CN111410386A - O-M-A/A nitrogen and phosphorus removal device and method based on MBR-MD coupling membrane - Google Patents

O-M-A/A nitrogen and phosphorus removal device and method based on MBR-MD coupling membrane Download PDF

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CN111410386A
CN111410386A CN202010424966.3A CN202010424966A CN111410386A CN 111410386 A CN111410386 A CN 111410386A CN 202010424966 A CN202010424966 A CN 202010424966A CN 111410386 A CN111410386 A CN 111410386A
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membrane
anaerobic
mbr
nitrogen
anoxic
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赖信可
赖志鹏
卢凤华
张远斌
李俊贤
庄烨
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Fujian Longking Co Ltd.
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Fujian Longking Co Ltd.
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/14—Maintenance of water treatment installations
    • 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

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

The invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane. The aerobic tank is arranged in front, the aerobic microorganisms convert ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen, and then the nitrate nitrogen and the nitrite nitrogen flow into the anaerobic/anoxic zone, and the nitrate nitrogen and the nitrite nitrogen are converted into nitrogen through denitrification reaction, so that reflux denitrification is not needed, reflux equipment is saved, and the energy consumption of a system is reduced; the invention applies the principle of denitrifying phosphorus accumulation to place the deoxygenation membrane with small diameter in the filtration membrane with large diameter, compared with the only interception and filtration functions of the traditional MBR membrane group device, the coupled membrane group device has the functions of intercepting sludge, filtering produced water, deoxidizing nitrified liquid, purging membrane, aerating, recycling and the like. Meanwhile, due to the multi-membrane nesting design of the coupling membrane combiner, the anti-pollution capacity and tensile strength of the coupling membrane filaments are enhanced, so that compared with the traditional MBR (membrane bioreactor) membrane, the coupling membrane filament only needs less blowing gas amount and is not easy to break.

Description

O-M-A/A nitrogen and phosphorus removal device and method based on MBR-MD coupling membrane
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an O-M-A/A nitrogen and phosphorus removal device and method based on an MBR-MD coupling membrane.
Background
In recent decades, with the wide application of chemical fertilizers, pesticides, detergents and the like, nitrogen and phosphorus pollution and water eutrophication become more and more serious, and China also puts forward higher and stricter standards and requirements on nitrogen and phosphorus emission. With the continuous improvement of national requirements on sewage discharge, particularly the stricter and stricter discharge standards of nitrogen and phosphorus, the combination of the traditional biochemical process and the MBR process is a research hotspot of the sewage treatment process in recent years in order to achieve lower effluent requirements.
The MBR process utilizes the membrane interception characteristic to replace a secondary sedimentation tank to realize sludge water filtration, so that a biochemical system achieves higher sludge concentration, the volume of a biochemical reaction area is greatly reduced, and the biochemical treatment capacity is enhanced. Among various biochemical processes, the AAO process is favored because it has a simple process flow and can achieve simultaneous phosphorus and nitrogen removal. Therefore, the AAO-MBR process and the MBR process are paid more and more attention and research, but the AAO-MBR process has the defect of high energy consumption, and the energy consumption for treating water per ton is 2-3 times that of the traditional activated sludge method, which limits the popularization and application of the process.
The energy consumption of the AAO-MBR process mainly comes from the reflux of the AAO process and the membrane purge of the MBR process: in the traditional AAO process, nitrogen and phosphorus removal are respectively carried out by utilizing different strains under different reaction environments: the denitrification utilizes nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen in an aerobic environment, then utilizes denitrifying bacteria in an anoxic environment to convert the nitrate nitrogen into nitrogen, and the dephosphorization utilizes phosphorus accumulating bacteria to release phosphorus in an anaerobic environment and then absorb phosphorus in an aerobic environment. Because the carbon source in the inlet water is limited, and the denitrifying bacteria and the phosphorus accumulating bacteria are heterotrophic bacteria, in order to ensure that the carbon source required by the denitrifying bacteria and the phosphorus accumulating bacteria is ingested, an anaerobic pool and an anoxic pool are usually arranged in front in the traditional AAO process, the carbon source is preferentially obtained, then the nitrifying liquid flows back to the anoxic pool from the aerobic pool by utilizing the backflow, and the phosphorus accumulating bacteria flows back to the anaerobic pool from the aerobic pool. Therefore, more carbon source and larger reflux are needed to achieve better denitrification and dephosphorization effects. However, domestic sewage in China has the characteristics of low carbon-nitrogen ratio and low carbon-phosphorus ratio and the like, and the requirements of denitrifying bacteria and phosphorus accumulating bacteria on carbon sources are difficult to meet simultaneously, so that competition of the denitrifying bacteria and the phosphorus accumulating bacteria is caused, and in order to ensure the nitrogen and phosphorus removal effect of a system, the carbon sources are required to be artificially supplemented in many municipal projects. In the MBR process, as the membrane is adopted to suck and filter effluent, under the interception effect of the membrane, the sludge concentration in a biological reaction zone can reach 2-3 times of that of the traditional activated sludge method, in order to slow down membrane pollution blockage, the most mainstream mode at present is to wash membrane filaments by a large amount of aeration at the bottom of a membrane module through a perforated pipe so as to shake the membrane filaments, the gas-water ratio is about 15: 1-20: 1, the aeration amount required by membrane sweeping aeration alone is far higher than that of the activated sludge method, and the aeration energy consumption is increased. However, the oxygen transfer efficiency of large bubble aeration is low, and the aeration range is mainly concentrated near the membrane group device, so a large amount of aeration used for membrane sweeping only plays a role in flushing and shaking, a large amount of oxygen can only be wasted, and a micropore aeration device is required to be additionally arranged in the aerobic tank to supply oxygen for aerobic microorganisms.
Therefore, how to solve the problem of high energy consumption is a worthy direction.
Disclosure of Invention
In view of the above, the technical problem to be solved by the present invention is to provide an O-M-a/a nitrogen and phosphorus removal method based on an MBR-MD coupled membrane, which has low energy consumption and good nitrogen and phosphorus removal effect.
The invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane, which comprises:
a water inlet device;
the inlet of the superfine grating is connected with the outlet of the water inlet device;
the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank;
the microporous aeration disc is arranged at the bottom of the aerobic tank;
an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank;
the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump;
the switching type anaerobic/anoxic tank is provided with a suspended filler;
the MBR-MD coupling membrane comprises:
the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump.
Preferably, the deoxygenation membrane is an organic membrane or an inorganic membrane; the deoxygenation membrane is a hollow fiber membrane or a flat membrane; the pore size of the deoxygenation membrane is preferably 0.01-0.03 mu m, and the pore size of the MBR membrane is preferably 0.03-0.4 mu m; the membrane blowing aeration device is a perforated pipe.
The deoxidation mode adopted by the deoxidation membrane is as follows: gas purging, negative pressure suction, or a combination of gas purging and negative pressure suction.
Preferably, in the MBR-MD coupled membrane: the membrane sweeping aeration device leads the membrane wire to shake and wash the surface of the membrane wire through aeration of the gas collecting pipe; the aperture of the perforated pipe is preferably 3-8 mm
Preferably, the suspension filler is a spherical suspension filler, and the specification of the ultrafine grating is particularly preferably 1-5 mm, and the aperture of the microporous aeration disc is preferably 0.22-100 μm.
Preferably, the inner diameter size range of the membrane filaments of the deoxidation membrane in the MBR-MD coupling membrane is 0.1-0.3 mm, and the outer diameter size range is 0.2-0.4 mm; the inner diameter size range of the MBR membrane filaments is 0.8-1.1 mm, and the outer diameter size range is 0.9-1.2 mm.
The invention provides an O-M-A/A nitrogen and phosphorus removal method based on an MBR-MD coupling membrane, which comprises the following steps:
sewage is filtered by a superfine grating and then flows into an aerobic tank and a switching type anaerobic/anoxic tank respectively according to a proportion;
part of sewage is subjected to nitration reaction under the action of aerobic nitrifying bacteria in an aerobic tank to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and digestion liquid flows into an MBR-MD coupling membrane;
the nitrified liquid enters the inner layer after being filtered by the outer MBR membrane, gas molecules are pumped to a microporous aeration disc of the aerobic tank under the action of the inner deoxygenation membrane, and the nitrified liquid after deoxygenation is pumped into the anaerobic/anoxic tank;
the other part of sewage enters an anaerobic/anoxic tank to provide carbon source and phosphorus for denitrifying phosphorus accumulating bacteria, and the denitrifying phosphorus accumulating bacteria absorb the carbon source under anaerobic condition to complete phosphorus release and obtain energy at the same time; and (3) introducing a deoxygenation and nitrification solution, and reducing nitrate nitrogen/nitrite nitrogen into nitrogen while absorbing phosphorus by using the energy obtained under the anaerobic condition by denitrifying phosphorus accumulating bacteria under the anoxic condition by taking nitrate nitrogen/nitrite nitrogen as an electron acceptor so as to realize synchronous nitrogen and phosphorus removal.
Preferably, the switching anaerobic/anoxic tank controls and realizes the switching between anaerobic and anoxic environments by the inflow time of the nitrified liquid after deoxidation: the anaerobic/anoxic zone is not provided with an aeration device, the reaction tank has no molecular oxygen or combined oxygen before the deoxidized nitrified liquid flows in, and is an anaerobic environment, and the reaction tank becomes an anoxic environment along with the entry of the combined oxygen after the deoxidized nitrified liquid flows in.
Preferably, the microporous aeration disc for pumping the gas molecules into the aerobic tank is specifically as follows: gas molecules are pumped out/swept and collected to the gas collecting pipe by a degassing vacuum pump under the action of negative pressure/partial pressure, and then pumped to a microporous aeration disc of the aerobic tank;
the method for pumping the deoxygenated nitrified liquid into the anaerobic/anoxic tank specifically comprises the following steps: the deoxidized nitrified liquid is pumped into an anaerobic/anoxic tank by a water producing vacuum pump.
Preferably, the hydraulic retention time of the aerobic tank is 6-10 h; the hydraulic retention time of the other part of sewage entering the anaerobic/anoxic tank is 2-4 h; the hydraulic retention time of the deoxygenated and nitrified liquid after entering the anaerobic/anoxic tank is 3-6 h;
after the sewage is subjected to nitrogen and phosphorus removal treatment, supernatant is overflowed and discharged from the anaerobic/anoxic zone.
Preferably, an extremely low oxygen negative pressure is formed inside the deoxidation membrane under the combined action of air inlet of the air blower and suction of the deaeration vacuum pump, and oxygen molecules in the sewage are pressed into the deoxidation membrane under the action of a high oxygen partial pressure to complete the deoxidation process.
Compared with the prior art, the invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane, which comprises: a water inlet device; the inlet of the superfine grating is connected with the outlet of the water inlet device; the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank; the microporous aeration disc is arranged at the bottom of the aerobic tank; an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank; the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump; the switching type anaerobic/anoxic tank is provided with a suspended filler; the MBR-MD coupling membrane comprises: the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump. The aerobic tank is arranged in front, the aerobic microorganisms convert ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen, and then the nitrate nitrogen and the nitrite nitrogen flow into the anaerobic/anoxic zone, and the nitrate nitrogen and the nitrite nitrogen are converted into nitrogen through denitrification reaction, so that reflux denitrification is not needed, reflux equipment is saved, and the energy consumption of a system is reduced; the invention applies the principle of denitrifying phosphorus accumulation, the reaction principle can realize synchronous nitrogen and phosphorus removal and simultaneously maximally utilize the influent carbon source, the deoxygenation membrane with small diameter is arranged in the filtration membrane with large diameter, compared with the only interception and filtration functions of the traditional MBR membrane group device, the coupling membrane group device has the functions of intercepting sludge, producing water filtration, nitrifying liquid deoxygenation, membrane purging aeration recycling and the like. Meanwhile, due to the multi-membrane nesting design of the coupling membrane combiner, the anti-pollution capacity and tensile strength of the coupling membrane filaments are enhanced, so that compared with the traditional MBR (membrane bioreactor) membrane, the coupling membrane filament only needs less blowing gas amount and is not easy to break.
Drawings
FIG. 1 is a flow chart of an O-M-A/A nitrogen and phosphorus removal process based on an MBR-MD coupling membrane;
FIG. 2 is a schematic diagram of an O-M-A/A denitrification and dephosphorization apparatus based on MBR-MD coupling membrane according to the present invention;
FIG. 3 is a schematic view of an MBR-MD coupled membrane of the present invention.
Detailed Description
The invention provides an O-M-A/A nitrogen and phosphorus removal device and method based on an MBR-MD coupling membrane, and a person skilled in the art can appropriately improve process parameters for realization by referring to the content. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the scope of the invention. While the methods and applications of this invention have been described in terms of preferred embodiments, it will be apparent to those of ordinary skill in the art that variations and modifications in the methods and applications described herein, as well as other suitable variations and combinations, may be made to implement and use the techniques of this invention without departing from the spirit and scope of the invention.
The invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane, which comprises:
a water inlet device;
the inlet of the superfine grating is connected with the outlet of the water inlet device;
the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank;
the microporous aeration disc is arranged at the bottom of the aerobic tank;
an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank;
the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump;
the switching type anaerobic/anoxic tank is provided with a suspended filler;
the MBR-MD coupling membrane comprises:
the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump.
The invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane, which comprises a water inlet device.
The water inlet device is not limited, and only needs to be an inlet channel of sewage.
The O-M-A/A nitrogen and phosphorus removal device based on the MBR-MD coupling membrane comprises an ultrafine grid with an inlet connected with an outlet of the water inlet device.
The specification of the superfine grating is 1-5 mm.
The superfine grating has a filtering function, and sewage filtered by the superfine grating flows into the aerobic zone and the anaerobic/anoxic zone respectively according to a proper proportion.
The outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank.
The ratio of sewage flowing into the aerobic tank and the switching type anaerobic/anoxic tank is preferably 7: 1-1: 1.
The O-M-A/A nitrogen and phosphorus removal device based on the MBR-MD coupling membrane comprises a microporous aeration disc arranged at the bottom of the aerobic tank.
The preferable aperture of the microporous aeration disc is 0.22-100 mu m.
The aerobic pool is an aerobic zone, the bottom of the aerobic zone is provided with a microporous aeration disc for oxygen supply, and sewage flowing into the aerobic zone is subjected to nitration reaction under the action of aerobic nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen.
The O-M-A/A nitrogen and phosphorus removal device based on the MBR-MD coupling membrane comprises an MBR-MD coupling membrane with an inlet connected with an outlet of the aerobic tank.
The MBR-MD coupling membrane comprises:
the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump.
Specifically, the MBR-MD coupling membrane comprises a coupling membrane combiner.
The MBR-MD coupling membrane comprises a gas collecting pipe arranged at the lower part of the coupling membrane group device; and the water collecting pipe is arranged at the upper part of the coupling membrane group device. The specification of the gas collecting pipe and the water collecting pipe is not limited, and the length of the gas collecting pipe and the water collecting pipe is preferably consistent with the width of the coupling film.
The coupling membrane group device comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane.
The coupling membrane group device is the core of the coupling membrane system, and the double-layer composite membrane is formed by placing a deoxygenation membrane with a smaller diameter inside an MBR membrane with a larger diameter.
Wherein the inner diameter of the deoxygenation membrane filaments in the MBR-MD coupling membrane ranges from 0.1mm to 0.3mm, and can be 0.1mm, 0.2mm, 0.3mm or the value between any two of the above; the outer diameter size range is 0.2-0.4 mm; may be 0.2mm, 0.3mm, 0.4mm, or a point value between any of the foregoing; the inner diameter of the MBR membrane filaments can be 0.8-1.1 mm, and can be 0.8mm, 0.9mm, 1.0mm, 1.1mm or the point value between any two of the above; the outer diameter size range is 0.9-1.2 mm, and can be 0.9mm, 1.0mm, 1.1mm, 1.2mm or the point value between any two of the above.
The sewage enters an MBR membrane inner layer after being filtered by an MBR membrane, the filtered sewage is contacted with an MD deoxidizing membrane in the MBR membrane inner layer, gas molecules in the sewage are pumped out/swept and collected to a bottom gas collecting pipe by a degassing vacuum pump under the action of negative pressure/partial pressure, the gas collecting pipe is connected with a microporous aeration disc of an aerobic zone, and the deoxidized sewage is pumped into an anaerobic/anoxic zone by a water producing vacuum pump.
The double-layer composite membrane has four main functions of sludge-water separation, nitration liquid deoxidation, membrane cleaning effect reinforcement, membrane blowing aeration recycling and the like.
Wherein, the effect of outer MBR membrane: (1) intercepting sludge, and keeping nitrifying bacteria in an aerobic zone; (2) pretreating the deoxidation film to prevent suspended particles from blocking the deoxidation film; (3) the sweeping aeration of the MBR membrane supplies oxygen to the microorganisms in the aerobic zone in the intermittent period of the microporous aeration device in the aerobic zone.
The inner layer deoxidized film has the following functions: (1) dissolved oxygen in the nitrified liquid is removed, and the nitrified liquid is prevented from entering an anaerobic/anoxic zone to destroy the original anaerobic/anoxic environment; (2) delivering the separated oxygen-enriched air to an aerobic zone microporous aeration device to supply oxygen for aerobic microorganisms; (3) the outer MBR membrane is driven to shake by using the shake formed by blowing and sucking during deoxidation, the blown air recoils out of the membrane from the inside of the MBR membrane during deoxidation, the membrane shaking and the air recoiling are beneficial to relieving membrane pollution, and the membrane blowing aeration can be reduced, so that the aeration energy consumption is reduced; (4) the inner layer deoxidation film is equivalent to adding a lining to the outer layer filtering film, so that the tensile strength of the film yarn is enhanced, and the phenomenon of yarn breakage can be effectively avoided.
According to the membrane assembly device, membrane assemblies with different functions are not simply superposed and combined, membrane filaments with smaller diameters are placed inside membrane filaments with larger diameters according to the diameters of the membranes, and the combination sequence of different membranes is selected according to the functions of the membranes. Compared with the traditional membrane combiner stacking and coupling mode, the coupling membrane combiner in the multilayer membrane nesting mode is smaller in size. The invention couples the deoxidation membrane with the filtering membrane, the deoxidation membrane with smaller diameter is arranged in the filtering membrane, the deoxidation membrane can be in the form of a hollow fiber membrane and a flat membrane, and can adopt three deoxidation modes of gas blowing, negative pressure suction, combination of the gas blowing and the negative pressure suction, etc., the filtering membrane can be in the form of a hollow fiber membrane and a flat membrane, etc., and negative pressure suction is adopted for filtering. The outer layer filtering membrane filters suspended particles, the inner layer deoxidation membrane has a pretreatment effect, pollution and blockage of the deoxidation membrane are avoided, the inner layer deoxidation membrane drives the outer layer filtering membrane to shake in the deoxidation process and performs gas backwashing, and the pollution speed of the outer layer membrane is reduced.
The deoxygenation membrane is an organic membrane or an inorganic membrane; the deoxygenation membrane is a hollow fiber membrane or a flat membrane; the preferred aperture of the deoxygenation membrane is 0.01-0.03 mu m; may be 0.01 μm, 0.02 μm or 0.03 μm; . The preferable aperture of the MBR membrane is 0.03-0.4 μm; preferably 0.05 to 0.35 μm.
The deoxidation mode adopted by the deoxidation membrane provided by the invention is as follows: gas purging, negative pressure suction, or a combination of gas purging and negative pressure suction. The air-entrapping stripping is mainly carried out by blowing nitrogen or compressed air, so that the partial pressure of oxygen measured in the film is reduced, the gas in a liquid phase is transferred from the liquid phase to a gas phase, and the air-entrapping pressure is generally controlled below 0.7 kPa; the vacuum pumping mode is to create a partial pressure gradient between the liquid and gas phases. The vacuum causes dissolved oxygen to diffuse from the liquid interior to the vacuum side, where it is drawn in by the vacuum pump and discharged. The removal efficiency is directly influenced by the vacuum degree, the larger the vacuum degree is, the lower the gas content of the outlet liquid is, and the vacuum degree is controlled to be 150mbar-50mbar in the general use process. The vacuum suction assisted air entrainment and air stripping combines the two modes, and can be adjusted according to actual use conditions.
The design processing capacity of the deoxygenation membrane adopted by the invention is 20L/m2/h～120L/m2The designed treatment capacity of the filter membrane is 15L/m2/h～30L/m2H; therefore, in order to utilize the treatment capacities of the deoxygenation membrane and the filtering membrane to the maximum extent, the common filtering membrane can be selected for the membrane filaments arranged close to the outer side, and the MBR-MD coupling membrane can be selected for the membrane filaments arranged at the inner side.
The MBR-MD coupling membrane comprises a membrane purging aeration device arranged at the lower part of the gas collecting pipe; the membrane blowing aeration device is a perforated pipe. The preferable length of the perforated pipe is consistent with the width of the coupling membrane combiner, and the preferable aperture of the perforated pipe is 3-8 mm.
The MBR-MD coupling membrane comprises a blower for blowing the coupling membrane assembly.
The present invention is not limited to the type and specification of the blower, and those skilled in the art will appreciate that the blower is not limited to the above type and specification.
The MBR-MD coupling membrane comprises a water production vacuum pump connected with the water collecting pipe; the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through a degassing vacuum pump.
In the MBR-MD coupling membrane: the membrane sweeping aeration device leads the membrane wire to shake and wash the surface of the membrane wire through the aeration of the gas collecting pipe. A large amount of oxygen enters the wastewater during this process.
Sewage enters the inner layer after being filtered by the outer-layer MBR membrane, flows upwards under the suction of the water-producing vacuum pump, and is collected to the water collecting pipe, the sewage flows through the inner-layer deoxygenation membrane, extremely low oxygen negative pressure is formed inside the deoxygenation membrane under the combined action of air inlet of the air blower and suction of the degassing vacuum pump inside the deoxygenation membrane, oxygen molecules in the sewage are pressed into the interior of the deoxygenation membrane under the action of high oxygen partial pressure, the sewage deoxygenation process is completed, and the collected oxygen-enriched air flows downwards to the gas collecting pipe. The deoxygenation and nitration liquid in the water collecting pipe is pumped into the anaerobic/anoxic zone by a water producing vacuum pump, and the oxygen-enriched air in the gas collecting pipe is pumped into the microporous aeration device by a degassing vacuum pump.
The MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump. The switching type anaerobic/anoxic tank is provided with a suspended filler.
The suspended filler of the present invention is particularly preferably a spherical suspended filler.
The sewage entering the anaerobic/anoxic zone provides a carbon source for denitrifying phosphorus-accumulating bacteria, as the anaerobic/anoxic zone is not provided with an aeration device, phosphorus is released by the denitrifying phosphorus-accumulating bacteria under the completely anaerobic condition to obtain energy, then the denitrifying phosphorus-accumulating bacteria pumps deoxygenated nitrified liquid into the anaerobic/anoxic zone along with a vacuum pump, nitrate nitrogen/nitrite nitrogen in the nitrified liquid enables the anaerobic/anoxic zone to be changed from the anaerobic environment to the anoxic environment, the denitrifying phosphorus-accumulating bacteria uses the nitrate nitrogen/nitrite nitrogen as an electron acceptor with the carbon source flowing in of the nitrified liquid, the nitrate nitrogen/nitrite nitrogen is reduced to nitrogen while phosphorus is absorbed, and the synchronous nitrogen and phosphorus removal process is completed. After the sewage is subjected to nitrogen and phosphorus removal treatment, supernatant is overflowed and discharged from the anaerobic/anoxic zone.
The invention carries out nitration reaction in the aerobic zone, carries out denitrification dephosphorization in the anaerobic/anoxic zone, supplements carbon source required by the processes of phosphorus release and denitrification phosphorus accumulation by water inflow and diversion, realizes nitrogen and phosphorus removal under the condition of no reflux, and saves energy consumption required by reflux. Based on the principle of denitrifying phosphorus accumulation, nitrate nitrogen and nitrite nitrogen are injected under anaerobic conditions, and suspended fillers are added into the reaction tank, so that denitrifying phosphorus accumulation bacteria can be enriched conveniently, denitrifying phosphorus accumulation bacteria can realize denitrification while accumulating phosphorus, one carbon and two purposes are realized, a carbon source is greatly saved, and the condition that the carbon source is influenced by competition of the phosphorus accumulation bacteria and denitrifying bacteria in the anaerobic environment in the traditional AAO process is avoided.
FIG. 1 is a flow chart of an O-M-A/A nitrogen and phosphorus removal process based on an MBR-MD coupling membrane;
FIG. 2 is a schematic diagram of an O-M-A/A denitrification and dephosphorization apparatus based on MBR-MD coupling membrane according to the present invention;
FIG. 3 is a schematic view of an MBR-MD coupled membrane of the present invention.
Wherein, 1 is a water inlet device, 2 is a superfine grid, 3 is an aerobic tank, 4 is a switching anaerobic/anoxic tank, and 5 is a microporous aeration disc; 6 is a degassing vacuum pump; 7 is a membrane purging aeration device (perforated pipe); 8 is MBR-MD coupling membrane; 9 is a blower; 10 is a water producing vacuum pump, 11 is a suspension filler, 12 is a water collecting pipe, 13 is a degassing pipe, 14 is a deoxygenation membrane, and 15 is an MBR membrane.
The invention provides an O-M-A/A nitrogen and phosphorus removal method based on an MBR-MD coupling membrane, which comprises the following steps:
sewage is filtered by a superfine grating and then flows into an aerobic tank and a switching type anaerobic/anoxic tank respectively according to a proportion;
part of sewage is subjected to nitration reaction under the action of aerobic nitrifying bacteria in an aerobic tank to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and digestion liquid flows into an MBR-MD coupling membrane;
the nitrified liquid enters the inner layer after being filtered by the outer MBR membrane, gas molecules are pumped to a microporous aeration disc of the aerobic tank under the action of the inner deoxygenation membrane, and the nitrified liquid after deoxygenation is pumped into the anaerobic/anoxic tank;
the other part of sewage enters an anaerobic/anoxic tank to provide carbon source and phosphorus for denitrifying phosphorus accumulating bacteria, and the denitrifying phosphorus accumulating bacteria absorb the carbon source under anaerobic condition to complete phosphorus release and obtain energy at the same time; and (3) introducing a deoxygenation and nitrification solution, and reducing nitrate nitrogen/nitrite nitrogen into nitrogen while absorbing phosphorus by using the energy obtained under the anaerobic condition by denitrifying phosphorus accumulating bacteria under the anoxic condition by taking nitrate nitrogen/nitrite nitrogen as an electron acceptor so as to realize synchronous nitrogen and phosphorus removal.
The invention discloses an O-M-A/A nitrogen and phosphorus removal method based on an MBR-MD coupling membrane, which is characterized in that sewage is filtered by an ultrafine grid and then flows into an aerobic tank and a switching type anaerobic/anoxic tank respectively in proportion.
The sewage is filtered by the superfine grating and then flows into the aerobic zone and the anaerobic/anoxic zone respectively according to a proper proportion. The proportion is preferably 4: 1-1: 1.
Part of the sewage is subjected to nitration reaction under the action of aerobic nitrifying bacteria in the aerobic tank to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the digestion liquid flows into the MBR-MD coupling membrane.
The bottom of the aerobic zone is provided with a microporous aeration disc for oxygen supply, and the sewage flowing into the aerobic zone is subjected to nitration reaction under the action of aerobic nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen.
The nitrified liquid is filtered by the MBR membrane on the outer layer and then enters the inner layer, gas molecules are pumped to the microporous aeration disc of the aerobic tank under the action of the deoxygenation membrane on the inner layer, and the nitrified liquid after deoxygenation is pumped into the anaerobic/anoxic tank.
The preferable concrete is as follows: nitrifying liquid enters an MBR (membrane bioreactor) membrane inner layer after being filtered by an MBR membrane, filtered sewage is contacted with an MD (methyl methacrylate) deoxidation membrane in the MBR membrane inner layer, gas molecules in the sewage are pumped out/swept by a degassing vacuum pump under the action of negative pressure/partial pressure and collected to a bottom gas collecting pipe, and the gas collecting pipe is connected with a microporous aeration disc of an aerobic zone.
Sewage enters an MBR membrane inner layer after being filtered by an MBR membrane, the filtered sewage is contacted with an MD deoxidizing membrane in the MBR membrane inner layer, gas molecules in the sewage are pumped out/swept by a degassing vacuum pump under the action of negative pressure/partial pressure and collected to a gas collecting pipe at the bottom, the gas collecting pipe is connected with a microporous aeration disc of an aerobic zone, and the deoxidized sewage is pumped into an anaerobic/anoxic zone by a water producing vacuum pump.
The coupling membrane group device is the core of the coupling membrane system, and a deoxygenation membrane with a smaller diameter is arranged inside an MBR membrane with a larger diameter to form a double-layer composite membrane. The air blower supplies air to the membrane blowing device of the coupling membrane group device, the membrane blowing device enables membrane filaments to shake and wash the surfaces of the membrane filaments through aeration of the perforated pipes, and a large amount of oxygen enters sewage in the process. Sewage enters the inner layer after being filtered by the outer-layer MBR membrane, flows upwards under the suction of the water-producing vacuum pump, and is collected to the water collecting pipe, the sewage flows through the inner-layer deoxygenation membrane, extremely low oxygen negative pressure is formed inside the deoxygenation membrane under the combined action of air inlet of the air blower and suction of the degassing vacuum pump inside the deoxygenation membrane, oxygen molecules in the sewage are pressed into the interior of the deoxygenation membrane under the action of high oxygen partial pressure, the sewage deoxygenation process is completed, and the collected oxygen-enriched air flows downwards to the gas collecting pipe. The deoxygenation and nitration liquid in the water collecting pipe is pumped into the anaerobic/anoxic zone by a water producing vacuum pump, and the oxygen-enriched air in the gas collecting pipe is pumped into the microporous aeration device by a degassing vacuum pump.
The other part of sewage enters an anaerobic/anoxic tank to provide carbon source and phosphorus for denitrifying phosphorus accumulating bacteria, and the denitrifying phosphorus accumulating bacteria absorb the carbon source under anaerobic condition to complete phosphorus release and obtain energy at the same time; and (3) introducing a deoxygenation and nitrification solution, and reducing nitrate nitrogen/nitrite nitrogen into nitrogen while absorbing phosphorus by using the energy obtained under the anaerobic condition by denitrifying phosphorus accumulating bacteria under the anoxic condition by taking nitrate nitrogen/nitrite nitrogen as an electron acceptor so as to realize synchronous nitrogen and phosphorus removal.
The switching type anaerobic/anoxic tank provided by the invention specifically realizes the switching of anaerobic and anoxic environments by controlling the inflow time of the nitrified liquid after deoxidation: the anaerobic/anoxic zone is not provided with an aeration device, the reaction tank has no molecular oxygen or combined oxygen before the deoxidized nitrified liquid flows in, and is an anaerobic environment, and the reaction tank becomes an anoxic environment along with the entry of the combined oxygen after the deoxidized nitrified liquid flows in.
The anaerobic/anoxic zone non-aeration device is characterized in that the reaction tank has no molecular oxygen or combined oxygen before nitrifying liquid flows in, and is an anaerobic environment, and after the nitrifying liquid flows in, the reaction tank becomes an anoxic environment along with the entry of the combined oxygen (nitrate nitrogen and nitrite nitrogen). The beneficial effects are as follows: (1) the anoxic/anaerobic zone does not need to switch the environment by aeration like the traditional SBR process, so that the aeration energy consumption is saved, and the environment completely without molecular oxygen can avoid the competition of carbon sources by aerobic heterotrophic bacteria, thereby being beneficial to the enrichment of denitrifying phosphorus accumulating bacteria; (2) the anaerobic reaction process and the anoxic reaction process are completely separated by utilizing water inflow distribution, and the enrichment of denitrifying phosphorus accumulating bacteria is facilitated: and the anaerobic/anoxic zone enters water in two stages, wherein one stage is that water is shunted by the system to provide phosphorus and a carbon source for phosphorus release of the denitrifying phosphorus-accumulating bacteria in an anaerobic environment, and the other stage is that nitrifying liquid enters water to provide nitrate nitrogen/nitrite nitrogen and a carbon source for phosphorus accumulation of the denitrifying phosphorus-accumulating bacteria in an anoxic environment. In the first stage, the reaction tank does not contain nitrate nitrogen or nitrite nitrogen, so that denitrifying bacteria cannot compete with denitrifying phosphorus-accumulating bacteria for a carbon source in the first stage, and the denitrifying phosphorus-accumulating bacteria occupy a dominant position.
The sequencing batch anaerobic/anoxic zone changes the anaerobic and anoxic environment of the reaction tank through the inflow of the nitrifying liquid, and the design is favorable for the enrichment of denitrifying phosphorus accumulating bacteria and simultaneously saves the energy consumption required by aeration. In addition, suspended fillers are added in the anaerobic/anoxic zone, so that denitrifying phosphorus-accumulating bacteria are enriched on the fillers, the status of the denitrifying phosphorus-accumulating bacteria as flora is enhanced, the concentration of suspended sludge in the tank can be reduced, and the supernatant can overflow to produce water conveniently.
The method for pumping the deoxidized nitrified liquid into the anaerobic/anoxic tank specifically comprises the following steps: the deoxidized nitrified liquid is pumped into an anaerobic/anoxic tank by a water producing vacuum pump.
The sewage entering the anaerobic/anoxic zone provides a carbon source for denitrifying phosphorus-accumulating bacteria, as the anaerobic/anoxic zone is not provided with an aeration device, phosphorus is released by the denitrifying phosphorus-accumulating bacteria under the completely anaerobic condition to obtain energy, then the denitrifying phosphorus-accumulating bacteria pumps deoxygenated nitrified liquid into the anaerobic/anoxic zone along with a vacuum pump, nitrate nitrogen/nitrite nitrogen in the nitrified liquid enables the anaerobic/anoxic zone to be changed from the anaerobic environment to the anoxic environment, the denitrifying phosphorus-accumulating bacteria uses the nitrate nitrogen/nitrite nitrogen as an electron acceptor with the carbon source flowing in of the nitrified liquid, the nitrate nitrogen/nitrite nitrogen is reduced to nitrogen while phosphorus is absorbed, and the synchronous nitrogen and phosphorus removal process is completed. After the sewage is subjected to nitrogen and phosphorus removal treatment, supernatant is overflowed and discharged from the anaerobic/anoxic zone.
Wherein the hydraulic retention time of the aerobic tank is 6-10 h; the hydraulic retention time of the other part of sewage entering the anaerobic/anoxic tank is 2-4 h; the hydraulic retention time of the deoxygenated and nitrified liquid after entering the anaerobic/anoxic tank is 3-6 h;
the invention provides an O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane, which comprises: a water inlet device; the inlet of the superfine grating is connected with the outlet of the water inlet device; the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank; the microporous aeration disc is arranged at the bottom of the aerobic tank; an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank; the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump; the switching type anaerobic/anoxic tank is provided with a suspended filler; the MBR-MD coupling membrane comprises: the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump. The aerobic tank is arranged in front, the aerobic microorganisms convert ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen, and then the nitrate nitrogen and the nitrite nitrogen flow into the anaerobic/anoxic zone, and the nitrate nitrogen and the nitrite nitrogen are converted into nitrogen through denitrification reaction, so that reflux denitrification is not needed, reflux equipment is saved, and the energy consumption of a system is reduced; the invention applies the principle of denitrifying phosphorus accumulation, the reaction principle can realize synchronous nitrogen and phosphorus removal and simultaneously maximally utilize the influent carbon source, the deoxygenation membrane with small diameter is arranged in the filtration membrane with large diameter, compared with the only interception and filtration functions of the traditional MBR membrane group device, the coupling membrane group device has the functions of intercepting sludge, producing water filtration, nitrifying liquid deoxygenation, membrane purging aeration recycling and the like. Meanwhile, due to the multi-membrane nesting design of the coupling membrane combiner, the anti-pollution capacity and tensile strength of the coupling membrane filaments are enhanced, so that compared with the traditional MBR (membrane bioreactor) membrane, the coupling membrane filament only needs less blowing gas amount and is not easy to break.
In order to further illustrate the invention, the following will describe in detail an O-M-a/a denitrification and dephosphorization apparatus and method based on MBR-MD coupled membrane according to the present invention with reference to the following examples.
Example 1
MBR-MD coupling membrane based O-M-A/A nitrogen and phosphorus removal device includes: a water inlet device; the inlet of the superfine grating is connected with the outlet of the water inlet device and is 3 mm; the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank; a 50-micron microporous aeration disc arranged at the bottom of the aerobic tank; an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank; the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump; the switching type anaerobic/anoxic tank is provided with a suspended filler; the MBR-MD coupling membrane comprises: the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR (membrane bioreactor) membrane (the inner diameter of the adopted MBR membrane wire is 0.8mm, and the outer diameter is 0.9mm) and a deoxygenation membrane (the inner diameter of the adopted deoxygenation membrane wire is 0.15mm, and the outer diameter is 0.25mm) arranged inside the MBR membrane; the membrane blowing aeration device (adopting a perforated aeration pipe with the aperture of 5mm) arranged at the lower part of the coupling membrane group device, an air blower used for blowing the coupling membrane group device and a water production vacuum pump connected with the gas collecting pipe, wherein the gas collecting pipe is connected with a microporous aeration disc at the bottom of the aerobic tank through a degassing vacuum pump.
Filtering sewage by using an ultrafine grid, and then mixing the following components in parts by weight: 1 respectively flows into an aerobic zone and an anaerobic/anoxic zone, and the total retention time is 7 h: in the aerobic zone, the membrane group device is perforated for aeration and oxygen supply, and the sewage flowing into the aerobic zone is subjected to nitration reaction under the action of aerobic nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen. Sewage enters an MBR membrane inner layer after being filtered by an MBR membrane, the filtered sewage is contacted with an MD deoxidizing membrane in the MBR membrane inner layer, oxygen in the sewage is pumped out/swept by a degassing vacuum pump under the action of negative pressure/partial pressure and is collected to a gas collecting pipe at the bottom, the gas collecting pipe is connected with a micropore aeration disc of an aerobic area, oxygen is supplied to the aerobic area by recovered oxygen-enriched air through the micropore aeration disc, and the sewage after being deoxidized is pumped into an anaerobic/anoxic area by a water-producing vacuum pump. The sewage enters an anaerobic/anoxic zone twice, the untreated sewage directly enters the anaerobic/anoxic zone according to a proper proportion for the first time, the hydraulic retention time of the stage is 3h, the sewage provides a carbon source for denitrifying phosphorus-accumulating bacteria, and because an aeration device is not arranged in the anaerobic/anoxic zone, the denitrifying phosphorus-accumulating bacteria release phosphorus and synthesize PHA/PHB to be stored in a body under the completely anaerobic condition. And in the second time, the sewage after nitrification and deoxidation treatment is pumped into an anaerobic/anoxic zone by a vacuum pump, the hydraulic retention time in the stage is 4 hours, nitrate nitrogen/nitrite nitrogen in nitrifying liquid changes the anaerobic/anoxic zone from an anaerobic environment to an anoxic environment, denitrifying phosphorus accumulating bacteria take the nitrate nitrogen/nitrite nitrogen as an electron acceptor, PHA/PHB stored in the body is used as energy, the nitrate nitrogen/nitrite nitrogen is reduced into nitrogen while phosphorus is absorbed, and synchronous nitrogen and phosphorus removal is completed. After a series of treatments, the supernatant is discharged from the anaerobic/anoxic zone in an overflow manner.
The test water is taken from domestic sewage of a certain municipal sewage treatment plant in Fujian, and the main water quality indexes are as follows: CODCr＝344mg/L，NH3-N-47 mg/L-51 mg/L-3.2 mg/L, the above criteria are determined according to the standard methods in water and wastewater monitoring and analysis methods (fourth edition).
The device of this embodiment is when using, and aerobic district and anaerobism/anoxic zone are squeezed into respectively to sewage through the intake pump, and the proportion of intaking is 7:1, the total hydraulic retention time of the sewage in the reactor is 7h, and the reactor is a sequencing batch reactor: in the first 3h, the aerobic nitrification bacteria in the aerobic zone are aerated by the perforated aeration pipe below the membrane group device to supply oxygen for nitrification reaction, and in the 3h, the sewage entering the anaerobic/anoxic zone provides a carbon source for the denitrifying phosphorus accumulating bacteria under the complete anaerobic condition to carry out anaerobic phosphorus release and synthesize PHA/PHB. After 3 hours, a vacuum pump of the MBR-MD coupling membrane system is started, oxygen in the oxygen-enriched sewage near the membrane group device is removed and recovered, then the oxygen-enriched sewage is pumped into a microporous aeration disc to supply oxygen to an aerobic area, the sewage after deoxygenation is pumped into an anaerobic/anoxic area by water production vacuum, and the process lasts for 4 hours. After entering the anaerobic/anoxic zone, the deoxidized and nitrified liquid brings in nitrate and nitrite, and the denitrifying phosphorus-accumulating bacteria in the anaerobic/anoxic zone perform synchronous nitrogen and phosphorus removal by taking nitrate nitrogen and nitrite nitrogen as electron acceptors and PHA/PHB stored in vivo as carbon sources (electron donors).
After 2 months of acclimatization and culture according to the implementation steps, the COD of the effluent waterCr、NH3The average concentration of-N, TN and TP is 26.7 mg/L, 1.3 mg/L, 7.9 mg/L and 0.4 mg/L respectively, and the water is finally produced by an anaerobic/anoxic zone, and the denitrification dephosphorization process is easy to control, so that the system has good removal effect on TN and TP and meets the A standard requirement of the primary standard of urban sewage discharge standard (GB 18918-2002). in addition, a special aeration oxygen supply device is omitted, the gas-water ratio of the system is 8: 1, the gas-water ratio of the system is more than half of the aeration amount compared with the gas-water ratio of 20: 1-30: 1 in the traditional MBR process, and a reflux device of the MBR is omitted, so the energy consumption (0.38kWh/t) of the system for treating water per ton is lower than that of the traditional MBR process (0.9-1.3 kWh/t).
Example 2
MBR-MD coupling membrane based O-M-A/A nitrogen and phosphorus removal device includes: a water inlet device; the inlet of the superfine grating is connected with the outlet of the water inlet device and is 1 mm; the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank; a 0.22 mu m micropore aeration disc arranged at the bottom of the aerobic tank; an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank; the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump; the switching type anaerobic/anoxic tank is provided with a suspended filler; the MBR-MD coupling membrane comprises: the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR (membrane bioreactor) membrane (the inner diameter of the adopted MBR membrane wire is 1.0mm, and the outer diameter range is 1.2mm) and a deoxygenation membrane (the inner diameter of the adopted deoxygenation membrane wire is 0.2mm, and the outer diameter range is 0.25mm) arranged inside the MBR membrane; the membrane blowing aeration device (adopting a perforated aeration pipe with the aperture of 8 mm) arranged at the lower part of the coupling membrane group device, an air blower used for blowing the coupling membrane group device and a water production vacuum pump connected with the gas collecting pipe are arranged, and the gas collecting pipe is connected with a microporous aeration disc at the bottom of the aerobic tank through a degassing vacuum pump.
Filtering sewage by using an ultrafine grid, and then performing treatment according to the following steps of 4:1 respectively flows into an aerobic zone and an anaerobic/anoxic zone, and the total retention time is 8 h: in the aerobic zone, the membrane group device is perforated for aeration and oxygen supply, and the sewage flowing into the aerobic zone is subjected to nitration reaction under the action of aerobic nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen. Sewage enters an MBR membrane inner layer after being filtered by an MBR membrane, the filtered sewage is contacted with an MD deoxidizing membrane in the MBR membrane inner layer, oxygen in the sewage is pumped out/swept by a degassing vacuum pump under the action of negative pressure/partial pressure and is collected to a gas collecting pipe at the bottom, the gas collecting pipe is connected with a micropore aeration disc of an aerobic area, oxygen is supplied to the aerobic area by recovered oxygen-enriched air through the micropore aeration disc, and the sewage after being deoxidized is pumped into an anaerobic/anoxic area by a water-producing vacuum pump. The sewage enters an anaerobic/anoxic zone twice, the untreated sewage directly enters the anaerobic/anoxic zone according to a proper proportion for the first time, the hydraulic retention time of the stage is 4 hours, the sewage provides a carbon source for denitrifying phosphorus-accumulating bacteria, and because an aeration device is not arranged in the anaerobic/anoxic zone, the denitrifying phosphorus-accumulating bacteria release phosphorus and synthesize PHA/PHB to be stored in a body under the completely anaerobic condition. And in the second time, the sewage after nitrification and deoxidation treatment is pumped into an anaerobic/anoxic zone by a vacuum pump, the hydraulic retention time in the stage is 4 hours, nitrate nitrogen/nitrite nitrogen in nitrifying liquid changes the anaerobic/anoxic zone from an anaerobic environment to an anoxic environment, denitrifying phosphorus accumulating bacteria take the nitrate nitrogen/nitrite nitrogen as an electron acceptor, PHA/PHB stored in the body is used as energy, the nitrate nitrogen/nitrite nitrogen is reduced into nitrogen while phosphorus is absorbed, and synchronous nitrogen and phosphorus removal is completed. After a series of treatments, the supernatant is discharged from the anaerobic/anoxic zone in an overflow manner.
The test water is taken from domestic sewage of a certain municipal sewage treatment plant in Fujian, and the main water quality indexes are as follows: CODCr＝289mg/L，NH3-N-51 mg/L-56 mg/L-4.5 mg/L, the above criteria are determined according to the standard methods in water and wastewater monitoring and analysis methods (fourth edition).
The device of this embodiment is when using, and aerobic district and anaerobism/anoxic zone are squeezed into respectively to sewage through the intake pump, and the proportion of intaking is 4:1, the total hydraulic retention time of the sewage in the reactor is 8h, and the reactor is a sequencing batch reactor: the aeration is carried out for the first 4h through a perforated aeration pipe below the membrane group device to supply oxygen for the aerobic nitrification bacterial nitrification reaction in the aerobic zone, and in the 4h, the sewage entering the anaerobic/anoxic zone provides a carbon source for the denitrifying phosphorus accumulating bacteria under the complete anaerobic condition to carry out anaerobic phosphorus release and synthesize PHA/PHB. After 4 hours, a vacuum pump of the MBR-MD coupling membrane system is started, oxygen in the sewage in the aerobic zone is removed and recovered, then the sewage is pumped into a microporous aeration disc to supply oxygen to the aerobic zone, the sewage after deoxygenation is pumped into an anaerobic/anoxic zone, and the process lasts for 4 hours. After entering the anaerobic/anoxic zone, the deoxidized and nitrified liquid brings in nitrate and nitrite, and the denitrifying phosphorus-accumulating bacteria in the anaerobic/anoxic zone perform synchronous nitrogen and phosphorus removal by taking nitrate nitrogen and nitrite nitrogen as electron acceptors and PHA/PHB stored in vivo as carbon sources (electron donors).
After 1 month acclimatization and culture according to the above implementation steps, effluent CODCr、NH3The average concentration of-N, TN and TP is 20.6 mg/L, 2.1 mg/L, 6.6 mg/L and 0.5 mg/L respectively, and the water is finally produced by an anaerobic/anoxic zone, and the denitrification dephosphorization process is easy to control, so that the system has good removal effect on TN and TP and meets the A standard requirement of the primary standard of urban sewage discharge standard (GB 18918-2002). in addition, a special aeration oxygen supply device is omitted, the gas-water ratio of the system is less than 9: 1, the gas-water ratio of the system is more than half of the aeration amount compared with the gas-water ratio of 20: 1-30: 1 in the traditional MBR process, and a reflux device is omitted, so the energy consumption (0.46kWh/t) of the system for water treatment per ton is lower than that of the traditional MBR process (0.9-1.3 kWh/t).
Example 3
MBR-MD coupling membrane based O-M-A/A nitrogen and phosphorus removal device includes: a water inlet device; the inlet of the superfine grating is connected with the outlet of the water inlet device and is 1 mm; the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank; a 0.22 mu m micropore aeration disc arranged at the bottom of the aerobic tank; an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank; the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump; the switching type anaerobic/anoxic tank is provided with a suspended filler; the MBR-MD coupling membrane comprises: the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR (membrane bioreactor) membrane (the inner diameter of the adopted MBR membrane wire is 1.0mm, and the outer diameter range is 1.2mm) and a deoxygenation membrane (the inner diameter of the adopted deoxygenation membrane wire is 0.2mm, and the outer diameter range is 0.25mm) arranged inside the MBR membrane; the membrane blowing aeration device (adopting a perforated aeration pipe with the aperture of 8 mm) arranged at the lower part of the coupling membrane group device, an air blower used for blowing the coupling membrane group device and a water production vacuum pump connected with the gas collecting pipe are arranged, and the gas collecting pipe is connected with a microporous aeration disc at the bottom of the aerobic tank through a degassing vacuum pump.
Filtering sewage by using an ultrafine grid, and then performing treatment according to the following steps of 4:1 respectively flows into an aerobic zone and an anaerobic/anoxic zone, and the total retention time is 8 h: in the aerobic zone, the membrane group device is perforated for aeration and oxygen supply, and the sewage flowing into the aerobic zone is subjected to nitration reaction under the action of aerobic nitrifying bacteria to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen. Sewage enters an MBR membrane inner layer after being filtered by an MBR membrane, the filtered sewage is contacted with an MD deoxidizing membrane in the MBR membrane inner layer, oxygen in the sewage is pumped out/swept by a degassing vacuum pump under the action of negative pressure/partial pressure and is collected to a gas collecting pipe at the bottom, the gas collecting pipe is connected with a micropore aeration disc of an aerobic area, oxygen is supplied to the aerobic area by recovered oxygen-enriched air through the micropore aeration disc, and the sewage after being deoxidized is pumped into an anaerobic/anoxic area by a water-producing vacuum pump. The sewage enters an anaerobic/anoxic zone twice, the untreated sewage directly enters the anaerobic/anoxic zone according to a proper proportion for the first time, the hydraulic retention time of the stage is 4 hours, the sewage provides a carbon source for denitrifying phosphorus-accumulating bacteria, and because an aeration device is not arranged in the anaerobic/anoxic zone, the denitrifying phosphorus-accumulating bacteria release phosphorus and synthesize PHA/PHB to be stored in a body under the completely anaerobic condition. And in the second time, the sewage after nitrification and deoxidation treatment is pumped into an anaerobic/anoxic zone by a vacuum pump, the hydraulic retention time in the stage is 4 hours, nitrate nitrogen/nitrite nitrogen in nitrifying liquid changes the anaerobic/anoxic zone from an anaerobic environment to an anoxic environment, denitrifying phosphorus accumulating bacteria take the nitrate nitrogen/nitrite nitrogen as an electron acceptor, PHA/PHB stored in the body is used as energy, the nitrate nitrogen/nitrite nitrogen is reduced into nitrogen while phosphorus is absorbed, and synchronous nitrogen and phosphorus removal is completed. After a series of treatments, the supernatant is discharged from the anaerobic/anoxic zone in an overflow manner.
The test water is taken from domestic sewage of a certain municipal sewage treatment plant in Fujian, and the main water quality indexes are as follows: CODCr＝378mg/L，NH3-59 mg/L-66 mg/L-5.6 mg/L, the above criteria being determined according to the standard method in water and wastewater monitoring and analysis methods (fourth edition).
The device of this embodiment is when using, and aerobic district and anaerobism/anoxic zone are squeezed into respectively to sewage through the intake pump, and the proportion of intaking is 3: 1, the total hydraulic retention time of the sewage in the reactor is 10h, and the reactor is a sequencing batch reactor: in the first 6h, the aerobic nitrification bacteria in the aerobic zone are aerated by the perforated aeration pipe below the membrane group device to supply oxygen for nitrification reaction, and in the 6h, the sewage entering the anaerobic/anoxic zone provides a carbon source for the denitrifying phosphorus accumulating bacteria under the complete anaerobic condition so as to carry out anaerobic phosphorus release and synthesize PHA/PHB. After 4 hours, a vacuum pump of the MBR-MD coupling membrane system is started, oxygen in the sewage in the aerobic zone is removed and recovered, then the sewage is pumped into a microporous aeration disc to supply oxygen to the aerobic zone, the sewage after deoxygenation is pumped into an anaerobic/anoxic zone, and the process lasts for 4 hours. After entering the anaerobic/anoxic zone, the deoxidized and nitrified liquid brings in nitrate and nitrite, and the denitrifying phosphorus-accumulating bacteria in the anaerobic/anoxic zone perform synchronous nitrogen and phosphorus removal by taking nitrate nitrogen and nitrite nitrogen as electron acceptors and PHA/PHB stored in vivo as carbon sources (electron donors).
After 1 month acclimatization and culture according to the above implementation steps, effluent CODCr、NH3The average concentration of-N, TN and TP is respectively 27.6 mg/L, 1.1 mg/L, 11.6 mg/L and 0.8 mg/L, and the water is finally produced by an anaerobic/anoxic zone, and the denitrification dephosphorization process is easy to control, so that the system has good removal effect on TN and TP and meets the A standard requirement of the primary standard of urban sewage discharge standard (GB 18918-2002). in addition, a special aeration oxygen supply device is omitted, the gas-water ratio of the system is less than 10: 1, the gas-water ratio of the system is saved by more than half compared with the gas-water ratio of 20: 1-30: 1 in the traditional MBR process, and a reflux device is omitted, so the energy consumption (0.58kWh/t) of the system for water treatment per ton is lower than that of the traditional MBR process (0.9-1.3 kWh/t).
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (10)

1. An O-M-A/A nitrogen and phosphorus removal device based on an MBR-MD coupling membrane is characterized by comprising:
a water inlet device;
the inlet of the superfine grating is connected with the outlet of the water inlet device;
the outlet of the superfine grating is respectively connected with the aerobic tank and the switching type anaerobic/anoxic tank;
the microporous aeration disc is arranged at the bottom of the aerobic tank;
an inlet of the MBR-MD coupling membrane is connected with an outlet of the aerobic tank;
the MBR-MD coupling membrane is connected with a switching type anaerobic/anoxic tank through a water production vacuum pump;
the switching type anaerobic/anoxic tank is provided with a suspended filler;
the MBR-MD coupling membrane comprises:
the gas collecting pipe is arranged at the lower part of the coupling membrane group device, and the water collecting pipe is arranged at the upper part of the coupling membrane group device; the coupling membrane combiner comprises an MBR membrane and a deoxygenation membrane arranged inside the MBR membrane; the membrane sweeping and aerating device is arranged at the lower part of the gas collecting pipe, the air blower is used for blowing the coupled membrane group device, the water producing vacuum pump is connected with the water collecting pipe, and the gas collecting pipe is connected with the microporous aeration disc at the bottom of the aerobic tank through the degassing vacuum pump.
2. The device of claim 1, wherein the deoxygenation membrane is an organic membrane or an inorganic membrane; the deoxygenation membrane is a hollow fiber membrane or a flat membrane; the pore diameter of the deoxygenation membrane is 0.01-0.03 mu m; the diameter of the MBR membrane is 1-3 mm, and the aperture is 0.03-0.4 μm; the membrane blowing aeration device is a perforated pipe;
the deoxidation mode adopted by the deoxidation membrane is as follows: gas purging, negative pressure suction, or a combination of gas purging and negative pressure suction.
3. The apparatus of claim 1, wherein the MBR-MD coupled membrane has: the membrane sweeping aeration device leads the membrane wire to shake and wash the surface of the membrane wire through aeration of the gas collecting pipe; the aperture of the perforated pipe is preferably 3-8 mm.
4. The device according to claim 1, wherein the suspension filler is a spherical suspension filler, and the specification of the ultrafine grid is 1-5 mm; the aperture of the micropore aeration disc is 0.22-100 mu m.
5. The device of claim 1, wherein the inner diameter size of the deoxygenation membrane filaments in the MBR-MD coupling membrane ranges from 0.1mm to 0.3mm, and the outer diameter size ranges from 0.2mm to 0.4 mm; the inner diameter size range of the MBR membrane filaments is 0.8-1.1 mm, and the outer diameter size range is 0.9-1.2 mm.
6. An O-M-A/A nitrogen and phosphorus removal method based on an MBR-MD coupling membrane is characterized by comprising the following steps:
sewage is filtered by a superfine grating and then flows into an aerobic tank and a switching type anaerobic/anoxic tank respectively according to a proportion;
part of sewage is subjected to nitration reaction under the action of aerobic nitrifying bacteria in an aerobic tank to convert ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and digestion liquid flows into an MBR-MD coupling membrane;
the nitrified liquid enters the inner layer after being filtered by the outer MBR membrane, gas molecules are pumped to a microporous aeration disc of the aerobic tank under the action of the inner deoxygenation membrane, and the nitrified liquid after deoxygenation is pumped into the anaerobic/anoxic tank;
the other part of sewage enters an anaerobic/anoxic tank to provide carbon source and phosphorus for denitrifying phosphorus accumulating bacteria, and the denitrifying phosphorus accumulating bacteria absorb the carbon source under anaerobic condition to complete phosphorus release and obtain energy at the same time; and (3) introducing a deoxygenation and nitrification solution, and reducing nitrate nitrogen/nitrite nitrogen into nitrogen while absorbing phosphorus by using the energy obtained under the anaerobic condition by denitrifying phosphorus accumulating bacteria under the anoxic condition by taking nitrate nitrogen/nitrite nitrogen as an electron acceptor so as to realize synchronous nitrogen and phosphorus removal.
7. The preparation method of claim 6, wherein the switching anaerobic/anoxic tank controls the switching between anaerobic and anoxic environments by controlling the inflow time of the nitrified liquid after deoxidation: the anaerobic/anoxic zone is not provided with an aeration device, the reaction tank has no molecular oxygen or combined oxygen before the deoxidized nitrified liquid flows in, and is an anaerobic environment, and the reaction tank becomes an anoxic environment along with the entry of the combined oxygen after the deoxidized nitrified liquid flows in.
8. The preparation method according to claim 6, wherein the gas molecules are pumped to the microporous aeration disc of the aerobic tank by the gas molecules: gas molecules are pumped out/swept and collected to the gas collecting pipe by a degassing vacuum pump under the action of negative pressure/partial pressure, and then pumped to a microporous aeration disc of the aerobic tank;
the method for pumping the deoxygenated nitrified liquid into the anaerobic/anoxic tank specifically comprises the following steps: the deoxidized nitrified liquid is pumped into an anaerobic/anoxic tank by a water producing vacuum pump.
9. The preparation method of claim 6, wherein the hydraulic retention time of the aerobic tank is 6-10 h; the hydraulic retention time of the other part of sewage entering the anaerobic/anoxic tank is 2-4 h; the hydraulic retention time of the deoxygenated and nitrified liquid after entering the anaerobic/anoxic tank is 3-6 h;
after the sewage is subjected to nitrogen and phosphorus removal treatment, supernatant is overflowed and discharged from the anaerobic/anoxic zone.
10. The preparation method of claim 6, wherein an extremely low negative oxygen pressure is formed inside the deoxygenation membrane under the combined action of air inlet of the blower and suction of the degassing vacuum pump, and oxygen molecules in the sewage are pressed into the interior of the deoxygenation membrane under the action of a higher oxygen partial pressure, so that the deoxygenation process is completed.
CN202010424966.3A 2020-05-19 2020-05-19 O-M-A/A nitrogen and phosphorus removal device and method based on MBR-MD coupling membrane Pending CN111410386A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112429846A (en) * 2020-11-19 2021-03-02 海天水务集团股份公司 Sewage nitrogen and phosphorus removal system based on membrane

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112429846A (en) * 2020-11-19 2021-03-02 海天水务集团股份公司 Sewage nitrogen and phosphorus removal system based on membrane
CN112429846B (en) * 2020-11-19 2022-07-19 海天水务集团股份公司 Sewage nitrogen and phosphorus removal system based on membrane

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