includes a plurality of sequentially arranged upflow zones and a downflow zone, and the sewage can be flow-flowed in the plurality of sequentially arranged upflow zones and the downflow zone, further increasing The contact area between the sewage and the bio-carrier filler further improves the sewage treatment efficiency.
  • the volume of the upflow zone is smaller than the volume of the downflow zone. Therefore, the flow rate of the sewage in the downflow zone is relatively slow, which is favorable for forming an anaerobic or anoxic environment in the downflow zone, so that the microorganisms can treat the sewage by anaerobic or anoxic treatment, thereby further improving the sewage treatment efficiency.
  • the biofilm combination processing unit further includes: a plurality of second aeration ports, the second aeration ports being located at a bottom of at least one of the upflow zone and the downflow zone.
  • the dissolved oxygen content in the upflow zone and the downflow zone can be easily adjusted, which is advantageous in the upflow zone and the drop as needed.
  • Aerobic, anoxic and anaerobic environments are formed in the flow zone so that the microorganisms can treat the sewage aerobic, anoxic or anaerobic, further improving the effluent water quality, and the gas-water lift generated by the aeration also contributes to the upflow zone.
  • the sewage in the flow flows upwards.
  • the biofilm combination processing unit further includes: a plurality of auxiliary first water inlets disposed at a top of the bioreactor space and located in the downflow region.
  • the second water flow passage between the first partition and the second housing is arranged to be closable. Therefore, the flow path of the sewage in the biological reaction space can be easily controlled as needed.
  • the biofilm combination processing unit further includes: a return water outlet disposed at a bottom of the downflow region adjacent to the membrane filtration space; and a return water inlet, A return water inlet is disposed at a bottom of the upflow zone adjacent to the first water inlet, and the return water outlet and the return water inlet are connected by a water flow line.
  • the sewage treatment system further includes: at least one ozone-filled column, the water inlet end of the ozone-filled column is connected to the water inlet tank, and the water-discharging end of the ozone-filled column is respectively An ozone fluidized bed processing unit and the biofilm combined processing unit are connected.
  • the organic matter in the sewage can be further subjected to ozone oxidation treatment to further improve the quality of the effluent water.
  • the invention provides a method of sewage treatment using the sewage treatment system previously described.
  • the method comprises: performing at least one of ozone fluidized bed catalytic oxidation treatment and biofilm combined degradation treatment on the sewage by using the ozone fluidized bed processing unit and the biofilm combination unit
  • the ozone fluidized bed catalytic oxidation treatment comprises: supplying sewage from a first water inlet to an ozone fluidized bed processing unit, so that the sewage is filtered through the ceramic membrane module in the first casing And forming a circulation flow through the first water flow passage between the side wall, the top surface and the bottom surface of the first casing through the ceramic membrane module, and flowing out of the ozone fluidized bed processing unit from the first water outlet; the biofilm
  • the combined degradation treatment comprises: supplying the sewage from the second first water inlet to the biofilm combination treatment unit, and aerating the biological reaction space by using the second aeration port, so as to be in the biological carrier filler
  • At least one of ozone catalytic oxidation treatment and biofilm combined degradation treatment can be easily performed on the sewage, the mass transfer is enhanced, the mass transfer rate in the ozone fluidized bed treatment unit is improved, and the effluent water quality is further improved.
  • Stable can reduce membrane fouling, reduce water pressure and operating cost, and the sewage treatment method can flexibly select the sewage treatment unit according to the quality of the incoming water, which is convenient to operate and has strong applicability.
  • the ozone fluidized bed catalytic oxidation treatment further comprises: adding a first catalyst to the first casing, exposing ozone and air from the first aeration port, and causing the sewage and the first catalyst Rising from the bottom of the ceramic membrane module and flowing from the first water flow passage between the ceramic membrane assembly and the top surface of the first casing to the ceramic membrane assembly and the first casing
  • the first water flow passage between the side walls is lowered and raised under aeration conditions to form the circulation.
  • the biofilm combination degradation treatment further comprises: opening a second water circulation hole at the top of the separator so that the sewage in the membrane filtration space is returned to the biological reaction space.
  • the sewage can be further returned from the first water circulation hole at the bottom of the partition to the membrane filtration space to circulate and flow in the sewage.
  • the sewage can wash the surface of the cleaning membrane module to reduce membrane fouling, and the internal circulation flow can fall off the surface of the biological carrier filler and pass through the first water circulation hole to enter the free microorganisms in the membrane filtration space, and return to the place.
  • the bioreactor space is re-fixed, thereby reducing free microorganisms in the membrane filtration space, further reducing membrane fouling, and reducing water pressure and operating costs.
  • the biofilm combined degradation treatment further comprises: supplying the sewage in the water inlet tank to one of the plurality of auxiliary first water inlets into the downflow zone, and closing the circulation along the sewage a direction, a second water flow passage between the top of the first partition and the second casing before the auxiliary first water inlet connected to the water inlet tank.
  • the biofilm combination degradation treatment further comprises: opening a reflux water outlet, and supplying sewage passing through a downflow zone close to the membrane filtration space to the first water through the reflux water inlet The upflow zone of the water inlet.
  • the sewage can be easily circulated in the biological reaction space according to the treated sewage water quality, thereby further improving the effluent water quality.
  • the biofilm combined degradation treatment further includes: a plurality of the upflow regions and a bottom of each of the plurality of downflow regions, each of which is provided with the second aeration port,
  • the method further includes: controlling a plurality of switches of the second aeration port to control a processing environment of each of the plurality of the upflow zones and each of the plurality of downflow zones according to the incoming water quality of the sewage . Therefore, the sewage treatment environment can be flexibly selected according to the quality of the water to be aerobic, anaerobic and/or hypoxic, and the effluent water quality can be further improved.
  • the sewage treatment method further includes: supplying the sewage in the inlet tank to the ozone packed column according to the incoming water quality of the sewage; or supplying the sewage in the inlet tank to the Ozone catalytic oxidation unit.
  • the effluent water quality can be further improved.
  • FIG. 1 shows a schematic structural view of a sewage treatment system according to an embodiment of the present application
  • FIG. 2 shows a partial plan view of a ceramic membrane module in accordance with an embodiment of the present application
  • FIG. 3 shows a partial plan view of a ceramic membrane module in accordance with another embodiment of the present application.
  • FIG. 4 is a schematic structural view of a biofilm combination processing unit according to an embodiment of the present application.
  • FIG. 5 is a schematic structural view of a sewage treatment system according to another embodiment of the present application.
  • FIG. 6 is a schematic structural view of a sewage treatment system according to still another embodiment of the present application.
  • FIG. 7 shows a flow chart of a method of a sewage treatment method according to an embodiment of the present application.
  • Figure 8 shows a flow chart of a method of a sewage treatment method in accordance with another embodiment of the present application.
  • 1000 sewage treatment system; 100: inlet tank; 200: ozone fluidized bed treatment unit; 210: first casing; 220: ceramic membrane module; 221: ceramic membrane; 222: baffle; 223: membrane module shell Body; 230: first water flow channel; 240: first aeration port; 300: biofilm combined treatment unit; 310: second casing; 320: partition; 321: first water circulation hole; 322: second water Flow hole; 330: biological reaction space; 331: first partition; 332: upflow zone; 333: downflow zone; 334: second water flow channel; 335: auxiliary first water inlet; 336: reflux water outlet; : reflux inlet: 340: membrane filtration space; 341: membrane module; 350: biocarrier filler; 361: second aeration; 362: membrane filtration aeration; 363: aeration pipeline; Spout; 20: first water outlet; 30: second water inlet; 40: second water outlet; 400: clean water tank; 500: ozone
  • the current effluent quality of the sewage treatment system is not good, and there are still refractory organic pollutants remaining in the effluent, and the sewage treatment cost is relatively high.
  • the inventors have found through in-depth research that this is caused by defects in the current ozone catalytic oxidation reactor, microbial reactor, sewage treatment system and treatment process.
  • a sewage treatment system 1000 includes a water inlet tank 100, an ozone fluidized bed processing unit 200, and a biofilm combination processing unit 300.
  • the sewage treatment system 1000 can flexibly select a sewage treatment unit according to the quality of the incoming water, and is convenient to operate and has strong applicability.
  • the ozone fluidized bed processing unit 200 is connected to the water inlet tank 100, and the ozone fluidized bed processing unit 200 includes a first housing 210 and a ceramic membrane module 220 disposed vertically in the first housing 210, wherein the ceramic membrane module The 220 includes one or more ceramic membranes 221.
  • the ceramic membrane assembly 220 and the sidewalls, the top surface and the bottom surface of the first housing 210 are each provided with a first water flow channel 230 communicating with each other (as shown in FIG. 1).
  • the first housing 210 is provided with a first water inlet 10, first A first water outlet 20 is disposed on a side of the upper portion of the housing 210 opposite to the first water inlet 10, and the sewage is passed between the ceramic membrane module 220 and the side wall of the first housing 210 through the first water inlet 10.
  • the first water flow channel 230A is supplied into the ceramic membrane module 220. Thereby, the sewage can flow around the ceramic membrane module 220 and the first water flow channel 230, thereby enhancing the mass transfer, improving the mass transfer rate in the ozone fluidized bed processing unit 200, and making the effluent more stable and stable, and Reduced sewage treatment costs.
  • the biofilm combination processing unit 300 includes a second housing 310, a partition 320 disposed in the second housing 310, and a bioreactor space defined by the partition 320 in the second housing 310. 330 and membrane filtration space 340.
  • a second water inlet 30 is disposed on a side of the second casing 310 adjacent to the biological reaction space 330. The second water inlet 30 is respectively connected to the water inlet tank 100 and the first water outlet 20, and the second casing 310 is adjacent to the membrane.
  • a second water outlet 40 is disposed at a top of one side of the space 340, a bio-carrier filler 350 is disposed in the bio-reaction space 330, a second aeration port 361 is disposed at a bottom of the bio-reaction space 330, and a bottom portion of the partition plate 320 is disposed first.
  • the water circulation hole 321 is provided with a membrane module 341 in the membrane filtration space 340, and a membrane filtration aeration port 362 is provided at the bottom of the membrane filtration space 340.
  • the biofilm combination treatment unit 300 is not only resistant to impact loads, but also has a simple and compact structure, a small footprint, a low sludge expansion rate, and reduces contamination of the membrane module 341 by free microorganisms, and has the following advantages:
  • the membrane module 341 can filter the detached microorganisms to make the effluent more stable and stable; on the other hand, the sewage flows from the first water circulation hole 321 at the bottom of the partition 320 into the membrane filtration space 340, and is aerated at the membrane filtration aeration port 362. Under the action of the generated gas water lift, during the discharge from the water outlet 20 at the top of the second casing 310, the surface of the membrane module 341 can be cleaned, further reducing membrane fouling, reducing operating pressure and production cost.
  • the inventors have found that the current ozone catalytic oxidation reactor generally has problems such as low catalytic oxidation efficiency and high cost.
  • the inventors have found through in-depth research that this is mainly caused by insufficient contact between ozone, sewage and catalyst (ie gas-liquid-solid three-phase).
  • the contact mode of ozone, sewage and catalyst is relatively simple, and the reaction is generally only contacted by the same direction or anisotropic flow, and the contact between ozone, sewage and catalyst is insufficient, thereby limiting
  • the mass transfer process of organic matter in ozone and sewage causes the overall catalytic oxidation efficiency to be low, and it is difficult to further reduce the COD value of the sewage, and the problem of low ozone utilization rate and high sewage treatment cost.
  • the ceramic membrane module 220 is disposed at the center of the first housing 210, that is, at the side wall, the top surface, and the bottom surface of the ceramic membrane assembly 220 and the first housing 210.
  • the first water flow channel 230 connected to each other is reserved, whereby the sewage can rise from the bottom of the ceramic membrane module 220 to the ceramic membrane under the action of the gas and water lift generated by the aeration of the first aeration port 240.
  • the top of the assembly 220 and the first water flow passage 230B between the ceramic membrane assembly 220 and the top surface of the first housing 210 circulate downward, passing between the ceramic membrane assembly 220 and the sidewall of the first housing 210
  • a water flow channel 230A and a first water flow channel 230C between the ceramic membrane module 220 and the bottom surface of the first housing 210 are reflowed from the bottom into the ceramic membrane assembly 220.
  • the sewage flows circulating between the ceramic membrane module 220 and the first water flow channel 230, and the sewage can flow in all directions around the ceramic membrane module 220, thereby greatly enhancing the mass transfer and improving the ozone fluidized bed.
  • the mass transfer rate in the processing unit 200 makes the effluent more stable and stable, and reduces the sewage treatment cost.
  • the inventors have found that there are some drawbacks in the current methods of treating sewage by microorganisms.
  • the biofilm method has the advantages of impact load resistance, small footprint, low sludge expansion rate, and the like, there are few free microorganisms in the reactor.
  • the microbial population easily falls off from the surface of the biocarrier filler, so that The clarity of the effluent is reduced and the effluent water quality is unstable.
  • membrane bioreactor as a new water treatment technology combined with membrane separation unit and biological treatment unit, has the advantages of high quality and stable effluent, less residual sludge, and small footprint.
  • a membrane filtration space 340 is disposed on one side of the bioreaction space 330, and the membrane A membrane module 341 is disposed in the filter space 340.
  • the membrane module 341 can effectively filter the microbial population falling off the surface of the bio-carrier filler 350, thereby making the effluent more excellent and stable, and improving the disadvantages of the conventional biofilm reactor; Replacing the biological treatment unit in the conventional MBR with the bioreactor space 330 with the biocarrier filler 350 reduces the contamination of the MBR membrane module by free microorganisms in the conventional MBR, and improves the disadvantages of the conventional MBR.
  • the flow path of the sewage is ingeniously designed, that is, the sewage flows from the first water circulation hole 321 at the bottom of the partition plate 320 into the membrane filtration space 340, and the membrane aeration port 362 is filtered through the membrane.
  • the sewage can wash the surface of the cleaning membrane module 341, reducing membrane fouling and reducing operating pressure and cost.
  • the inventors have found that current sewage treatment systems and treatment processes also have some drawbacks.
  • a plurality of sewage treatment units are generally used in combination.
  • the sewage treatment system may include an ozone catalytic oxidation treatment unit and a microorganism treatment unit.
  • the connection between the plurality of processing units is unidirectional and fixed, that is, the flow direction of the sewage in each processing unit and the flow path are fixed.
  • the sewage treatment system cannot flexibly select a suitable sewage treatment unit and a sewage flow path according to the quality of the incoming water and the sewage treatment situation, thereby causing limited application of the sewage treatment system and causing poor sewage treatment and Waste the cost of sewage treatment.
  • the ozone fluidized bed processing unit 200 and the biofilm combined treatment unit 300 have better sewage treatment effects, thereby ensuring the stability of the effluent water quality in each unit.
  • the water inlet tank 100 is respectively connected to the ozone fluidized bed processing unit 200 and the biofilm combined processing unit 300, that is, according to the water quality of the sewage water, it is determined which unit to supply the sewage to for treatment, thereby avoiding the sewage fixed place. Through each unit in the system, the processing time is extended and the operating cost of the equipment is increased.
  • the sewage treatment unit by ingeniously designing the connection manner between each sewage treatment unit, such as the water inlet tank 100, the ozone fluidized bed processing unit 200, and the biofilm combination treatment unit 300, the sewage can be made
  • the treatment from the inlet tank 100 through the ozone fluidized bed processing unit 200 and the biofilm combination processing unit 300 may be performed only by the ozone fluidized bed processing unit 200 or only by the biofilm combination processing unit 300.
  • the sewage treatment unit can be flexibly selected according to the quality of the incoming water, and the operation is convenient, the applicability is strong, the effluent quality is high, and the sewage treatment cost is saved.
  • the sizes of the first housing 210 and the second housing 310 are not particularly limited, and those skilled in the art can flexibly select according to the size of the sewage treatment site, the quality of the treated sewage, and the amount of treatment. spiritual choice.
  • the integrated pipeline design reduces the connection pipeline between the sewage treatment units, thereby reducing the head loss caused by each connection pipeline, and the process of the sewage treatment device The connection is more compact and smooth, so it is easier to enlarge the sewage treatment device and make a large sewage treatment device.
  • the size of the ceramic membrane module 220 in the ozone fluidized bed processing unit 200 is not particularly limited as long as the ceramic membrane module 220 can be located at the center of the first housing 210, that is, the ceramic membrane assembly 220 and the first A first water flow channel 230 that communicates with each other is reserved between the side wall, the top surface, and the bottom surface of a casing 210.
  • the size of the ceramic membrane module 220 may be set according to the size of the first housing 210.
  • the ceramic membrane module 220 may include one or more ceramic membranes 221, and the specific material of the ceramic membrane 221 is not particularly limited, and may be a conventional ceramic membrane as long as it can filter sewage and have a small intercepting particle diameter.
  • the catalyst can be used.
  • the ceramic membrane module 220 when there is only one ceramic film 221 in the ceramic membrane module 220, the sewage can flow on both sides between the ceramic membrane module 220 and the first water flow passage 230.
  • the sewage can flow around the ceramic membrane assembly 220 and the first water flow passage 230 on all four sides.
  • the ceramic membrane 221 may further include a catalytic metal such as manganese dioxide particles, so that the ceramic membrane 221 can catalyze the ozone oxidation reaction in the pores while filtering out the water. Therefore, on the one hand, it is beneficial to further oxidize and degrade the organic matter in the sewage, and improve the water quality; on the other hand, through the ozone oxidation reaction in the pore of the ceramic membrane, the membrane pollution can be effectively reduced, and the water pressure and energy consumption can be reduced.
  • the number and arrangement of the ceramic membranes 221 are not particularly limited as long as the flow passage in which the sewage flows upward in the ceramic membrane module 220 can be defined.
  • the ceramic membrane module 220 may further include a baffle 222 disposed between the ceramic membranes 221, whereby the baffle 222 may define a flow of more sewage upwardly between the ceramic membranes 221
  • the channel further enhances the mass transfer and improves the mass transfer rate in the ozone fluidized bed processing unit 200, so that the effluent is more stable and stable.
  • the number and arrangement of the baffles 222 are not particularly limited as long as a plurality of flow paths in which the sewage flows upward can be divided.
  • the baffle 222 may be disposed parallel to the ceramic membrane 221. Referring to FIG.
  • the baffle 222 may also be disposed perpendicular to the ceramic membrane 221.
  • the ceramic membrane module 220 may further include a membrane module housing 223 disposed around the plurality of ceramic membranes 221, that is, the membrane module housing 223 may have four side walls and four side walls.
  • a first water flow channel 230 is reserved between the sidewalls of the first housing 210.
  • the ozone fluidized bed processing unit 200 may further include an ozone generating device (not shown) connected to the first aeration port 240. .
  • the ozone generating device can supply ozone to the first casing 210, promote the oxidative decomposition of the organic matter in the sewage, and make the effluent more excellent.
  • the ozone fluidized bed treatment unit 200 may further include a first catalyst inlet (not shown) disposed on the first casing 210.
  • a first catalyst can be provided into the first housing through the first catalyst inlet, and the ozone, sewage, and first catalyst can be circulated between the ceramic membrane assembly 220 and the first water flow passage 230.
  • ozone, sewage and the first catalyst can be fully contacted and reacted, and the organic matter in the sewage can be more fully degraded, thereby improving the ozone catalytic oxidation treatment efficiency of the organic matter, improving the utilization rate of ozone, and reducing the sewage treatment. cost.
  • the specific type of the first catalyst is not particularly limited as long as it can catalyze the generation of hydroxyl radicals by ozone and oxidize the organic matter in the sewage.
  • the first catalyst may be a particulate catalyst or a powder catalyst.
  • the manner of adding the first catalyst is not particularly limited, and the first catalyst may be directly added from the first catalyst inlet, under the action of the gas and water lift generated by the aeration of the first aeration port 240, A catalyst may be in a fluidized state within the first housing 210, sufficiently in contact with ozone and sewage.
  • the first catalyst may also be coated on the surface of the ceramic membrane 221, and the ozone and the sewage may also sufficiently contact the first catalyst on the ceramic membrane 221 when circulating in the ceramic membrane module 220. reaction.
  • the ozonation fluidized bed treatment unit 200 may further include a hydrogen peroxide inlet (not shown) disposed on the first casing 210.
  • hydrogen peroxide can be supplied into the first casing 210 through the hydrogen peroxide inlet, and the ozone, the hydrogen peroxide, the sewage, and the first catalyst described above can be circulated between the ceramic membrane module 220 and the first water flow passage 230. In this process, ozone, hydrogen peroxide, sewage, and the first catalyst can be sufficiently contacted and reacted.
  • the synergistic action of ozone and hydrogen peroxide is beneficial to generate hydroxyl radicals with strong oxidation, which can fully oxidize and degrade the organic matter in the sewage, further improving the oxidation of organic matter in the sewage.
  • Decomposition efficiency improves the quality of the effluent.
  • the ozone fluidized bed processing unit 200 may further include an ultraviolet illumination device (not shown) disposed in the first casing 210, and ultraviolet light.
  • the device is adapted to illuminate the ceramic membrane assembly 220 with ultraviolet light.
  • the ozone in the first casing 210 can generate hydroxyl radicals under the action of ultraviolet light, further improving the ozone oxidation decomposition efficiency of the organic matter in the sewage, and improving the water quality.
  • the ultraviolet light irradiation device can also simultaneously interact with at least one of the first catalyst and the hydrogen peroxide, thereby further increasing the rate of generation of hydroxyl radicals by the ozone, and improving the ozone oxidation decomposition efficiency of the organic matter in the sewage. Further improve the quality of the effluent.
  • the ozone fluidized bed processing unit 200 may further include an exhaust gas recovery port (not shown) disposed at the top of the first casing 210, thereby The ozone which does not react in the first casing 210 and the air generated by the aeration can be discharged from the exhaust gas recovery port, thereby improving the safety of the ozone fluidized bed processing unit 200.
  • the manner in which the partition plate 320 is disposed in the biofilm combination processing unit 300 is not particularly limited as long as the vertically disposed bioreaction space 330 and the membrane filtration space 340 can be separated in the second casing 310.
  • a first water circulation hole 321 is reserved at the bottom of the partition plate 320.
  • a gap may be left between the bottom of the partition plate 320 and the bottom of the second casing 310 to form the first water circulation hole 321 .
  • the partition plate 320 may be disposed to be movable in the vertical direction in the second housing 310, whereby the first movement can be easily realized by the movement of the partition plate 320 in the vertical direction in the second housing 310.
  • the water circulation hole 321 is opened and closed.
  • a water flow shutoff valve may be disposed on the partition plate 320, and the opening and closing of the first water circulation hole 321 may be easily realized by the water flow closing the switch of the valve.
  • a second water circulation hole 322 may also be disposed at the top of the partition plate 320.
  • the manner in which the second water circulation hole 322 is disposed is not particularly limited, and for example, it may be provided in the same manner as the first water circulation hole 321 .
  • the sewage treated through the membrane filtration space 340 can be passed over the partition 320 and flowed from the second water circulation hole 322 at the top of the partition 320 to the biological reaction space 330, and then through the first water circulation hole at the bottom of the partition 320.
  • the 321 is refluxed into the membrane filtration space 340 to form an inner circulation flow.
  • the sewage flows upward from the bottom of the membrane filtration space 340, and the surface of the cleaning membrane module 341 can be washed away to reduce membrane fouling, and the internal circulation flow energy will fall off from the surface of the biocarrier filler 350 and pass through the first water circulation hole.
  • the free microorganisms entering the membrane filtration space 340 are returned to the biological reaction space 330 and re-fixed, thereby reducing the free microorganisms in the membrane filtration space 400, further reducing membrane fouling, reducing the water pressure and operating costs. . Further, since the microorganisms treat dissolved sewage in the biological reaction space 330, dissolved oxygen is consumed.
  • the membrane filtration space 340 separates the biodegradation process from the membrane filtration process, there is no significant dissolved oxygen consumption in the membrane filtration space 340. Therefore, the sewage flowing back into the biological reaction space 330 contains more dissolved oxygen (provided by the membrane filtration first aeration port 620), so that the treatment effect of the biological reaction space 330 can be further enhanced, and the biological reaction space can also be saved. The amount of aeration, which in turn reduces operating costs.
  • part of the sludge containing microorganisms may also enter the membrane filtration space 340. Since the membrane filtration aeration port 362 is provided at the bottom of the membrane filtration space 340, and the water flow direction is parallel to the membrane module 341, the membrane module 341 does not cause contamination due to sludge entering the membrane filtration space 340.
  • the specific kind of the membrane module 341 is not particularly limited as long as the membrane module 341 is vertically disposed in the membrane filtration space 340, and may be, for example, at least one of a microfiltration membrane and an ultrafiltration membrane.
  • the material of the membrane module 341 is not particularly limited, and may be, for example, an organic film or an inorganic film.
  • the specific shape of the filter membrane is also not particularly limited, and may be at least one of a flat membrane and a hollow fiber membrane.
  • the kind and the number of the biological carrier filler 350 are not particularly limited as long as it can contribute to the adhesion of microorganisms and contribute to sufficient contact and reaction of the sewage with the microorganisms, for example, it can be a suspended fiber. At least one of a filler, a filled particulate filler.
  • the bio-carrier filler 350 may further include a second catalyst, and the specific kind of the second catalyst is not particularly limited as long as the organic matter in the sewage can be catalytically oxidized. Therefore, when the sewage is supplied to the biological reaction space 330, not only biochemical treatment but also chemical oxidation treatment can be performed to further improve the quality of the effluent water.
  • the BOD/COD ratio of the sewage can be improved by the chemical oxidation treatment of the second catalyst, thereby facilitating the biochemical treatment of the sewage by the microorganism, further Improve the quality of the effluent.
  • the biofilm combination processing unit 300 may further include: a sorbent inlet (not shown), and the sorbent inlet may be disposed at a side of the second housing 310 near the bioreactor space 330.
  • a powder capable of adsorbing biological and organic substances such as activated carbon powder, can be added to the biological reaction space 330 through the adsorbent inlet, whereby the water quality can be further improved.
  • the first partition 331 may be vertically disposed in the biological reaction space 330, and between the top of the first partition 331 and the second housing 310 or the bottom of the first partition 331
  • a second water flow channel 334 (refer to 334A and 334A' in FIG. 4) is reserved between the second casing 310 and the second casing 310, and the second casing 310, the first partition plate 331, and the partition plate 320 are defined in order.
  • the upflow zone 332 and the downflow zone 333 are arranged (refer to the direction of water flow shown by the arrows in Fig. 4).
  • the biofilm assembly processing unit 300 may include a plurality of first spacers 331 arranged in parallel, that is, the number of the first spacers 331 is not particularly limited, and those skilled in the art may The water quality and the amount of the sewage are properly designed, and the plurality of first partitions 331 can define a plurality of sequentially arranged upflow zones 332 and a downflow zone 333 in the biological reaction space 330, thereby further increasing sewage and The contact area of the biocarrier filler increases the efficiency of sewage treatment.
  • the specific arrangement manner of the second water flow channel 334 is not particularly limited, for example, may be in a direction in which the water flow flows in the biological reaction space 330 (as indicated by an arrow in FIG. 4), in the first A gap may be left between the top of one partition 331 and the second casing 310 or between the bottom of the first partition 331 and the second casing 310. Further, the first partition plate 331 can be moved in the vertical direction in the biological reaction space 330, whereby the movement of the first partition plate 331 in the vertical direction in the biological reaction space 330 can easily realize the second water flow channel 334. Open and close.
  • the second water flow passage 334 may also open and close the second water flow passage 334 by a water flow shutoff valve disposed on the first partition 331.
  • a water flow shutoff valve disposed on the first partition 331.
  • the bottom of the bioreaction space 330 is provided with a plurality of second aeration ports 361, and the second aeration ports 361 are located at the bottom of at least one of the upflow zone 332 and the downflow zone 333.
  • the second aeration port 361 may be located in each of the upflow zone 332 and the downflow zone 333.
  • the processing environment in each of the upflow zone 332 and each of the downflow zones 333 can be adjusted by the switch of the second aeration port 361 or the amount of gas supplied.
  • the gas-water lift generated by the aeration also contributes to the upward flow of the sewage in the upflow zone 332.
  • the second aeration port 361 in the upflow zone 332 can be opened, and the second aeration port 361 in the downflow zone 333 can be closed, thereby forming an aerobic environment in the upflow zone 332. It helps the microorganism to degrade the organic matter in the sewage and carry out the nitrification reaction.
  • the aeration zone 333 does not perform aeration, so the dissolved oxygen content in the downflow zone 333 is relatively low, and it is easy to form an anaerobic environment, which is beneficial to the microorganisms.
  • the organic matter in the sewage is treated, and denitrification and denitrification reaction occurs to further improve the quality of the effluent water.
  • the biological reaction space 330 includes a plurality of sequentially arranged upflow regions 332 and a downflow region 333
  • the sewage can be subjected to multi-stage aerobic treatment and anorexia/anoxic treatment in the biological space 300, thereby enabling The organic matter in the sewage is fully removed to further improve the sewage treatment efficiency and the effluent quality.
  • the volume of the upflow zone 332 and the downflow zone 333 may be the same or different.
  • the volume of the upflow zone 332 may be smaller than the downflow zone.
  • the volume of 333 may be the volume of 333.
  • the descending speed of the sewage in the downflow zone 333 is relatively slow, which is favorable for the discharge of dissolved oxygen in the sewage, thereby facilitating the formation of an anaerobic or anoxic environment in the downflow zone 333, and the microorganisms can treat the organic matter in the sewage. Perform adequate anaerobic or anoxic treatments, such as denitrification and denitrification, to further improve wastewater treatment efficiency and effluent quality.
  • Those skilled in the art can understand that the above specific embodiments are merely illustrative of the present application and are not to be construed as limiting the processing environment in the upflow zone 332 and the downflow zone 333.
  • each of the upflow zone 332 and the downflow zone 333 can adjust the environment of each of the upflow zone 332 and the downflow zone 333 according to the actual situation of the sewage water quality, and the processing environment of each of the upflow zone 332 and the downflow zone 333 can be separately controlled as Aerobic, hypoxic or anaerobic.
  • the arrangement of the second aeration port 361 located in the bioreactor space 330 and the membrane filtration aeration port 362 located at the bottom of the membrane filtration space 340 is not particularly limited, and for example, may be in the second casing 310.
  • the aeration line 363 is disposed at the bottom and perforated at an appropriate position of the aeration line 363 to form a second aeration port 361 and a membrane filtration aeration port 362.
  • the formed second aeration port 361 and the membrane filtration aeration port 362 can both be capable of being closed, or can have the function of adjusting the amount of aeration, thereby flexibly adjusting the dissolution of different regions in the biological reaction space. Oxygen content to form a variety of aerobic, anoxic, and anaerobic environments as needed.
  • the biofilm combination treatment unit 300 may further include: a return water outlet 336 and a return water inlet 337, and the return water outlet 336 is disposed near the membrane.
  • the return water inlet 337 is disposed near the bottom of the upflow zone 332 of the first water inlet 10, and the return water outlet 336 and the return water inlet 337 are connected by a water flow line.
  • the manner of setting the return water inlet 337 is not particularly limited.
  • the water inlet 10 disposed on the second casing 310 can be directly used as the return water inlet 337, thereby making it possible to more conveniently return the sewage back. It flows into the biological reaction space 330.
  • the sewage treatment system 1000 may further include: a clean water tank 400, a clean water tank 400 and a first water inlet 10, and a first water outlet. 20 and the second water outlet 40 are connected.
  • the sewage treatment system can have a more flexible processing flow.
  • the sewage in the water inlet tank 100 may be sequentially processed by the ozone fluidized bed processing unit 200 and the biofilm combination processing unit 300, and then stored in the clean water tank 400.
  • the sewage in the water inlet tank 100 may also be treated only by the ozone fluidized bed processing unit 200 and stored directly into the clean water tank 400.
  • the sewage in the water inlet tank 100 may be first flowed into the biofilm combination processing unit 300 for treatment, discharged to the clean water tank 400 after the treatment, and then supplied to the ozone fluidized bed processing unit 200 for ozone catalytic oxidation. deal with. Therefore, the sewage treatment system 1000 can flexibly select the sewage treatment unit according to the quality of the incoming water, and is convenient to operate and has strong applicability.
  • the sewage treatment system 1000 may further include a backwashing unit (not shown) for backwashing the ceramic membrane module 220 and the membrane module 341.
  • a backwashing unit (not shown) for backwashing the ceramic membrane module 220 and the membrane module 341.
  • the specific structure of the backwashing unit and the process of backwashing are not particularly limited, and those skilled in the art can select according to actual conditions.
  • the treated water produced by the sewage treatment system can be used for backwashing, or a backwash tank can be separately provided for backwashing, thereby further reducing membrane fouling and reducing the water pressure and operating cost.
  • the sewage treatment system 1000 may further include a sampling port (not shown) disposed at a middle portion of the first casing 210 and a middle portion of the second casing 310. . Thereby, the water quality in the first casing 210 and the second casing 310 can be easily monitored in real time.
  • the sewage treatment system 1000 may further include an air discharge port (not shown) disposed at the bottom of the first casing 210 and the second casing 310. .
  • an air discharge port (not shown) disposed at the bottom of the first casing 210 and the second casing 310.
  • the sewage treatment system 1000 may further include an overflow port (not shown) disposed at the top of the first casing 210 and the second casing 310. .
  • an overflow port (not shown) disposed at the top of the first casing 210 and the second casing 310.
  • the sewage treatment system 1000 may further include a liquid level control unit (not shown) for regulating access to the first casing 210 and the second casing.
  • the amount of sewage in the body 310 may include a liquid level sensor and a water inlet pump (not shown), and the liquid level sensor may monitor the water level in the first housing 210 and the second housing 310 and can control the start and stop of the water pump. Thereby, the amount of sewage in the first casing 210 and the second casing 310 can be easily adjusted.
  • the sewage treatment system 1000 may further include: at least one ozone-filled column 500 having a packed column inlet end 510 and a packed column outlet end 520, the packed column inlet end 510 Connected to the water inlet tank 100, the packed column water outlet end 520 is connected to the ozone fluidized bed processing unit 200 and the biofilm combination processing unit 300, respectively. That is, after the sewage is treated by the ozone packed column 500, it may be treated by at least one of the ozone fluidized bed processing unit 200 and the biofilm combined processing unit 300. Thereby, the organic matter in the sewage can be further subjected to ozone oxidation treatment to further improve the quality of the effluent water.
  • the specific arrangement position of the packed column inlet end 510 and the packed column water outlet end 520 is not particularly limited.
  • the packed column inlet end 510 may be disposed at the upper portion of the ozone packed column 500, and the packed column is discharged.
  • the end 520 may be disposed at a lower portion of the ozone-filled column 500, and the sewage may flow from the upper portion of the ozone-filled column 500 and flow out from the lower portion thereof, so that the sewage may flow in a countercurrent flow in the ozone-packed column 500, thereby facilitating the ozone and the sewage.
  • the organic matter is in full contact with the reaction.
  • the type and number of the ozone-filled column 500 are not particularly limited.
  • the inlet tank 100 may be connected to the packed column inlet end 510A, or It is connected to the packed column inlet end 510A', and the connection manner of the plurality of ozone-filled columns 500 is also not particularly limited, and may be connected in parallel or in series, and can be set as needed by those skilled in the art.
  • the sewage treatment system 1000 may further include: a coagulation sedimentation tank, a sewage treatment unit such as a security filter, a coagulation sedimentation tank, and a security filter. Conventionally used in the field, as long as the sewage can be purified.
  • each unit has a reasonable structural design, which can ensure the sewage treatment effect of the unit and provide stable effluent water quality.
  • the water inlet tank is respectively connected with the ozone packed column, the ozone fluidized bed processing unit and the biofilm combined processing unit, whereby the water quality of the water entering the water tank can be determined, and the sewage is first supplied to which unit for processing. That is, the sewage treatment system can determine the specific process of treating sewage in the system according to the water quality, and the operation is flexible and convenient. Therefore, the system can be used not only to treat sewage with extremely poor biodegradability (such as coal chemical wastewater, etc.), but also to treat general sewage without causing excessive system operating costs.
  • the present application proposes a method of sewage treatment using the sewage treatment system described above.
  • the sewage treatment method can have all of the features and advantages of the sewage treatment system previously described.
  • the method includes: performing at least one of an ozone fluidized bed catalytic oxidation treatment and a biofilm combined degradation treatment on the sewage by using the ozone fluidized bed processing unit and the biofilm combination unit , sewage treatment.
  • the ozone fluidized bed catalytic oxidation treatment includes:
  • sewage is supplied from the first water inlet to the ozone fluidized bed processing unit.
  • the sewage to be treated is supplied from the first water inlet to the first casing, and passes through the first water flow passage between the side wall of the first casing and the ceramic membrane module, Supply to the ceramic membrane module.
  • the sewage flows in a circulating flow between the ceramic membrane module and the first water flow passage.
  • the sewage can rise from the bottom of the ceramic membrane module to the top of the ceramic membrane module by the lift of gas and water generated by the aeration of the first aeration port, and between the ceramic membrane module and the top surface of the first casing.
  • the first water flow channel circulates downward, recirculates from the bottom to the ceramic through the first water flow channel between the ceramic membrane module and the sidewall of the casing and the first water flow channel between the ceramic membrane module and the bottom surface of the first casing In the membrane module.
  • the sewage can circulate between the ceramic membrane module and the first water flow passage, and the sewage can flow to all directions around the ceramic membrane module, thereby greatly enhancing the mass transfer and improving the ozone fluidized bed processing unit.
  • the mass transfer rate in the middle makes the effluent more stable and stable, and reduces the cost of sewage treatment.
  • the sewage treatment method further includes: adding a first catalyst to the first casing, exposing the ozone gas and the air from the first aeration port, causing the sewage and the catalyst to rise from the bottom of the ceramic membrane module, and a first water flow passage between the ceramic membrane module and the top surface of the first casing flows to the first water flow passage between the ceramic membrane assembly and the side wall of the first casing and descends, and rises under aeration conditions so that The circulation is formed.
  • the ozone, the sewage and the first catalyst can be fully contacted and reacted in the circulation process, thereby promoting the ozone catalytic oxidative decomposition of the organic matter in the sewage and improving the effluent water quality.
  • the sewage treatment method may further include: adding hydrogen peroxide to the casing from the hydrogen peroxide inlet, the ozone, the hydrogen peroxide, the sewage, and the first catalyst circulating in a circulation between the ceramic membrane module and the first water flow passage.
  • ozone, hydrogen peroxide, sewage, and the first catalyst can be sufficiently contacted and reacted.
  • the synergistic action of ozone and hydrogen peroxide is beneficial to generate hydroxyl radicals with strong oxidation, and thus can fully oxidize and degrade the organic matter in the sewage, thereby further improving the oxidative decomposition efficiency of organic substances in the sewage. Improve the quality of the effluent.
  • the sewage treatment method may further include irradiating the ceramic membrane module with ultraviolet light by an ultraviolet light device disposed in the first casing.
  • the ozone in the first casing can generate hydroxyl radicals under the action of ultraviolet light, further improving the ozone oxidation decomposition efficiency of the organic matter in the sewage, and improving the water quality.
  • the ultraviolet light device can also be used simultaneously with at least one of the first catalyst and the hydrogen peroxide, thereby further increasing the rate of generation of hydroxyl radicals by the ozone, and improving the ozone oxidation decomposition efficiency of the organic matter in the sewage. To further improve the quality of the effluent.
  • the sewage is filtered through the ceramic membrane module and discharged from the first water outlet.
  • the purified water filtered by the ceramic membrane module can be sucked into the clean water tank by the water discharge pump.
  • the sewage treatment method further comprises: backwashing the ceramic membrane module by using the treated water produced by the sewage treatment system, or separately providing a backwashing water tank, thereby further reducing membrane fouling.
  • the biofilm combination degradation treatment includes:
  • the sewage to be treated is supplied from the second water inlet to the biological reaction space, so that under the aeration condition, the microorganisms in the biological carrier filler react with the sewage to purify the sewage.
  • the plurality of first partitions when a plurality of first partitions are disposed in the biological reaction space, the plurality of first partitions may define a plurality of sequentially arranged upflow zones and a downflow zone in the biological reaction space, and the sewage may be The flow-through flow in the biological reaction space increases the contact area between the sewage and the bio-carrier filler, and improves the sewage treatment efficiency.
  • the upflow zone can be aerated, and an aerobic environment can be formed in the upflow zone, so that the microorganisms can degrade the organic matter in the sewage and carry out the nitration reaction.
  • the aeration zone is not aerated, so the dissolved oxygen content in the downflow zone is relatively low, which is easy to form an anaerobic environment, which is beneficial to the microorganisms to treat the organic matter in the sewage, and denitrification and denitrification reaction occurs to further enhance the effluent. Water quality.
  • the biological reaction space includes a plurality of sequentially arranged upflow zones and a downflow zone
  • the sewage can be sequentially subjected to multi-stage aerobic treatment and anaerobic treatment in the biological space, thereby enabling The organic matter in the sewage is more fully removed, and the sewage treatment efficiency and the effluent water quality are further improved.
  • the supply position and the supply mode of the sewage to the biological reaction space can be flexible, and the skilled person can according to the treated sewage water quality. And the amount of water to choose.
  • the sewage water quality when the sewage water quality is poor, it may be supplied to the biological reaction space from the second water inlet provided on the side wall of the second casing close to the biological reaction space, thereby utilizing the entire biological reaction space.
  • the sewage has good water quality, and may be selected from one of the plurality of auxiliary first water inlets disposed in the downflow zone, supplied to the upflow zone, and closed to the top and the second of the first partition defining the downflow zone
  • a second water flow path between the housings is treated with a portion of the bioreactor space.
  • S220 the sewage is treated by microorganisms in the biological reaction space, and is supplied from the water circulation hole at the bottom of the separator to the membrane filtration space.
  • the microorganism-treated sewage is supplied from the water circulation hole at the bottom of the separator to the membrane filtration space.
  • a membrane filtration aeration port may be disposed at the bottom of the membrane filtration space, whereby the microbial treated sewage is supplied to the membrane filtration space from the first water circulation hole at the bottom of the separator, and the membrane is filtered and aerated.
  • the mouth aeration generates gas and water lift, flows upwards, and can be discharged from the second water outlet at the top of the second casing, or can be over the baffle and from the top of the baffle to the second casing
  • the two water flow holes are returned to the downflow zone adjacent to the membrane filtration space, and the rising water flow during the process can flush the cleaning membrane module, further reducing membrane fouling.
  • the sewage flowing from the water flow gap into the downflow zone close to the membrane filtration space may further flow into the membrane filtration space from the water circulation hole at the bottom of the partition, thereby forming a circulating flow process in the sewage, and the internal circulation process may
  • the membrane module is repeatedly washed, whereby membrane fouling can be greatly reduced, and the internal circulation flow can be detached from the surface of the biocarrier filler, and the free microorganisms in the space can be filtered through the first water circulation membrane to be refluxed to The bioreactor space is re-fixed, thereby reducing free microorganisms in the membrane filtration space, further reducing membrane fouling, and reducing water pressure and operating costs.
  • the membrane assembly may be backwashed with treated water produced by the sewage treatment system, or a separate backwash tank may be separately provided to further reduce membrane fouling.
  • the sewage filtered through the membrane module is discharged from the second water outlet located at the top of the membrane filtration space.
  • the water flow when the water flow rises from the bottom of the membrane filtration space to the top of the membrane filtration space and is discharged, the water flow can clean the surface of the membrane module, thereby further reducing membrane fouling, reducing operating pressure and Cost of production.
  • the biofilm combined degradation treatment further comprises: opening the reflux outlet, and supplying the sewage passing through the downflow zone close to the membrane filtration space to the upflow zone near the water inlet through the reflux inlet. Therefore, according to the water quality of the treated sewage, the sewage can be recycled in the biological reaction space, the effluent water quality is further improved, and the operation is convenient. According to the embodiment of the present application, according to the water quality of the treated sewage, the sewage treated by the downflow zone near the membrane filtration space can be detected for the effluent water quality, and if the organic matter content is still high, it can be discharged through the reflux outlet, and Supply to the upflow zone near the inlet and continue biochemical treatment.
  • the plurality of upflow zones and the bottom of each of the plurality of downflow zones are provided with a second aeration port.
  • the switches of the plurality of second aeration ports are controlled, thereby controlling the processing environments of each of the plurality of upflow zones and the plurality of downflow zones. Therefore, the sewage treatment environment can be flexibly selected according to the quality of the water to be aerobic, anaerobic and/or hypoxic, and the effluent water quality can be further improved.
  • controlling the second aeration switch to adjust the sewage treatment environment may include but is not limited to the following steps:
  • the aeration port of the upflow zone can be opened, and the aeration port of the downflow zone can be closed to form an aerobic environment in the upflow zone, and an oxygen-deficient environment is formed in the downflow zone for multi-stage aerobic-deficient sewage. Oxygen treatment. Thereby, the effluent water quality can be further improved.
  • the upflow zone and the second aeration port of the downflow zone may be opened to form an aerobic environment in the upflow zone and the downflow zone for aerobic treatment of the sewage.
  • the effluent water quality can be further improved.
  • the upflow zone and the second aeration port of the downflow zone may be closed to form an anaerobic/anoxic environment in the upflow zone and the downflow zone for anaerobic/anoxic treatment of the sewage .
  • the effluent water quality can be further improved.
  • the aeration port at the bottom of one or more upflow zones near the water inlet can be closed, that is, an anaerobic environment is formed in the upflow zone and the downflow zone near the water inlet, and the upflow zone near the membrane filtration space is opened.
  • the gas port closes the aeration port of the downflow zone near the membrane filtration space, thereby forming an anaerobic-multi-stage (aerobic-anoxic) sewage treatment environment in the biological reaction space, which can further degrade the organic matter in the sewage. Improve the quality of the effluent.
  • each upflow zone and downflow zone can be adjusted at any time according to the change of water quality (real-time monitoring of the sewage in the system through the sampling port). That is to say, each upwelling zone and downflow zone can form an aerobic, anoxic or anaerobic environment according to the needs, and adopt the best combination method to efficiently degrade the organic matter in the sewage.
  • the sewage treatment method can easily carry out biochemical treatment on the sewage, the effluent water quality is more stable, and the membrane pollution can be reduced.
  • the sewage treatment method may further include: supplying the sewage in the water inlet tank to the ozone-filled column according to the water quality of the sewage water; or supplying the sewage in the water inlet tank to the water supply tank Said in the ozone catalytic oxidation unit.
  • the effluent water quality can be further improved.
  • the ozone packed column-ozone fluidized bed processing unit biofilm combined processing unit can be coupled to fully degrade the organic matter in the sewage.
  • the flow path of the sewage is not particularly limited, and those skilled in the art can flexibly select according to the water quality and the sewage treatment situation.
  • the sewage may be treated only by the ozone packed column, may be treated only by the ozone fluidized bed processing unit, or may be processed only by the biofilm combined processing unit, and may be processed through any two or three of the three processing units.
  • the order of the above treatment is not particularly limited.
  • the biofilm combination treatment unit may be first treated and subjected to an ozone fluidized bed treatment unit.
  • the sewage treatment method is flexible and convenient to operate, and has wide applicability, especially for coal chemical wastewater containing more refractory organic matter, and the treatment effect is good.
  • the sewage treatment system can easily perform at least one of ozone catalytic oxidation treatment and biofilm combined degradation treatment on the sewage, strengthen the mass transfer, and improve the mass transfer rate in the ozone fluidized bed processing unit, and
  • the effluent water quality is more high quality and stable, the membrane pollution can be reduced, the water outlet pressure and the running cost can be reduced, and the sewage treatment method can flexibly select the sewage treatment unit according to the water quality, and the operation is convenient and the applicability is strong.
  • pre-treatment methods such as multi-media filtration, precipitation, etc.
  • coagulation sedimentation and security filtration are taken as examples.
  • a plurality of advanced oxidation processes of ozone may be employed, and the series-parallel form of each process is not unique.
  • an ozone packed bed and an ozone fluidized bed are connected in series as an example.
  • an ozone packed column is used for treatment.
  • the backwashing step can be performed when the unit is stopped.
  • the dosage of ozone is 50-150mg/L and the atmospheric pressure is 0.1MPa.
  • the dosage of ozone can also be adjusted according to the actual situation.
  • On-line drug washing is performed if the effluent pressure is below -30 kPa or for more than one week of operation.
  • This embodiment is suitable for the case where the COD of the MBR effluent is still high, that is, the fluidized bed post process is employed:
  • the pre-processing mode of this embodiment may be multiple. Specifically, multi-media filtering is taken as an example.
  • the quartz sand filter is used for pretreatment, and the medium is selected from quartz sand, anthracite, granular porous ceramics, manganese sand, and the like.
  • This step is the same as in Example 1, and it can be treated with a single packed bed or with two packed beds in parallel.
  • This step is the same as in the first embodiment.
  • the fluidized bed treatment step was the same as in Example 1.
  • This embodiment is applicable to the case where the COD concentration of the wastewater is low, but the biodegradability is extremely poor.
  • Step 1 and Step 2 were the same as in Example 1, and the coagulation sedimentation and the security filtration treatment were sequentially performed.
  • This step is the same as in Example 1, and it can be treated with a single packed bed or with two packed beds in parallel.
  • This embodiment is applicable to wastewater with high influent concentration and good biochemicality, that is, a process of direct MBR biochemistry at the front end and enhanced oxidation by an ozone fluidized bed.
  • the process in this embodiment is only used as a depth processing unit, and does not include a pre-processing unit.
  • This step deals with the same parameters as in Example 1. Directly discharged after treatment with an ozone fluidized bed.

Abstract

一种污水处理系统（1000），包括：进水箱（100）；臭氧流化床处理单元（200），臭氧流化床处理单元（200）与进水箱（100）相连，且包括第一壳体（210）、垂直设置在第一壳体（210）中的陶瓷膜组件（220）、第一进水口（10）以及第一出水口（20）；以及生物膜组合处理单元（300），生物膜组合处理单元（300）与进水箱（100）以及臭氧流化床处理单元（200）相连，且包括第二壳体（310），隔板（320）在第二壳体（310）中限定出生物反应空间（330）以及膜过滤空间（340）。还提供了利用该污水处理系统（1000）进行污水处理的方法，可根据来水水质灵活选择污水处理单元，操作方便，适用性强。

Description

深度污水处理系统以及污水处理方法
优先权信息
本申请请求2017年12月29日向中国国家知识产权局提交的、专利申请号为201711477365.3，以及2017年12月29日向中国国家知识产权局提交的、专利申请号为201721922235.1的专利申请的优先权和权益，并且通过参照将其全文并入此处。
技术领域
本申请涉及污水处理领域，具体地，涉及深度污水处理系统以及污水处理方法。
背景技术
随着人口规模的不断扩大和社会经济的持续发展，城市生活污水以及工业污水的排放量也随之增长，污水处理负荷持续加重。微生物可以去除污水中溶解性和胶体状态的可生化有机物以及磷素、氮素等，具有高效率、低能耗、低成本、操作简单以及反应条件温和等优点。臭氧催化氧化法利用臭氧分解产生的羟基自由基(·OH)氧化分解污水中的难降解有机物，具有氧化能力强、选择性弱、不产生二次污染等优势，臭氧氧化法是一种有效的污水深度处理技术。
然而，目前的污水处理系统以及污水处理方法仍有待改进。
发明内容
本申请提出了一种污水处理系统。该污水处理系统包括：进水箱；臭氧流化床处理单元，所述臭氧流化床处理单元与所述进水箱相连，且包括：第一壳体；陶瓷膜组件，所述陶瓷膜组件垂直设置在所述第一壳体中，所述陶瓷膜组件包括一个或多个陶瓷膜，所述陶瓷膜组件与所述第一壳体的侧壁、顶面以及底面之间，均预留有互相连通的第一水流通道；第一进水口，所述第一进水口设置在所述第一壳体的上部，所述第一进水口可利用所述陶瓷膜组件与所述第一壳体的侧壁之间的所述第一水流通道，将污水供给至所述陶瓷膜组件中；第一出水口，所述第一出水口设置在所述第一壳体的上部，且与所述第一进水口相对设置；以及第一曝气口，所述第一曝气口设置在所述第一壳体的底部；以及生物膜组合处理单元，所述生物膜组合处理单元包括：第二壳体，所述第二壳体中设置有隔板，所述隔板在所述第二壳体中限定出生物反应空间以及膜过滤空间，所述隔板的底部具有第一水流通孔，所述第二壳体靠近所述生物反应空间的一侧设置有第二进水口，所述第二进水口分别与所述进水箱以及所述第一出水口相连，所述第二壳体靠近所述膜过滤空间一侧的顶部 设置有第二出水口；生物载体填料，所述生物载体填料设置在所述生物反应空间中，且所述生物反应空间的底部，设置有第二曝气口；膜组件，所述膜组件垂直设置在所述膜过滤空间中，且所述膜过滤空间的底部，设置有膜过滤曝气口。由此，该污水处理系统不仅构造简单紧凑，占地面积小，污泥膨胀率低，传质效率高，出水更加优质稳定，还能减小膜污染，降低能耗和污水处理成本，并且该污水处理系统可根据来水水质灵活选择污水处理单元，操作方便，适用性强。
根据本发明的实施例，所述陶瓷膜组件进一步包括膜组件壳体，所述膜组件壳体具有4个侧壁，所述4个侧壁与所述第一壳体的侧壁之间，均预留有第一水流通道。由此，所述膜组件壳体可以进一步支撑和固定所述陶瓷膜，并且污水可在所述膜组件壳体与所述第一水流通道之间四面环流流动，进一步加强了传质，提高了该臭氧流化床处理单元内的传质速率。
根据本发明的实施例，所述陶瓷膜组件进一步包括：设置在多个所述陶瓷膜之间的隔流板。由此，所述隔流板可在陶瓷膜之间限定出多个流道，进一步加强了传质，提高了该臭氧流化床处理单元内的传质速率，使出水更加优质稳定。
根据本发明的实施例，所述臭氧流化床处理单元进一步包括：第一催化剂入口，所述第一催化剂入口设置在所述第一壳体上。由此，可通过所述第一催化剂入口向所述第一壳体内提供第一催化剂，促进污水中有机物的臭氧催化氧化分解，使出水更加优质。
根据本发明的实施例，所述臭氧流化床处理单元进一步包括：双氧水入口，所述双氧水入口设置在所述第一壳体上。由此，可通过所述双氧水入口向所述第一壳体内提供双氧水，对污水中的有机物进行臭氧和双氧水的联合氧化，进一步提高了污水中有机物的氧化分解效率，提升了出水水质。
根据本发明的实施例，所述臭氧流化床处理单元进一步包括：紫外光照装置，所述紫外光照装置适于向所述陶瓷膜组件照射紫外光。由此，所述紫外光可以促进臭氧产生羟基自由基，进一步提高污水中有机物的臭氧氧化分解效率，提升了出水水质。
根据本发明的实施例，所述生物膜组合处理单元中，所述隔板的顶部设置有第二水流通孔。由此，经过所述膜过滤空间处理的污水可以翻越所述隔板，并从所述第二水流通孔流至所述生物反应空间中，再通过所述隔板底部的所述第一水流通孔回流至所述膜过滤空间中，形成内循环流动。该过程中，污水从膜过滤空间底部向上流动，可以冲刷清洗膜组件表面，减小膜污染，并且，该内循环流动能将从生物载体填料表面脱落，并通过第一水流通孔进入膜过滤空间中的游离微生物，回流至所述生物反应空间中并重新固定，由此，减少了膜过滤空间中的游离微生物，进一步减小了膜污染，降低了出水压力和运行成本。
根据本发明的实施例，所述生物膜组合处理单元中，所述生物反应空间中具有第一隔 板，所述第一隔板垂直设置在所述生物反应空间中，所述第一隔板的顶部与所述第二壳体之间、或者所述第一隔板的底部与所述第二壳体之间均预留有第二水流通道，所述第二壳体、所述第一隔板以及所述隔板之间，限定出依次排列的升流区以及降流区。由此，污水可在所述生物反应空间内折流式流动，增大了污水与生物载体填料的接触面积，从而提高了污水处理效率。
根据本发明的实施例，所述生物膜组件处理单元进一步包括多个平行排列的所述第一隔板。由此，所述生物反应空间内包括多个依次排列的升流区以及降流区，污水可在所述多个依次排列的升流区以及降流区内折流式流动，进一步增大了污水与生物载体填料的接触面积，进一步提高了污水处理效率。
根据本发明的实施例，所述升流区的体积小于所述降流区的体积。由此，污水在所述降流区的流动速度比较慢，有利于在降流区形成厌氧或缺氧环境，以便微生物对污水进行厌氧或缺氧处理，进一步提高了污水处理效率。
根据本发明的实施例，所述生物膜组合处理单元进一步包括：多个第二曝气口，所述第二曝气口位于所述升流区以及所述降流区至少之一的底部。由此，通过控制所述多个第二曝气口的打开和关闭，可以简便地调节所述升流区以及降流区中的溶解氧含量，有利于根据需要在所述升流区以及降流区中形成好氧、缺氧以及厌氧环境，以便微生物对污水进行好氧、缺氧或者厌氧处理，进一步提高了出水水质，并且曝气产生的气水升力还有助于升流区中的污水向上流动。
根据本发明的实施例，所述生物膜组合处理单元进一步包括：多个辅助第一进水口，所述辅助第一进水口设置在所述生物反应空间的顶部且位于所述降流区中。由此，有利于灵活调节进水位置以及水力停留时间，从而可以根据所处理的污水水质选择合适的生物反应空间的体积，有助于降低处理成本。
根据本发明的实施例，所述第一隔板与所述第二壳体之间的第二水流通道被设置为可关闭。由此，可以简便地根据需要控制污水在所述生物反应空间内的流动路径。
根据本发明的实施例，所述生物膜组合处理单元进一步包括：回流出水口，所述回流出水口设置在靠近所述膜过滤空间的所述降流区的底部；以及回流进水口，所述回流进水口设置在靠近所述第一进水口的所述升流区的底部，且所述回流出水口以及所述回流进水口之间通过水流管路相连。由此，可以根据所处理的污水水质，简便地使所述污水在所述生物反应空间内循环处理，进一步提高了出水水质。
根据本发明的实施例，所述污水处理系统进一步包括：至少一个臭氧填充柱，所述臭氧填充柱的进水端与所述进水箱相连，所述臭氧填充柱的出水端分别与所述臭氧流化床处理单元以及所述生物膜组合处理单元相连。由此，可以进一步对污水中的有机物进行臭氧 氧化处理，进一步提升出水水质。
在本发明的另一方面，本发明提出了一种利用前面所述的污水处理系统进行污水处理的方法。根据本发明的实施例，该方法包括：利用所述臭氧流化床处理单元以及所述生物膜组合单元，对所述污水进行臭氧流化床催化氧化处理以及生物膜组合降解处理的至少之一，其中，所述臭氧流化床催化氧化处理包括：将污水从第一进水口供给至臭氧流化床处理单元中，以便所述污水在所述第一壳体中经陶瓷膜组件进行过滤处理，并通过陶瓷膜组件与所述第一壳体的侧壁、顶面以及底面之间的第一水流通道形成环流，由第一出水口流出所述臭氧流化床处理单元；所述生物膜组合降解处理包括：将所述污水由所述第二第一进水口供给至生物膜组合处理单元中，并利用第二曝气口对所述生物反应空间进行曝气，以便生物载体填料中的微生物，在生物反应空间与所述污水发生反应，并从隔板底部的第一水流通孔供给至膜过滤空间，在膜过滤曝气口曝气的条件下，从位于所述膜过滤空间顶部的第二出水口排出。由此，可以简便地对污水进行臭氧催化氧化处理以及生物膜组合降解处理的至少之一，加强了传质，提高了该臭氧流化床处理单元内的传质速率，并且使出水水质更加优质稳定，可减小膜污染，降低出水压力和运行成本，并且该污水处理方法可根据来水水质灵活选择污水处理单元，操作方便，适用性强。
根据本发明的实施例，所述臭氧流化床催化氧化处理进一步包括：向所述第一壳体内加入第一催化剂，从第一曝气口曝臭氧以及空气，使污水以及所述第一催化剂从所述陶瓷膜组件的底部上升，并从所述陶瓷膜组件和所述第一壳体的顶面之间的第一水流通道，流至所述陶瓷膜组件和所述第一壳体的侧壁之间的第一水流通道并下降，在曝气条件下上升，以便形成所述环流。由此，促进了污水中有机物的臭氧催化氧化分解，提高了反应速率，提升了出水水质。
根据本发明的实施例，所述生物膜组合降解处理进一步包括：打开所述隔板顶部的第二水流通孔，以便所述膜过滤空间中的污水，回流至生物反应空间。污水可进一步从隔板底部的第一水流通孔回流至膜过滤空间，使污水内循环流动。由此，污水可以冲刷清洗膜组件表面，减小膜污染，并且，该内循环流动能将从生物载体填料表面脱落、并通过第一水流通孔进入膜过滤空间中的游离微生物，回流至所述生物反应空间中并重新固定，由此，减少了膜过滤空间中的游离微生物，进一步减小了膜污染，降低了出水压力和运行成本。
根据本发明的实施例，所述生物膜组合降解处理进一步包括：将进水箱中的污水由多个辅助第一进水口中的一个，供给至降流区中，并关闭沿着污水流通的方向，设置在与所述进水箱相连的所述辅助第一进水口之前的第一隔板的顶部与所述第二壳体之间的第二水流通道。由此，可以简便地调节进水位置以及水力停留时间，可以根据所处理的污水水质选择合适的生物反应空间的体积，有助于降低处理成本。
根据本发明的实施例，所述生物膜组合降解处理进一步包括：打开回流出水口，将经过靠近所述膜过滤空间的降流区的污水，通过所述回流进水口供给至靠近所述第一进水口的所述升流区。由此，可以根据所处理的污水水质，简便地使所述污水在所述生物反应空间内循环处理，进一步提高了出水水质。
根据本发明的实施例，所述生物膜组合降解处理进一步包括：多个所述升流区以及多个所述降流区中的每一个的底部，均设置有所述第二曝气口，所述方法进一步包括：根据污水的来水水质，控制多个所述第二曝气口的开关，以便控制多个所述升流区以及多个所述降流区中的每一个的处理环境。由此，可以根据来水水质灵活地选择污水处理环境为好氧、厌氧和/或缺氧，进一步提升出水水质。
根据本发明的实施例，所述污水处理方法进一步包括：根据污水的来水水质，将进水箱中的污水，供给至臭氧填充柱中；或将进水箱中的污水，供给至所述臭氧催化氧化单元中。由此，可以进一步提升出水水质。
附图说明
图1显示了根据本申请一个实施例的污水处理系统的结构示意图；
图2显示了根据本申请一个实施例的陶瓷膜组件的部分结构俯视图；
图3显示了根据本申请另一个实施例的陶瓷膜组件的部分结构俯视图；
图4显示了根据本申请一个实施例的生物膜组合处理单元的结构示意图；
图5显示了根据本申请另一个实施例的污水处理系统的结构示意图；
图6显示了根据本申请又一个实施例的污水处理系统的结构示意图；
图7显示了根据本申请一个实施例的污水处理方法的方法流程图；以及
图8显示了根据本申请另一个实施例的污水处理方法的方法流程图。
附图标记：
1000：污水处理系统；100：进水箱；200：臭氧流化床处理单元；210：第一壳体；220：陶瓷膜组件；221：陶瓷膜；222：隔流板；223：膜组件壳体；230：第一水流通道；240：第一曝气口；300：生物膜组合处理单元；310：第二壳体；320：隔板；321：第一水流通孔；322：第二水流通孔；330：生物反应空间；331：第一隔板；332：升流区；333：降流区；334：第二水流通道；335：辅助第一进水口；336：回流出水口；337：回流进水口：340：膜过滤空间；341：膜组件；350：生物载体填料；361：第二曝气口；362：膜过滤曝气口；363：曝气管路；10：第一进水口；20：第一出水口；30：第二进水口；40：第二出水口；400：净水箱；500：臭氧填充柱；510：填充柱进水端；520：填充柱出水端。
具体实施方式
下面详细描述本申请的实施例，所述实施例的示例在附图中示出，其中自始至终相同或类似的标号表示相同或类似的元件或具有相同或类似功能的元件。下面通过参考附图描述的实施例是示例性的，仅用于解释本申请，而不能理解为对本申请的限制。
需要说明的是，在本申请的各个方面中所描述的特征和效果可以互相适用，在此不再赘述。
本申请是基于发明人对以下事实和问题的发现和认识作出的：
目前的污水处理系统的出水水质不佳，出水中仍然残留有难降解的有机污染物，并且污水处理成本比较高。发明人经过深入研究发现，这是由目前的臭氧催化氧化反应器、微生物反应器、污水处理系统以及处理工艺均存在缺陷导致的。
在本申请的一个方面，本申请提出了一种污水处理系统。根据本申请的实施例，参考图1，污水处理系统1000包括：进水箱100、臭氧流化床处理单元200以及生物膜组合处理单元300。总的来说，该污水处理系统1000可根据来水水质灵活选择污水处理单元，操作方便，适用性强。
臭氧流化床处理单元200与进水箱100相连，并且臭氧流化床处理单元200包括：第一壳体210以及垂直设置在第一壳体210中的陶瓷膜组件220，其中，陶瓷膜组件220包括一个或多个陶瓷膜221，陶瓷膜组件220与第一壳体210的侧壁、顶面以及底面之间，均预留有互相连通的第一水流通道230(如图1所示出的，陶瓷膜组件220与第一壳体210的侧壁之间的第一水流通道230A、陶瓷膜组件220与第一壳体210的顶面之间的第一水流通道230B以及陶瓷膜组件220与第一壳体210的底面之间的第一水流通道230C)，第一壳体210底部设置有第一曝气口240，第一壳体210的上部设置有第一进水口10，第一壳体210的上部与第一进水口10相对的一侧设置有第一出水口20，并且通过第一进水口10，可将污水从陶瓷膜组件220与第一壳体210的侧壁之间的第一水流通道230A供给至陶瓷膜组件220中。由此，污水可在陶瓷膜组件220以及第一水流通道230之间环流流动，从而加强了传质，提高了该臭氧流化床处理单元200内的传质速率，使出水更加优质稳定，并且降低了污水处理成本。
根据本申请的实施例，生物膜组合处理单元300包括：第二壳体310、设置在第二壳体310中的隔板320、隔板320在第二壳体310中限定出的生物反应空间330以及膜过滤空间340。其中，第二壳体310靠近生物反应空间330的一侧设置有第二进水口30，第二进水口30分别与进水箱100以及第一出水口20相连，第二壳体310靠近膜过滤空间340一侧的顶部设置有第二出水口40，生物反应空间330中设置有生物载体填料350，生物反应空间330 的底部设置有第二曝气口361，隔板320的底部设置有第一水流通孔321，膜过滤空间340中设置有膜组件341，且膜过滤空间340的底部设置有膜过滤曝气口362。由此，该生物膜组合处理单元300不仅耐冲击负荷，构造简单紧凑，占地面积小，污泥膨胀率低，减小了游离微生物对膜组件341的污染，并且还具有以下优点：一方面，膜组件341可以过滤脱落的微生物，从而使出水更加优质稳定；另一方面，污水从隔板320底部的第一水流通孔321流入膜过滤空间340，并在膜过滤曝气口362曝气产生的气水升力的作用下，从第二壳体310顶部的出水口20排出的过程中，可以清洁膜组件341表面，进一步减小了膜污染，降低了运行压力和生产成本。
为了方便理解，下面首先对根据本申请实施例的污水处理系统能够实现上述有益效果的原理进行说明：
一方面，发明人发现，目前的臭氧催化氧化反应器普遍存在催化氧化效率较低、成本较高等问题。发明人经过深入研究发现，这主要是由臭氧、污水和催化剂(即气液固三相)的接触不够充分造成的。例如，传统的臭氧填充床反应器，臭氧、污水和催化剂的接触方式比较单一，一般只通过同向流或者异向流的方式接触反应，臭氧、污水和催化剂之间接触不够充分，从而限制了臭氧与污水中有机物的传质过程，导致催化氧化效能整体偏低，难以进一步降低污水的COD值，并且造成臭氧利用率低，污水处理成本较高的问题。根据本申请实施例的臭氧流化床处理单元200，将陶瓷膜组件220设置在第一壳体210的中心，即在陶瓷膜组件220与第一壳体210的侧壁、顶面以及底面之间，均预留由互相连通的第一水流通道230，由此，污水可从陶瓷膜组件220的底部，在第一曝气口240曝气产生的气水升力的作用下，上升至陶瓷膜组件220的顶部，并且通过陶瓷膜组件220与第一壳体210的顶面之间的第一水流通道230B向下环流，经过陶瓷膜组件220与第一壳体210的侧壁之间的第一水流通道230A以及陶瓷膜组件220与第一壳体210的底面之间的第一水流通道230C，重新从底部回流至陶瓷膜组件220中。由此，污水在陶瓷膜组件220与第一水流通道230之间环流流动，并且污水可以向陶瓷膜组件220四周的各个方向进行环流流动，从而极大地加强了传质，提高了臭氧流化床处理单元200内的传质速率，使出水更加优质稳定，并且降低了污水处理成本。
另一方面，发明人发现，目前利用微生物处理污水的方法，均存在一些缺陷。例如，生物膜法虽然具有耐冲击负荷、占地面积小、污泥膨胀率低等优点，反应器内游离微生物也较少，然而在实际运行中，微生物群容易从生物载体填料表面脱落，使得出水澄清度降低，出水水质不稳定。另一方面，膜生物反应器(MBR)作为一种由膜分离单元与生物处理单元相结合的新型水处理技术，具有出水优质稳定、剩余污泥量少、占地面积小等优点，然而传统的MBR中污泥浓度较高，游离微生物的存在容易形成膜污染，导致出水压力与运 行成本的增加。而根据本申请实施例的生物膜组合处理单元300，参考图1，通过工艺改造，一方面，在传统生物膜法的基础上，在生物反应空间330的一侧设置膜过滤空间340，并且膜过滤空间340中设置有膜组件341，膜组件341可以有效过滤从生物载体填料350表面脱落的微生物群，从而使出水更加优质和稳定，改善了传统生物膜法反应器的缺点；另一方面，将传统的MBR中的生物处理单元替换为具有生物载体填料350的生物反应空间330，减小了传统MBR中游离微生物对MBR膜组件的污染，改善了传统MBR的缺点。并且，根据本申请实施例的生物膜组合处理单元300，通过巧妙设计污水的流动路径，即污水从隔板320底部的第一水流通孔321流入膜过滤空间340，通过膜过滤曝气口362曝气产生气水升力的作用下，污水可以冲刷清洗膜组件341的表面，减小了膜污染，降低到了运行压力和成本。
又一方面，发明人发现，目前的污水处理系统以及处理工艺也存在一些缺陷。目前的污水处理系统，为了充分降解污水中的有机物，一般会将多个污水处理单元结合使用，例如，污水处理系统可以包括臭氧催化氧化处理单元以及微生物处理单元等。目前的污水处理系统，多个处理单元之间的连接方式是单向并且固定的，即污水在各个处理单元中的流动方向以及流动路径是固定的。因此，该污水处理系统不能根据来水的水质以及污水处理情况，灵活选择合适的污水处理单元以及污水流动路径，从而导致该污水处理系统的适用范围受限，并且会导致污水处理效果不佳以及浪费污水处理成本。而根据本申请实施例的污水处理系统1000，首先臭氧流化床处理单元200以及生物膜组合处理单元300均具有较好的污水处理效果，因此可以保证每个单元中出水水质的稳定。其次，进水箱100分别与臭氧流化床处理单元200以及生物膜组合处理单元300相连，即可以根据污水来水的水质，决定将污水供给至哪一个单元中进行处理，避免了污水固定地通过该系统中的每一个单元，造成处理时间的延长以及设备运行成本的升高。即：根据本申请实施例的污水处理系统，通过巧妙设计各个污水处理单元，例如进水箱100、臭氧流化床处理单元200以及生物膜组合处理单元300之间的连接方式，使污水既可以从进水箱100依次经过臭氧流化床处理单元200以及生物膜组合处理单元300的处理，也可以只经过臭氧流化床处理单元200，或者只经过生物膜组合处理单元300的处理，由此，根据本申请实施例的污水处理系统1000，可以根据来水水质灵活选择污水处理单元，操作方便，其适用性强，出水优质，并且节省污水处理成本。
下面，根据本申请的实施例，对该系统的各个单元及其工作原理、运行方式进行详细说明：
根据本申请的实施例，第一壳体210以及第二壳体310的大小不受特别限制，本领域技术人员可以根据污水处理场地的大小、所处理污水的水质和处理量等情况灵活选择。灵 活选择。并且，根据本申请实施例的污水处理系统，通过一体化的结构设计，减少了各个污水处理单元之间的连接管路，进而减少了各个连接管路造成的水头损失，该污水处理装置的工艺衔接更为紧凑流畅，因而，更容易将该污水处理装置放大，制作成大型的污水处理装置。
根据本申请的实施例，臭氧流化床处理单元200中，陶瓷膜组件220的大小不受特别限制，只要能使陶瓷膜组件220位于第一壳体210的中心，即陶瓷膜组件220与第一壳体210的侧壁、顶面以及底面之间均预留有互相连通的第一水流通道230即可。具体的，陶瓷膜组件220的大小可以根据第一壳体210的大小来进行设置。根据本申请的实施例，陶瓷膜组件220可以包括一个或多个陶瓷膜221，陶瓷膜221的具体材料不受特别限制，可以为常规的陶瓷膜，只要能过滤污水、截留粒径较小的催化剂即可。根据本申请的实施例，陶瓷膜组件220内只有一个陶瓷膜221时，污水可以在陶瓷膜组件220以及第一水流通道230之间两面环流流动。陶瓷膜组件220内有多个陶瓷膜221时，污水可以在陶瓷膜组件220以及第一水流通道230之间四面环流流动。根据本申请的实施例，陶瓷膜221的孔道中还可以包括具有催化作用的金属，例如二氧化锰颗粒，从而陶瓷膜221可以在过滤出水的同时，在其孔道中催化臭氧氧化反应。由此，一方面有利于进一步氧化降解污水中的有机物，提升出水水质；另一方面，通过陶瓷膜孔道内的臭氧氧化反应，可以有效地减小膜污染，降低出水压力和能耗。根据本申请的实施例，陶瓷膜221的数目以及设置方式不受特别限制，只要能限定出污水在陶瓷膜组件220内向上流动的流道即可。根据本申请的实施例，陶瓷膜组件220可以进一步包括设置在陶瓷膜221之间的隔流板222，由此，隔流板222可在陶瓷膜221之间限定出更多污水向上流动的流道，从而进一步加强了传质，提高了臭氧流化床处理单元200内的传质速率，使出水更加优质稳定。根据本申请的实施例，隔流板222的数目以及设置方式不受特别限制，只要能分割出多个污水向上流动的流道即可。例如，参考图2，隔流板222可以平行于陶瓷膜221设置；参考图3，隔流板222也可以垂直于陶瓷膜221设置。根据本申请的实施例，陶瓷膜组件220可以进一步包括膜组件壳体223，膜组件壳体223环绕多个陶瓷膜221设置，即膜组件壳体223可以具有4个侧壁，4个侧壁与第一壳体210的侧壁之间，均预留有第一水流通道230。由此，膜组件壳体220可以较好地支撑和固定多个陶瓷膜221，并且污水可在陶瓷膜壳体223与第一水流通道230之间四面环流流动，进一步加强了传质，提高了该臭氧流化床处理单元200内的传质速率。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，臭氧流化床处理单元200可以进一步包括臭氧产生装置(图中未示出)，臭氧产生装置与第一曝气口240相连。由此，臭氧产生装置可向第一壳体210中提供臭氧，促进污水中有机物的臭氧氧化分解，使出水更加优质。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，臭氧流化床处理单元200可以进一步包括设置在第一壳体210上的第一催化剂入口(图中未示出)。由此，可通过第一催化剂入口向第一壳体内提供第一催化剂，臭氧、污水以及第一催化剂可在陶瓷膜组件220以及第一水流通道230之间环流流动。在该过程中，臭氧、污水以及第一催化剂可以充分接触和反应，能更加充分地降解污水中的有机物，从而提升了有机物的臭氧催化氧化处理效率，提高了臭氧的利用率，降低了污水处理成本。根据本申请的实施例，第一催化剂的具体类型不受特别限制，只要能催化臭氧产生羟基自由基并氧化污水中的有机物即可。例如第一催化剂可以为颗粒状催化剂，也可以为粉末催化剂。根据本申请的实施例，第一催化剂的加入方式不受特别限制，可以直接将第一催化剂从第一催化剂入口加入，在第一曝气口240曝气产生的气水升力的作用下，第一催化剂可以在第一壳体210内处于流化状态，充分地与臭氧以及污水接触反应。根据本申请的另一些实施例，第一催化剂也可以涂覆在陶瓷膜221的表面，臭氧和污水在陶瓷膜组件220内环流流动时，也可以充分地与陶瓷膜221上的第一催化剂接触反应。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，臭氧化流床处理单元200可以进一步包括设置在第一壳体210上的双氧水入口(图中未示出)。由此，可通过双氧水入口向第一壳体210内提供双氧水，臭氧、双氧水、污水以及前面所述的第一催化剂可在陶瓷膜组件220以及第一水流通道230之间环流流动。在该过程中，臭氧、双氧水、污水以及第一催化剂可以充分接触和反应。并且在该过程中，臭氧和双氧水的协同作用有利于产生具有极强的氧化作用的羟基自由基，该羟基自由基可以对污水中的有机物进行充分的氧化降解，进一步提高了污水中有机物的氧化分解效率，提升了出水水质。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，臭氧流化床处理单元200可以进一步包括设置在第一壳体210内的紫外光照装置(图中未示出)，紫外光照装置适于向陶瓷膜组件220照射紫外光。由此，第一壳体210中的臭氧可在紫外光的作用下产生羟基自由基，进一步提高污水中有机物的臭氧氧化分解效率，提升出水水质。根据本申请的实施例，紫外光照装置也可以与第一催化剂以及双氧水的至少之一同时作用，由此，进一步提高了臭氧产生羟基自由基的速率，提高了污水中有机物的臭氧氧化分解效率，进一步提升出水水质。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，臭氧流化床处理单元200可以进一步包括设置在第一壳体210顶部的尾气回收口(图中未示出)，由此，第一壳体210内没有发生反应的臭氧以及曝气产生的空气可以从尾气回收口排出，提高了臭氧流化床处理单元200的安全性。
根据本申请的实施例，生物膜组合处理单元300中，隔板320的设置方式不受特别限 制，只要能在第二壳体310中分隔出垂直设置的生物反应空间330和膜过滤空间340，并且在隔板320的底部预留有第一水流通孔321即可，例如，可以在隔板320的底部与第二壳体310的底部之间留有间隙，以便形成第一水流通孔321。进一步地，隔板320可以设置为可在第二壳体310中沿垂直方向运动的，由此，可以通过隔板320在第二壳体310中沿垂直方向的运动，来简便地实现第一水流通孔321的打开和关闭。具体的，也可以在隔板320上设置水流截止阀，通过水流截至阀的开关，来简便地实现第一水流通孔321的打开和关闭。
根据本申请的另一些实施例，参考图4，隔板320的顶部也可以设置第二水流通孔322。第二水流通孔322的设置方式不受特别限制，例如，可以与第一水流通孔321的设置方式相同。由此，经过膜过滤空间340处理的污水可以翻越隔板320，并从隔板320顶部的第二水流通孔322流至生物反应空间330中，再通过隔板320底部的第一水流通孔321回流至膜过滤空间340中，形成内循环流动。该过程中，污水从膜过滤空间340底部向上流动，可以冲刷清洗膜组件341表面，减小膜污染，并且，该内循环流动能将从生物载体填料350表面脱落，并通过第一水流通孔321进入膜过滤空间340中的游离微生物，回流至生物反应空间330中并重新固定，由此，减少了膜过滤空间中400的游离微生物，进一步减小了膜污染，降低了出水压力和运行成本。此外，由于生物反应空间330中，微生物处理污水时会消耗溶解氧，因此，为了保证生物反应空间330的处理效果，通常需要对生物反应空间330进行强曝气处理。而根据本申请实施例的系统，由于膜过滤空间340将生物分解过程与膜过滤过程进行了分离，因此膜过滤空间340中并无显著的溶解氧消耗。因此，回流至生物反应空间330中的污水中，含有较多的溶解氧(依靠膜过滤第一曝气口620提供)，从而可以进一步增强生物反应空间330的处理效果，也可以节省生物反应空间的曝气量，进而降低运行成本。本领域技术人员能够理解的是，传统的MBR污水处理过程，依靠在污泥中添加微生物，与过滤膜进行复合，实现污水的处理。而在根据本申请实施例的系统中，也可以有部分含有微生物的污泥，进入膜过滤空间340中。由于膜过滤空间340底部设置有膜过滤曝气口362，且水流方向平行于膜组件341，因此膜组件341也不会因有污泥进入膜过滤空间340，而造成污染。
根据本申请的实施例，膜组件341的具体种类不受特别限制，只要将膜组件341垂直设置在膜过滤空间340中即可，例如可以为微滤膜、超滤膜的至少之一。根据本申请的实施例，膜组件341的材质不受特别限制，例如可以为有机膜也可以为无机膜。滤膜的具体形状也不受特别限制，可以为平板膜以及中空纤维膜的至少之一。
根据本申请的实施例，生物载体填料350的种类和数目不受特别限制，只要能有助于微生物的附着以及有助于污水与微生物的充分接触和反应即可，例如，可以为悬挂式纤维 填料、填充式颗粒填料的至少之一。根据本申请的实施例，生物载体填料350还可以包括第二催化剂，第二催化剂的具体种类不受特别限制，只要能使污水中的有机物发生催化氧化反应即可。由此，污水供给至生物反应空间330时，不仅可以进行生化处理，还可以进行化学氧化处理，进一步提升了出水水质。尤其待处理污水中的BOD/COD比较低、污水的可生化性较差时，通过第二催化剂的化学氧化处理，可以提高污水的BOD/COD比，从而有利于微生物对污水进行生化处理，进一步提升了出水水质。
根据本申请的实施例，生物膜组合处理单元300可以进一步包括：吸附剂入口(图中未示出)，吸附剂入口可以设置在第二壳体310靠近生物反应空间330的一侧。由此，可以通过吸附剂入口向生物反应空间330中加入可以吸附生物以及有机质的粉末，例如活性炭粉末，由此，可以进一步提升出水水质。
根据本申请的实施例，参考图4，第一隔板331可以垂直设置在生物反应空间330中，并且第一隔板331的顶部与第二壳体310之间或者第一隔板331的底部与第二壳体310之间均预留有第二水流通道334(参考图4中的334A以及334A’)，第二壳体310、第一隔板331以及隔板320之间，限定出依次排列的升流区332以及降流区333(参考图4中的箭头所示出的水流方向)。由此，污水可在生物反应空间330内折流式流动，增大了污水与生物载体填料350(图中未示出)的接触面积，从而提高了污水处理效率。根据本申请的实施例，生物膜组合处理单元300可以包括多个平行排列的第一隔板331，也即是说，第一隔板331的数目不受特别限制，本领域技术人员可以根据所处理污水的水质和水量等情况进行合理设计，多个第一隔板331可以在生物反应空间330内限定出多个依次排列的升流区332以及降流区333，从而进一步增大了污水与生物载体填料的接触面积，提高了污水处理效率。根据本申请的实施例，第二水流通道334的具体设置方式不受特别限制，例如，可以沿着水流在生物反应空间330中流通的方向(如图4中的箭头所示出)，在第一隔板331的顶部与第二壳体310之间或者第一隔板331的底部与第二壳体310之间留有间隙即可。进一步地，第一隔板331可以在生物反应空间330中沿垂直方向运动，由此，第一隔板331在生物反应空间330中沿垂直方向的运动，可以简便地实现第二水流通道334的打开和关闭。根据本申请的另一些实施例，第二水流通道334也可以由设置在第一隔板331上水流截止阀来实现第二水流通道334的打开和关闭。由此，可以根据所处理污水的水质来调节生物反应空间330内的污水的流动路径，操作方便而且灵活。
根据本申请的实施例，生物反应空间330的底部设置有多个第二曝气口361，第二曝气口361位于升流区332以及降流区333的至少之一的底部。具体的，第二曝气口361可位于每个升流区332以及降流区333中。由此，通过控制多个第二曝气口361的打开和关闭，可以简便地调节每一个升流区332以及每一个降流区333中的溶解氧含量，有利于根据需 要在升流区332以及降流区333中形成好氧、厌氧或者缺氧环境，以便微生物对污水进行好氧、缺氧或者厌氧处理，进一步提高了出水水质。此时，每一个升流区332以及每一个降流区333中的处理环境，均可以通过第二曝气口361的开关，或是供气量进行调节。曝气产生的气水升力还有助于升流区332中的污水向上流动。根据本申请的具体实施例，可以打开升流区332中的第二曝气口361，并关闭降流区333中的第二曝气口361，由此，升流区332中形成好氧环境，有助于微生物对污水中有机物进行降解以及硝化反应的进行，降流区333中不进行曝气，因此降流区333中的溶解氧含量相对较低，容易形成厌环境，有利于微生物对污水中的有机物进行处理，并发生反硝化脱氮反应，进一步提升出水水质。当生物反应空间330内包含多个依次排列的升流区332以及降流区333时，污水可在生物空间300内依次进行多级的好氧处理以及厌/缺氧处理，由此，能更加充分地去除污水中的有机物，进一步提升污水处理效率和出水水质。根据本申请的实施例，升流区332以及降流区333的体积可以相同也可以不相同，例如，根据本申请的具体实施例，参考图3，升流区332的体积可以小于降流区333的体积。由此，污水在降流区333中的下降速度相对较慢，有利于污水中溶解氧的排出，从而有利于在降流区333内形成厌氧或缺氧环境，微生物可以对污水中的有机物进行充分的厌氧或缺氧处理，例如发生反硝化脱氮反应，进一步提高污水处理效率和出水水质。本领域技术人员能够理解的是，上述的具体实施例，仅为了说明本申请，而不能够理解为对升流区332以及降流区333中的处理环境的限制。本领域技术人员可根据污水水质的实际情况，对每个升流区332以及降流区333的环境进行调节，且每一个升流区332以及降流区333的处理环境，均可单独控制为好氧、缺氧或者厌氧。
根据本申请的实施例，位于生物反应空间330的第二曝气口361以及位于膜过滤空间340底部的膜过滤曝气口362的设置方式不受特别限制，例如，可以在第二壳体310的底部设置曝气管路363，并在曝气管路363的适当位置穿孔，进而形成第二曝气口361以及膜过滤曝气口362。进一步地，形成的第二曝气口361以及膜过滤曝气口362均可以为能够闭合，或可兼具调节曝气量的功能，由此，可以灵活地调节生物反应空间内不同区域的溶解氧含量，以便根据需要形成多种好氧、缺氧以及厌氧环境。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，参考图4，生物膜组合处理单元300可以进一步包括：回流出水口336以及回流进水口337，回流出水口336设置在靠近膜过滤空间340的降流区333的底部，回流进水口337设置在靠近第一进水口10的升流区332的底部，回流出水口336以及回流进水口337之间通过水流管路相连。由此，可以根据所处理的污水水质，简便地使污水在生物反应空间330内循环处理，进一步提高了出水水质。根据本申请的实施例，回流进水口337的设置方式不受特别限制，例 如可以直接将设置在第二壳体310上的进水口10作为回流进水口337，由此可以更加方便地将污水回流入生物反应空间330内。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，参考图5，污水处理系统1000可以进一步包括：净水箱400，净水箱400与第一进水口10、第一出水口20以及第二出水口40相连。由此，该污水处理系统可以具有较为灵活的处理流程。具体的，进水箱100中的污水，可以依次经过臭氧流化床处理单元200以及生物膜组合处理单元300处理，然后保存在净水箱400中。或者，进水箱100中的污水也可以仅经过臭氧流化床处理单元200处理，直接储存至净水箱400中。或者，进水箱100中的污水可以先流入生物膜组合处理单元300中进行处理，处理后排出至净水箱400中之后，再供给至臭氧流化床处理单元200中，进行臭氧催化氧化的处理。由此，该污水处理系统1000可根据来水水质灵活选择污水处理单元，操作方便，适用性强。
根据本申请的实施例，污水处理系统1000还可以包括：反冲洗单元(图中未示出)，用于对陶瓷膜组件220以及膜组件341进行反冲洗。反冲洗单元的具体结构以及反冲洗的过程不受特别限制，本领域技术人员可以根据实际情况进行选择。例如，可以采用该污水处理系统产出的经过处理的水，进行反冲洗，或单独设置反冲洗水箱进行反冲洗，从而可进一步减轻膜污染，降低出水压力和运行成本。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，污水处理系统1000可以进一步包括设置在第一壳体210中部以及第二壳体310中部的取样口(图中未示出)。由此，可以简便地对第一壳体210以及第二壳体310内的水质进行实时监测。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，污水处理系统1000可以进一步包括设置在第一壳体210以及第二壳体310底部的排空口(图中未示出)。由此，可以简便地根据需要对第一壳体210以及第二壳体310进行排空以及检修。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，污水处理系统1000可以进一步包括设置在第一壳体210以及第二壳体310顶部的溢流口(图中未示出)。由此，可以在第一壳体210以及第二壳体310内液位过高时，对污水处理单元1000进行溢流保护，进一步提高该污水处理系统的使用性能。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，污水处理系统1000可以进一步包括液位控制单元(图中未示出)，用于调控进入第一壳体210以及第二壳体310内的污水量。具体的，液位控制单元可以包括液位传感器和进水泵(图中未示出)，液位传感器可以监测第一壳体210内以及第二壳体310的水位并且能控制进水泵的启停，由此，可以简便地调节第一壳体210以及第二壳体310内的污水量。
根据本申请的实施例，参考图6，污水处理系统1000可以进一步包括：至少一个臭氧 填充柱500，臭氧填充柱500具有填充柱进水端510以及填充柱出水端520，填充柱进水端510与进水箱100相连，填充柱出水端520分别与臭氧流化床处理单元200以及生物膜组合处理单元300相连。即：污水经过臭氧填充柱500处理后，可以经过臭氧流化床处理单元200以及生物膜组合处理单元300的至少之一处理。由此，可以进一步对污水中的有机物进行臭氧氧化处理，进一步提升出水水质。根据本申请的实施例，填充柱进水端510以及填充柱出水端520的具体设置位置不受特别限制，具体的，填充柱进水端510可以设置在臭氧填充柱500的上部，填充柱出水端520可以设置在臭氧填充柱500的下部，污水可以从臭氧填充柱500的上部流入，并从其下部流出，从而污水可在臭氧填充柱500中逆向流流动，从而有利于臭氧和污水中的有机物充分接触反应。根据本申请的实施例，臭氧填充柱500的类型以及数目不受特别限制，例如，可以如图6中所示出的两个，进水箱100可以与填充柱进水端510A相连，也可以与填充柱进水端510A’相连，并且多个臭氧填充柱500的连接方式也不受特别限制，可以为并联或者串联，本领域技术人员可以根据需要进行设置。
为了进一步提高污水处理系统的污水处理性能，根据本申请的实施例，污水处理系统1000可以进一步包括：混凝沉淀池，保安过滤器等污水处理单元，混凝沉淀池以及保安过滤器可以为本领域常规使用的，只要能对污水进行净化处理即可。
发明人发现，根据本申请实施例的污水处理系统，通过耦合臭氧填充柱、臭氧催化氧化处理单元以及生物膜组合处理单元等，并且根据来水水质灵活选择污水处理单元，操作方便，污水中的有机物可以得到充分地氧化降解，污水处理效果良好，尤其在处理含难降解有机物较多的煤化工污水时，该污水处理系统也能获得较佳的污水处理效果。
总的来说，根据本申请实施例的污水处理系统，各个单元均具有合理的结构设计，可以保证该单元的污水处理效果，提供稳定的出水水质。并且，进水箱分别和臭氧填充柱、臭氧流化床处理单元以及生物膜组合处理单元相连，由此可以根据进水箱来水的水质，决定将污水首先供给至哪一个单元中进行处理，即该污水处理系统可以根据水质决定该系统中处理污水的具体过程，操作灵活方便。因此，该系统不仅可以用于处理可生化性极差的污水(如煤化工废水等)，也可以用于处理一般污水，而不会造成系统运行成本过高。
在本申请的另一方面，本申请提出了一种利用前面所述的污水处理系统进行污水处理的方法。由此，该污水处理方法可以具有前面所述的污水处理系统所具有的全部特征以及优点。根据本申请的实施例，该方法包括：利用所述臭氧流化床处理单元以及所述生物膜组合单元，对所述污水进行臭氧流化床催化氧化处理以及生物膜组合降解处理的至少之一，对污水进行处理。
根据本申请的实施例，参考图7，臭氧流化床催化氧化处理包括：
S110：将污水从第一进水口供给至臭氧流化床处理单元中
在该步骤中，将污水从第一进水口供给至臭氧流化床处理单元中。根据本申请的实施例，在该步骤中，将待处理的污水从第一进水口供给至第一壳体，并通过第一壳体的侧壁与陶瓷膜组件之间的第一水流通道，供给至陶瓷膜组件中。
S120：污水在陶瓷膜组件以及第一水流通道之间形成环流
在该步骤中，污水在陶瓷膜组件以及第一水流通道之间环流流动。污水可从陶瓷膜组件的底部，在第一曝气口曝气产生的气水升力的作用下，上升至陶瓷膜组件的顶部，并且通过陶瓷膜组件与第一壳体的顶面之间的第一水流通道向下环流，经过陶瓷膜组件与壳体的侧壁之间的第一水流通道以及陶瓷膜组件与第一壳体的底面之间的第一水流通道，重新从底部回流至陶瓷膜组件中。由此，污水可在陶瓷膜组件与第一水流通道之间环流流动，并且污水可以向陶瓷膜组件四周的各个方向进行环流流动，从而极大地加强了传质，提高了臭氧流化床处理单元中的传质速率，使出水更加优质稳定，并且降低了污水处理成本。
根据本申请的实施例，该污水处理方法进一步包括：向第一壳体内加入第一催化剂，从第一曝气口曝臭氧气体以及空气，使污水以及催化剂从陶瓷膜组件的底部上升，并从陶瓷膜组件和第一壳体的顶面之间的第一水流通道，流至陶瓷膜组件和第一壳体的侧壁之间的第一水流通道并下降，在曝气条件下上升，以便形成所述环流。由此，臭氧、污水以及第一催化剂可以在该环流过程中，充分接触和反应，促进了污水中有机物的臭氧催化氧化分解，提升了出水水质。
根据本申请的实施例，该污水处理方法可以进一步包括：由双氧水入口向壳体中加入双氧水，臭氧、双氧水、污水以及第一催化剂在陶瓷膜组件以及第一水流通道之间环流流动。在该过程中，臭氧、双氧水、污水以及第一催化剂可以充分接触和反应。并且在该过程中，臭氧和双氧水的协同作用有利于产生具有极强的氧化作用的羟基自由基，进而可以对污水中的有机物进行充分的氧化降解，进一步提高了污水中有机物的氧化分解效率，提升了出水水质。
根据本申请的实施例，该污水处理方法可以进一步包括：由设置在第一壳体内的紫外光照装置向陶瓷膜组件照射紫外光。由此，第一壳体中的臭氧可在紫外光的作用下产生羟基自由基，进一步提高污水中有机物的臭氧氧化分解效率，提升出水水质。根据本申请的实施例，也可以将紫外光照装置与第一催化剂以及双氧水的至少之一同时使用，由此，进一步提高了臭氧产生羟基自由基的速率，提高了污水中有机物的臭氧氧化分解效率，进一步提升出水水质。
S130：污水经陶瓷膜组件过滤处理后，从第一出水口排出
在该步骤中，污水经陶瓷膜组件过滤处理后，从第一出水口排出。根据本申请的实施例，可以通过出水泵，将经陶瓷膜组件过滤处理后的净水抽吸至净水箱中。根据本申请的 实施例，该污水处理方法进一步包括：可以采用该污水处理系统产出的经过处理的水，或单独设置反冲洗水箱对陶瓷膜组件进行反冲洗，从而进一步减轻膜污染。
根据本申请的实施例，参考图8，生物膜组合降解处理包括：
S210：将污水从第二进水口供给至生物膜组合处理单元中
在该步骤中，将待处理的污水从第二进水口供给至生物反应空间，以便在曝气条件下，令生物载体填料中的微生物，与污水发生反应，对污水进行净化处理。
根据本申请的实施例，当生物反应空间内设置多个第一隔板时，多个第一隔板可以在生物反应空间内限定出多个依次排列的升流区以及降流区，污水可在生物反应空间内折流式流动，从而增大了污水与生物载体填料的接触面积，提高了污水处理效率。根据本申请的实施例，可以对升流区进行曝气，可在升流区形成好氧环境，以便微生物对污水中有机物进行降解以及硝化反应的进行。降流区中不进行曝气，因此降流区中的溶解氧含量相对较低，容易形成厌氧环境，有利于微生物对污水中的有机物进行处理，并发生反硝化脱氮反应，进一步提升出水水质。根据本申请的实施例，当生物反应空间内包含多个依次排列的升流区以及降流区时，污水可在生物空间内依次进行多级的好氧处理以及厌氧处理，由此，能更加充分地去除污水中的有机物，进一步提升污水处理效率和出水水质。
根据本申请的实施例，当生物反应空间内包含多个升流区以及降流区时，污水向生物反应空间的供给位置以及供给方式可以灵活多样，本领域技术人员可以根据所处理的污水水质以及水量等进选择。例如，根据本申请的实施例，当污水水质较差时，可以从设置在第二壳体靠近生物反应空间的侧壁上的第二进水口供给至生物反应空间，从而利用全部生物反应空间进行处理；污水水质好，可以选择从设置在降流区的多个辅助第一进水口中的一个，供给至升流区中，并关闭限定出该降流区的第一隔板顶部与第二壳体之间的第二水流通道，利用部分生物反应空间处理。由此，可以简便地调节进水位置以及水力停留时间，可以根据所处理的污水水质选择合适的生物反应空间的体积，有助于降低处理成本。
S220：污水在生物反应空间中经微生物处理，并从隔板底部的水流通孔供给至膜过滤空间
在该步骤中，将经微生物处理的污水，从隔板底部的水流通孔供给至膜过滤空间。根据本申请的实施例，膜过滤空间的底部可以设置膜过滤曝气口，由此，经微生物处理的污水从隔板底部的第一水流通孔供给至膜过滤空间后，在膜过滤曝气口曝气产生气水升力的作用下，向上流动，并且可以从第二壳体顶部的第二出水口排出，或者可以翻越过隔板，并从隔板顶部与第二壳体之间的第二水流通孔回流至与膜过滤空间靠近的降流区中，该过程中上升的水流可以冲洗清洁膜组件，进一步减少了膜污染。并且，从上述水流空隙流入与膜过滤空间靠近的降流区中的污水，可以进一步地从隔板底部的水流通孔流入膜过滤空 间，如此形成一个污水内循环流动过程，该内循环过程可以反复冲洗膜组件，由此，可以较大程度地减小膜污染，并且，该内循环流动能将从生物载体填料表面脱落，并通过第一水流通孔膜过滤空间中的游离微生物，回流至生物反应空间中并重新固定，由此，减少了膜过滤空间中的游离微生物，进一步减小了膜污染，降低了出水压力和运行成本。根据本申请的实施例，可以采用该污水处理系统产出的经过处理的水，或单独设置反冲洗水箱对膜组件进行反冲洗，从而进一步减轻膜污染。
S230：污水经膜组件过滤处理后，从第二出水口排出
在该步骤中，将经过膜组件过滤的污水，从位于膜过滤空间顶部的第二出水口排出。根据本申请的实施例，在该步骤中，水流从膜过滤空间的底部上升到膜过滤空间的顶部并排出时，水流可以清洁膜组件表面，从而进一步减小了膜污染，降低了运行压力和生产成本。
根据本申请的实施例，生物膜组合降解处理进一步包括：打开回流出水口，将经过靠近膜过滤空间的降流区的污水，通过回流进水口供给至靠近进水口的升流区。由此，可以根据所处理污水的水质，使污水在生物反应空间内循环处理，进一步提高了出水水质，并且操作方便。根据本申请的实施例，根据所处理污水的水质，经过靠近膜过滤空间的降流区处理的污水，可以检测其出水水质，如果其中的有机物含量仍然较高，可以通过回流出水口排出，并供给至靠近进水口的升流区中，继续进行生化处理。
根据本申请的实施例，多个升流区以及多个降流区中的每一个的底部，均设置有第二曝气口。根据污水的来水水质，控制多个第二曝气口的开关，进而控制多个升流区以及多个降流区中的每一个的处理环境。由此，可以根据来水水质灵活地选择污水处理环境为好氧、厌氧和/或缺氧，进一步提升出水水质。具体的，控制第二曝气口开关，调节污水处理环境，可以包括但不限于以下步骤：
可以打开升流区的曝气口，关闭降流区的曝气口，以便在升流区中形成好氧环境，在降流区中形成缺氧环境，以便对污水进行多级好氧-缺氧处理。由此，可以进一步提升出水水质。
根据本申请的实施例，可打开升流区以及降流区的第二曝气口，以便升流区以及降流区中形成好氧环境，以便对污水进行好氧处理。由此，可以进一步提升出水水质。
根据本申请的实施例，可关闭升流区以及降流区的第二曝气口，以便升流区以及降流区中形成厌氧/缺氧环境，以便对污水进行厌氧/缺氧处理。由此，可以进一步提升出水水质。
可以关闭靠近进水口的一个或多个升流区底部的曝气口，即在靠近进水口的升流区以及降流区中形成厌氧环境，而打开靠近膜过滤空间的升流区的曝气口，关闭靠近膜过滤空间的降流区的曝气口，由此，生物反应空间内形成了厌氧-多级(好氧-缺氧)的污水处理环 境，可以进一步降解污水中的有机物，提升出水水质。
需要说明的是，各个升流区以及降流区中的污水处理环境，可以根据水质的变化情况(通过取样口对系统中的污水进行实时监测)随时调整。也即是说，每个升流区以及降流区都可以根据需要形成好氧、缺氧或者厌氧环境，采用最佳的组合方式对污水中的有机物进行高效降解。综上可知，该污水处理方法可以简便地对污水进行生化处理，出水水质更加稳定，并且可减小膜污染。
根据本申请的实施例，由于前面描述的系统具有灵活的连接方式，因此，可以根据污水的具体情况，决定该系统进行水处理的具体操作。根据本申请的具体实施例，污水处理方法还可以进一步包括：根据污水的来水水质，将进水箱中的污水，供给至臭氧填充柱中；或将进水箱中的污水，供给至所述臭氧催化氧化单元中。由此，可以进一步提升出水水质。由此，可以耦合臭氧填充柱-臭氧流化床处理单元生物膜组合处理单元，对污水中的有机物进行充分降解。
需要说明的是，根据本申请实施例的污水处理方法，污水的流动途径不受特别限制，本领域技术人员可以根据来水水质以及污水处理情况灵活选择。例如，污水可以只经过臭氧填充柱处理，可以只经过臭氧流化床处理单元处理，也可以只经过生物膜组合处理单元处理，以及可以经过这三种处理单元中的任意两种或者三种处理。上述处理的先后顺序不受特别限制，例如，也可以先进行生物膜组合处理单元处理，在经过臭氧流化床处理单元处理。该污水处理方法操作灵活方便，适用性广泛，尤其对于含难降解有机物较多的煤化工废水，处理效果良好。
综上可知，该污水处理系统可以简便地对污水进行臭氧催化氧化处理以及生物膜组合降解处理的至少之一，加强了传质，提高了该臭氧流化床处理单元内的传质速率，并且使出水水质更加优质稳定，可减小膜污染，降低出水压力和运行成本，并且该污水处理方法可根据来水水质灵活选择污水处理单元，操作方便，适用性强。
下面将结合实施例对本申请的方案进行解释。本领域技术人员将会理解，下面的实施例仅用于说明本申请，而不应视为限定本申请的范围。实施例中未注明具体技术或条件的，按照本领域内的文献所描述的技术或条件或者按照产品说明书进行。
实施例1
前处理-臭氧高级氧化处理-膜生物(MBR)组合处理
本实施例中，可采用多种前处理方式，如多介质过滤、沉淀等，具体的，以混凝沉淀与保安过滤为例。
本实施例中，可采用多种臭氧高级氧化工艺，各工艺间串并联形式不唯一，具体的，以 臭氧填充床与臭氧流化床串联为例。
1.混凝沉淀
(a)打开加药区搅拌器，转速300rpm；打开反应区搅拌器，转速50rpm。
(b)打开给水泵，同时打开加药泵。
2.保安过滤
(a)打开给水泵，排空阀出水后关闭。
(b)实时监测压力值，压力过高或出水量过小时，停止进水，更换滤芯。
3.臭氧高级氧化
3.1 填充床
该步骤中，采用一个臭氧填充柱进行处理。
(a)打开臭氧发生器与空气(氧气)进气，臭氧投加量50-150mg/L，大气压0.1MPa。
(b)打开顶部进水阀，打开给水泵，HRT 30min；也可采用顶部1/3处进水，则HRT＝20min.
装置停止运行时，可以进行反冲洗步骤。
可以采用两个并联的臭氧填充柱进行处理：
(a)打开臭氧发生器与空气(氧气)进气，臭氧投加量50-150mg/L，大气压0.1MPa；也可根据实际情况调节臭氧投加量。
(b)打开顶部进水阀，打开给水泵，单个填充柱HRT 60min；若皆采用顶部1/3处进水，则HRT＝40min.
类似地，也可增加反冲洗步骤。
3.3 臭氧流化床
(a)打开臭氧发生器与空气嚗气，臭氧投加量50-150mg/L。
(b)打开给水泵，开启液位自控；打开陶瓷膜产水泵，开启产水/反洗自控，产水7-9.5min，反洗45-60s，交替。
(c)检查压力表，过滤压力超过35kPa时或运行超过一周，进行在线药洗：
4.MBR处理
(a)打开曝气，24h持续曝气
(b)打开给水泵，最左端进水，所有隔板打开，HRT＝10h；通过超越进水和隔板开闭调整HRT，范围3-10h。
(c)打开产水泵，开启自控，出水5-7min，停30-120s。
(d)出水压力低于-30kPa时停止出水，膜箱液位低于膜片时禁止出水。
(e)出水压力低于-30kPa或运行超过一周，进行在线药洗。
(f)回流，污泥定期从膜池旁降流区回流到第一个池子进水端下方。
实施例2
臭氧填充床-MBR-臭氧流化床
该实施例适于若MBR出水COD仍较高的情况，即：采用流化床后置工艺：
本实施例的前处理方式可选多种，具体的，以多介质过滤为例
1.多介质过滤
采用石英砂过滤器进行前处理，介质可选石英砂、无烟煤、颗粒多孔陶瓷、锰砂等。
(a)打开过滤器进水阀、出水阀、开启进水泵，调整流量在规定的范围内；
(b)两套过滤器轮流使用，一台正常过滤，一台反冲洗；
(c)反冲洗过程，先关闭进水阀和出水阀，打开反冲洗进水阀、反冲洗排水阀和进气阀，清洗时间10-30min左右。
2.臭氧高级氧化
2.1 填充床
该步骤同实施例1，可采用单个填充床进行处理，也可采用两个并联的填充床进行处理。
3.MBR
该步骤中同实施例1。
4.臭氧流化床
流化床处理步骤同实施例1。
实施例3
臭氧填充床-臭氧流化床
该实施例适用于废水COD浓度较低，但可生化性极差的情况。
步骤1以及步骤2同实施例1，依次进行混凝沉淀以及保安过滤处理。
3.臭氧高级氧化
3.1 填充床
该步骤同实施例1，可采用单个填充床进行处理，也可采用两个并联的填充床进行处理。
4.臭氧流化床
该步骤处理参数同实施例1.
实施例4
MBR-臭氧流化床
该实施例适用于进水浓度较高且生化性较好的废水，即前端直接MBR生化，后接臭氧流化床强化氧化的工艺。本实施例中的工艺仅作为深度处理单元使用，不包含前处理单元。
1.MBR
该步骤处理参数同实施例1。
2.臭氧流化床
该步骤处理参数同实施例1。经臭氧流化床处理后直接出水。
以上详细描述了本申请的实施方式，但是，本申请并不限于上述实施方式中的具体细节，在本申请的技术构思范围内，可以对本申请的技术方案进行多种简单变型，这些简单变型均属于本申请的保护范围。
另外需要说明的是，在上述具体实施方式中所描述的各个具体技术特征，在不矛盾的情况下，可以通过任何合适的方式进行组合。
此外，本申请的各种不同的实施方式之间也可以进行任意组合，只要其不违背本申请的思想，其同样应当视为本申请所公开的内容。
在本申请的描述中，需要理解的是，术语“上”、“下”、“前”、“后”、“顶”、“底”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本申请和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本申请的限制。

Claims (20)

  1. 一种污水处理系统，包括：
    进水箱；
    臭氧流化床处理单元，所述臭氧流化床处理单元与所述进水箱相连，且包括：
    第一壳体；
    陶瓷膜组件，所述陶瓷膜组件垂直设置在所述第一壳体中，所述陶瓷膜组件包括一个或多个陶瓷膜，所述陶瓷膜组件与所述第一壳体的侧壁、顶面以及底面之间，均预留有互相连通的第一水流通道；
    第一进水口，所述第一进水口设置在所述第一壳体的上部，所述第一进水口可利用所述陶瓷膜组件与所述第一壳体的侧壁之间的所述第一水流通道，将污水供给至所述陶瓷膜组件中；
    第一出水口，所述第一出水口设置在所述第一壳体的上部，且与所述第一进水口相对设置；以及第一曝气口，所述第一曝气口设置在所述第一壳体的底部；以及
    生物膜组合处理单元，所述生物膜组合处理单元包括：
    第二壳体，所述第二壳体中设置有隔板，所述隔板在所述第二壳体中限定出生物反应空间以及膜过滤空间，所述隔板的底部具有第一水流通孔，所述第二壳体靠近所述生物反应空间的一侧具有第二进水口，所述第二进水口分别与所述进水箱以及所述第一出水口相连，所述第二壳体靠近所述膜过滤空间一侧的顶部具有第二出水口；
    生物载体填料，所述生物载体填料设置在所述生物反应空间中，且所述生物反应空间的底部，设置有第二曝气口；
    膜组件，所述膜组件垂直设置在所述膜过滤空间中，且所述膜过滤空间的底部，设置有膜过滤曝气口。
  2. 根据权利要求1所述的污水处理系统，所述陶瓷膜组件进一步包括膜组件壳体，所述膜组件壳体具有4个侧壁，所述4个侧壁与所述第一壳体的侧壁之间，均预留有所述第一水流通道。
  3. 根据权利要求1所述的污水处理系统，所述陶瓷膜组件进一步包括：设置在多个所述陶瓷膜之间的隔流板。
  4. 根据权利要求1所述的污水处理系统，所述臭氧流化床处理单元进一步包括：第一催化剂入口，所述第一催化剂入口设置在所述第一壳体上。
  5. 根据权利要求1所述的污水处理系统，所述臭氧流化床处理单元进一步包括：双氧 水入口，所述双氧水入口设置在所述第一壳体上。
  6. 根据权利要求1所述的污水处理系统，所述臭氧流化床处理单元进一步包括：紫外光照装置，所述紫外光照装置适于向所述陶瓷膜组件照射紫外光。
  7. 根据权利要求1所述的污水处理系统，所述生物膜组合处理单元中，所述隔板的顶部设置有第二水流通孔。
  8. 根据权利要求1所述的污水处理系统，所述生物膜组合处理单元中，所述生物反应空间中具有第一隔板，所述第一隔板垂直设置在所述生物反应空间中，所述第一隔板的顶部与所述第二壳体之间、或者所述第一隔板的底部与所述第二壳体之间均预留有第二水流通道，所述第二壳体、所述第一隔板以及所述隔板之间，限定出依次排列的升流区以及降流区。
  9. 根据权利要求8所述的污水处理系统，所述升流区的体积小于所述降流区的体积。
  10. 根据权利要求8所述的污水处理系统，所述生物反应空间中具有多个平行排列的所述第一隔板。
  11. 根据权利要求8所述的污水处理系统，所述生物膜组合处理单元进一步包括：
    多个所述第二曝气口，所述第二曝气口位于所述升流区以及所述降流区至少之一的底部。
  12. 根据权利要求8所述的污水处理系统，所述生物膜组合处理单元进一步包括：
    多个辅助第一进水口，多个所述辅助第一进水口设置在所述生物反应空间的顶部且位于所述降流区中。
  13. 根据权利要求8所述的污水处理系统，所述第一隔板与所述第二壳体之间的第二水流通道被设置为可关闭。
  14. 根据权利要求8所述的污水处理系统，所述生物膜组合处理单元进一步包括：
    回流出水口，所述回流出水口设置在靠近所述膜过滤空间的所述降流区的底部；以及
    回流进水口，所述回流进水口设置在靠近所述第二进水口的所述升流区的底部，且所述回流出水口以及所述回流进水口之间通过水流管路相连。
  15. 根据权利要求1所述的污水处理系统，进一步包括：
    至少一个臭氧填充柱，所述臭氧填充柱的进水端与所述进水箱相连，所述臭氧填充柱的出水端分别与所述臭氧流化床处理单元以及所述生物膜组合处理单元相连。
  16. 一种利用权利要求1-15任一项所述的污水处理系统进行污水处理的方法，包括：利用所述臭氧流化床处理单元以及所述生物膜组合单元，对所述污水进行臭氧流化床催化氧化处理以及生物膜组合降解处理的至少之一，
    其中，所述臭氧流化床催化氧化处理包括：将污水从第一进水口供给至臭氧流化床处 理单元中，所述污水在所述第一壳体中经陶瓷膜组件进行过滤处理，并通过陶瓷膜组件与所述第一壳体的侧壁、顶面以及底面之间的第一水流通道形成环流，由第一出水口流出所述臭氧流化床处理单元；
    所述生物膜组合降解处理包括：将所述污水由所述第二进水口供给至生物膜组合处理单元中，并利用第二曝气口对所述生物反应空间进行曝气，生物载体填料中的微生物在生物反应空间与所述污水发生反应，并从隔板底部的第一水流通孔供给至膜过滤空间，在膜过滤曝气口曝气的条件下，从位于所述膜过滤空间顶部的第二出水口排出。
  17. 根据权利要求16所述的污水处理方法，所述臭氧流化床催化氧化处理进一步包括：
    向所述第一壳体内加入第一催化剂，从第一曝气口曝臭氧以及空气，使污水以及所述第一催化剂从所述陶瓷膜组件的底部上升，并从所述陶瓷膜组件和所述第一壳体的顶面之间的第一水流通道，流至所述陶瓷膜组件和所述第一壳体的侧壁之间的所述第一水流通道并下降，在曝气条件下上升，以便形成所述环流。
  18. 根据权利要求16所述的污水处理方法，所述生物膜组合降解处理进一步包括以下步骤的至少之一：
    打开所述隔板顶部的第二水流通孔，以便所述膜过滤空间中的污水，回流至生物反应空间；
    将进水箱中的污水由多个辅助第一进水口中的一个，供给至降流区中，并关闭沿着污水流通的方向，设置在与所述进水箱相连的所述辅助第一进水口之前的第一隔板的顶部与所述第二壳体之间的第二水流通道；
    打开回流出水口，将经过靠近所述膜过滤空间的降流区的污水，通过所述回流进水口供给至靠近所述第一进水口的所述升流区。
  19. 根据权利要求16所述的污水处理方法，所述生物膜组合降解处理进一步包括：
    多个所述升流区以及多个所述降流区中的每一个的底部，均设置有所述第二曝气口，所述方法进一步包括：
    根据污水的来水水质，控制多个所述第二曝气口的开关，以便控制多个所述升流区以及多个所述降流区中的每一个的处理环境。
  20. 根据权利要求16所述的污水处理方法，进一步包括：
    根据污水的来水水质，将进水箱中的污水，供给至臭氧填充柱中；或
    将进水箱中的污水，供给至所述臭氧催化氧化单元中。
PCT/CN2018/114153 2017-12-29 2018-11-06 深度污水处理系统以及污水处理方法 WO2019128474A1 (zh)

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CN201538729U (zh) * 2009-06-17 2010-08-04 北京中联动力技术有限责任公司 难降解废水回用装置
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