CN114368837A - Integrated denitrification membrane bioreactor and sewage treatment method using same - Google Patents

Integrated denitrification membrane bioreactor and sewage treatment method using same Download PDF

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CN114368837A
CN114368837A CN202210044015.2A CN202210044015A CN114368837A CN 114368837 A CN114368837 A CN 114368837A CN 202210044015 A CN202210044015 A CN 202210044015A CN 114368837 A CN114368837 A CN 114368837A
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CN114368837B (en
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田家宇
孟桐洋
肖峰
高珊珊
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Hebei University of Technology
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/001—Upstream control, i.e. monitoring for predictive control
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/16—Total nitrogen (tkN-N)
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/44—Time
    • 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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  • Separation Using Semi-Permeable Membranes (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

The invention provides an integrated denitrification membrane bioreactor and a sewage treatment method using the same. The integrated denitrification membrane bioreactor is provided with at least one reaction tank, and the reaction tank comprises an aerobic unit I area, an anoxic unit and an aerobic unit II area; partition plates are respectively arranged between the first aerobic unit area and the second anoxic unit area, and between the second anoxic unit area and the second aerobic unit area; the bottom of the anoxic unit is provided with a convex slope. The integrated denitrification membrane bioreactor disclosed by the invention enables microorganisms to better adapt to the environment with both aerobic and anoxic existence, avoids the problem of poor denitrification effect caused by sludge backflow, realizes efficient and stable removal of pollutants such as nitrogen, organic matters and the like in domestic sewage, and enhances the denitrification treatment effect.

Description

Integrated denitrification membrane bioreactor and sewage treatment method using same
Technical Field
The invention relates to a membrane bioreactor, which is applied to integrated denitrification sewage treatment and belongs to the technical field of sewage treatment.
Background
Membrane Bioreactor (MBR) is a sewage treatment technology in which a biological treatment unit is organically combined with a membrane separation unit. The biological treatment unit is mainly used for completing the conversion and removal of organic matters, inorganic matters and nutrient substances in the sewage; the membrane separation unit mainly completes solid-liquid separation and replaces a secondary sedimentation tank in the traditional sewage biological treatment process. The membrane interception function in the MBR can intercept all biomass in the reactor, improve the sludge age and the sludge concentration, and is beneficial to the reproduction of nitrifying bacteria, thereby improving the nitrification rate. Compared with the traditional sewage biological treatment process, the MBR integrates the effects of removing chromaticity, turbidity, organic pollutants, solid-liquid separation and the like, and has the advantages of good effluent quality, less residual sludge, small floor area, high sludge concentration, cost saving, stable system and the like. In recent years, with the gradual increase of the concern of governments and residents on the water ecological environment and water quality safety problems, the gradual upgrade of water quality discharge standards of sewage treatment plants, and the MBR process is widely applied to municipal, domestic and industrial sewage treatment.
However, the development and application of MBR process are still seriously affected due to the unsatisfactory denitrification effect. The conventional MBR process usually adopts high aeration rate to achieve the purpose of controlling membrane pollution, but the over-high dissolved oxygen can cause serious negative influence on an anoxic (anaerobic) microenvironment required by the denitrification process, and inhibit the activity of denitrifying bacteria, thereby influencing the denitrification effect and reducing the quality of effluent water. However, too low dissolved oxygen also results in the inability of nitrifying bacteria to effectively complete the conversion of ammonia nitrogen, thereby resulting in a decrease in the overall nitrogen removal efficiency. In recent years, in order to enhance the denitrification effect of the MBR process, researchers have proposed methods such as introducing an electrochemical reaction, improving a process flow, and creating a reactor structure.
For example, the chinese patent publication CN 112591877 a provides a membrane bioreactor for decentralized wastewater denitrification and dephosphorization and a wastewater treatment method, which improves the denitrification and dephosphorization effect by introducing an electrochemical reaction-assisted membrane bioreactor, increases the operation cost, and still needs to improve the denitrification effect.
The Chinese patent publication CN 113603304A discloses a three-sludge aerobic-hydrolysis-aerobic-membrane bioreactor and a method, wherein an aerobic tank, a hydrolysis tank and an MBR reactor are integrated, but the process flow is too complicated, the reactor construction investment cost is high, the denitrification effect is poor, and the TN removal rate is only 82.6%.
Chinese patent publication CN 111439892A discloses an integrated membrane bioreactor domestic sewage treatment device and method, wherein the device is too complex and the organic matter removal rate is only 85%.
Therefore, MBR reactor devices and operation flows are further innovated, the denitrification rate is increased, the stable quality of effluent is ensured, the sewage treatment process which can realize efficient denitrification and has the advantages of being green, low-carbon, energy-saving, consumption-reducing, low in cost, high in benefit and the like is developed, and the method has important practical significance.
Disclosure of Invention
The invention aims to provide an integrated denitrification membrane bioreactor.
The invention also aims to provide a sewage treatment method applying the integrated denitrification membrane bioreactor.
The integrated denitrification membrane bioreactor provided by the invention is provided with at least one reaction tank, wherein the reaction tank comprises an aerobic unit I area, an anoxic unit (anaerobic unit) and an aerobic unit II area; partition plates are respectively arranged between the first aerobic unit area and the second anoxic unit area, and between the second anoxic unit area and the second aerobic unit area; the bottom of the anoxic unit is provided with a convex slope.
The bottom of the anoxic unit is preferably a symmetrical convex slope; the gradient is preferably 1:0.5 to 1: 2.
An aerobic unit aeration oxygenation device is arranged at the inner bottom of the aerobic unit zone.
And an aerobic unit aeration oxygenation device is arranged at the inner bottom of the aerobic unit zone II.
The aerobic unit aeration and oxygenation device is connected with an oxygenation pump through a pipeline and an aerobic aeration check valve.
The oxygen-deficient unit is provided with a residual sludge discharge valve.
The first aerobic unit area and the second aerobic unit area are respectively provided with membrane components. When the reactor is in operation, sewage passes through the membrane module to be purified.
The above-mentionedThe membrane component is a ceramic flat membrane; preferably, the pore diameter is 0.20-0.80 μm, and the membrane flux is 10-30L/(m)2·h)。
The partition plate is arranged between the first aerobic unit area and the second anoxic unit area, and the partition plate is connected to the control electric box; the control electric box controls the partition plate to move up and down; when the reactor runs, the ratio of the height of the partition plate to the depth of the sludge mixed liquid in the reaction tank is 1: 3-2: 3.
The integrated denitrification membrane bioreactor disclosed by the invention enables microorganisms to better adapt to the environment with both aerobic and anaerobic conditions, avoids the problem of poor denitrification effect caused by sludge backflow, realizes efficient and stable removal of pollutants such as nitrogen, organic matters and the like in domestic sewage, and enhances the denitrification treatment effect.
Based on the integrated denitrification membrane bioreactor, the sewage treatment method using the integrated denitrification membrane bioreactor comprises the following treatment steps:
A. the domestic sewage is divided into two paths, is respectively output from two paths of pipelines of the water inlet tank, and respectively enters the aerobic unit first area and the aerobic unit second area through the water inlet valve and the water inlet pump;
B. the bottom parts of the first aerobic unit area and the second aerobic unit area are respectively provided with an aerobic unit aeration oxygenation device; air is respectively provided by an oxygenation pump and is respectively injected into the aerobic unit first area and the aerobic unit second area through a gas rotor flow meter, an aerobic aeration check valve and an aerobic unit aeration oxygenation device; the aeration intensity is respectively controlled and adjusted by a gas rotameter;
C. during the aeration work period of the first aerobic unit area and the second aerobic unit area, the partition plate is controlled by the control electric box and is in a putting down state (namely a closing state), so that three relatively independent units, namely the first aerobic unit area, the anoxic unit area and the second aerobic unit area, are formed in the reaction tank; activated sludge flocs in the sludge mixed liquor in the aerobic unit first area and the aerobic unit second area freely sink in the anoxic unit due to the aeration effect;
D. during the aeration work period of the first aerobic unit area and the second aerobic unit area, membrane components in the first aerobic unit area and the second aerobic unit area are respectively arranged above the aeration and oxygenation device of the aerobic unit, and air is respectively injected into the first aerobic unit area and the second aerobic unit area through the gas rotor flow meter, the aerobic aeration check valve and the aeration and oxygenation device of the aerobic unit; on one hand, necessary oxygen is improved for aerobic biochemical reaction, and on the other hand, the membrane pollution degree of the membrane component is controlled by utilizing the aeration scouring effect;
E. each membrane component is respectively connected with a water outlet pump through a water outlet valve, and the treated clean water is discharged through the suction of the water outlet pump;
F. the aeration of the first aerobic unit area and the second aerobic unit area is stopped, the water outlet pump stops pumping water, the water inlet pump stops feeding water, the partition plate is lifted up under the control of the control electric box, and the precipitated sludge in the anoxic unit slides down to the first aerobic unit area and the second aerobic unit area respectively through the convex slopes under the action of gravity; then the partition plate is put down under the control of the control electric box again, three relatively independent units are formed in the reaction tank again, and the aeration in the aerobic unit I area and the aerobic unit II area is in a working state again; the circulation is carried out in this way, and the domestic sewage treatment process is completed.
When the sewage treatment method is operated, the volume ratio of the aerobic unit first area, the anoxic unit and the aerobic unit second area is preferably 3:2: 3.
The ratio of the water inlet flow rate of the aerobic unit first area to the aerobic unit second area is preferably 1: 1.
The ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit I area to the aerobic unit II area is preferably 1: 1; a constant flow rate is preferred.
The ratio of the hydraulic retention time of the aerobic unit first zone and the aerobic unit second zone to the hydraulic retention time of the anoxic unit is preferably 3: 1.
The time of each aeration of the aerobic unit zone I and the aerobic unit zone II is preferably 10-60min, and the interval time between two times of aeration is preferably 1-10 min.
The aeration intensity of the aerobic unit first area and the aerobic unit second area is preferably controlled to be 0.5-3mg/L of DO.
In order to realize the regular discharge of the sludge, the anoxic unit is provided with a residual sludge discharge valve; one period is formed between two times of aeration, and sludge is discharged once in 10-50 periods.
The invention constructs an integrated high-efficiency denitrification membrane bioreactor device aiming at the problems of high capital construction and operating cost and low denitrification efficiency of a conventional MBR (membrane bioreactor) in the traditional sewage treatment process. The conventional MBR is divided into an aerobic unit and an anoxic (anaerobic) unit in a spatial functional partition manner, so that the structure can solve the contradiction that ammonia nitrogen oxidation needs an aerobic environment in the nitrification process and nitrate nitrogen reduction needs an anoxic (anaerobic) environment in the denitrification process, and efficiently complete synchronous nitrification and denitrification. The two aerobic units work simultaneously, so that the working efficiency and the denitrification effect of the whole process can be improved.
The domestic sewage realizes synchronous nitrification and denitrification under the combined action of the aerobic unit and the anoxic (anaerobic) unit, and then is subjected to solid-liquid separation through the membrane module and the water outlet pump to obtain stable outlet water meeting the water quality standard. In the process of the operation of the process, the interception function of the membrane component can ensure that microorganisms in the reactor can effectively stay and proliferate, and the nitrification rate is improved; bubbles generated by aeration of the aerobic unit have a certain scouring effect on the membrane component, so that membrane pollution can be reduced; when the aeration is stopped, the water outlet is stopped, the membrane component is stopped for a certain time, and the membrane pollution can be relieved.
Drawings
FIG. 1 is a process flow diagram of the operation of the integrated denitrification membrane bioreactor device of the present invention.
FIG. 2 is a top view of the integrated denitrification membrane bioreactor apparatus of the present invention.
FIG. 3 is a front view of the integrated denitrification membrane bioreactor apparatus of the present invention.
FIG. 4 is a left side view of the integrated denitrification membrane bioreactor apparatus of the present invention.
1-reaction tank 2-aerobic unit first zone 3-anoxic (anaerobic) unit 4-aerobic unit second zone
5-clapboard 6-clapboard 7-symmetrical convex slope 8-membrane component
9-membrane component 10-aerobic unit aeration oxygenation device
11-aerobic unit aeration oxygenation device 12-excess sludge discharge valve 13-water inlet tank
14-inlet tank 15-inlet valve 16-inlet valve 17-inlet pump
18-water inlet pump 19-oxygenation pump 20-oxygenation pump
21-gas rotameter 22-gas rotameter
23-aerobic aeration check valve 24-aerobic aeration check valve
25-water outlet pump 26-water outlet pump 27-water outlet valve 28-water outlet valve
29-control electrical box
Detailed Description
The invention is further described below in conjunction with fig. 1 to 4.
The invention discloses an integrated high-efficiency denitrification membrane bioreactor device for domestic sewage treatment, which comprises: reaction tank (1), reaction tank (1) is including good oxygen unit first district (2), lack (anaerobism) oxygen unit (3) and good oxygen unit second district (4), separates by baffle (5) between good oxygen unit first district (2) and lack (anaerobism) oxygen unit (3), lacks (anaerobism) oxygen unit (3) and good oxygen unit second district (4) and separates by baffle (6), lacks (anaerobism) oxygen unit (3) bottom and has symmetry protruding form slope (7).
Wherein an aerobic unit aeration and oxygenation device (10) is arranged at the inner bottom of the aerobic unit first zone (2);
wherein, lack the interior bottom of (anaerobism) oxygen unit (3) and be equipped with symmetrical protruding form slope (7), the slope is 1: 0.5-1: 2;
wherein an aerobic unit aeration and oxygenation device (11) is arranged at the inner bottom of the aerobic unit second zone (4);
wherein the aerobic unit aeration oxygen increasing device (10) and the aerobic unit aeration oxygen increasing device (11) are connected with an oxygen increasing pump (19) and an oxygen increasing pump (20) through pipelines and an aerobic aeration check valve (23) and an aerobic aeration check valve (24).
Wherein the anoxic (anaerobic) unit (3) is provided with a surplus sludge discharge valve (12).
Wherein the membrane component (8) and the membrane component (9) both adopt ceramic flat membrane, the aperture is 0.20-0.80 μm, and the membrane flux is 10-30L/(m)2·h)。
The partition plate (5) between the aerobic unit first zone (2) and the anoxic (anaerobic) unit (3), and the partition plate (6) between the anoxic (anaerobic) unit (3) and the aerobic unit second zone (4) are connected to the control electric box (29), and the control electric box (29) controls the partition plate (5) and the partition plate (6) to move up and down at regular time; the ratio of the height of the sludge to the depth of the sludge mixed liquid in the reaction tank is 1: 3-2: 3.
the invention can be realized by the following specific use steps:
the domestic sewage is divided into two paths and is output from two paths of pipelines of a water inlet tank (13) and a water inlet tank (14), wherein the first path of domestic sewage enters an aerobic unit zone I (2) through a water inlet valve (15) and a water inlet pump (17);
the second path of domestic sewage enters the second aerobic unit area (4) through a water inlet valve (16) and a water inlet pump (18);
the bottom parts of the aerobic unit first area (2) and the aerobic unit second area (4) are respectively provided with an aerobic unit aeration oxygen increasing device (10) and an aerobic unit aeration oxygen increasing device (11); at the moment, air (oxygen) is respectively provided by an oxygenation pump (19) and an oxygenation pump (20), the air (oxygen) is respectively injected into an aerobic unit first area (2) and an aerobic unit second area (4) through a gas rotor flow meter (21), a gas rotor flow meter (22), an aerobic aeration check valve (23), an aerobic aeration check valve (24), an aerobic unit aeration device (10) and an aerobic unit aeration device (11), and the aeration intensity is respectively controlled and adjusted by the gas rotor flow meter (21) and the gas rotor flow meter (22);
during the aeration work period of the first aerobic unit area (2) and the second aerobic unit area (4), the partition plates (5) and the partition plates (6) are controlled by the control electric box (29) and are in a putting down state (namely a closing state), so that three relatively independent units are formed in the reaction tank, namely the first aerobic unit area (2), the anoxic (anaerobic) unit (3) and the second aerobic unit area (4), and activated sludge flocs in sludge mixed liquid in the first aerobic unit area (2) and the second aerobic unit area (4) freely sink in the anoxic (anaerobic) unit (3) due to the aeration effect;
during the aeration work period of the first aerobic unit area (2) and the second aerobic unit area (4), membrane components (8) and membrane components (9) in the first aerobic unit area (2) and the second aerobic unit area (4) are arranged above an aerobic unit aeration oxygen increasing device (10) and an aerobic unit aeration oxygen increasing device (11), air (oxygen) is respectively injected into the first aerobic unit area (2) and the second aerobic unit area (4) through a gas rotor flow meter (21), a gas rotor flow meter (22), an aerobic aeration check valve (23), an aerobic aeration check valve (24), the aerobic unit aeration oxygen increasing device (10) and the aerobic unit aeration oxygen increasing device (11), on one hand, necessary oxygen is increased for aerobic biochemical reaction, on the other hand, membrane pollution of the membrane components (8) and the membrane components (9) is controlled by utilizing an aeration scouring effect;
the water outlet pump (25) and the water outlet pump (26) are respectively connected with the membrane component (8) and the membrane component (9) through a water outlet valve (27) and a water outlet valve (28), and the treated clean water is discharged through the suction of the water outlet pump;
the aeration of the first aerobic unit area (2) and the second aerobic unit area (4) is stopped, the water outlet pump (25) and the water outlet pump (26) stop pumping out water, the water inlet pump (17) and the water inlet pump (18) stop feeding water, at the moment, the partition plate (5) and the partition plate (6) are controlled by the control electric box (29) to lift up, and the precipitated sludge in the anoxic (anaerobic) unit (3) slides down to the first aerobic unit area (2) and the second aerobic unit area (4) through the symmetrical convex slope (7) under the action of gravity; then the partition plates (5) and the partition plates (6) are controlled by the control electric box (29) to be put down again, three relatively independent units are formed in the reaction tank again, and the aeration in the aerobic unit first area (2) and the aerobic unit second area (4) is in a working state again. The circulation is carried out in this way, and the domestic sewage treatment process is completed.
The volume ratio of the aerobic unit first area (2), the anoxic (anaerobic) unit (3) and the aerobic unit second area (4) is 3:2: 3.
the ratio of the water inflow rate of the aerobic unit first area (2) to the water inflow rate of the aerobic unit second area (4) is 1: 1.
the ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit first area (2) to the aerobic unit second area (4) is 1:1, constant flow.
The ratio of the hydraulic retention time of the aerobic unit first zone (2) and the aerobic unit second zone (4) to the hydraulic retention time of the anoxic (anaerobic) unit (3) is 3: 1.
Each time of aeration of the aerobic unit first area (2) and the aerobic unit second area (4) is 10-60min, and the interval time between two times of aeration is 1-10 min.
The aeration intensity of the aerobic unit first area (2) and the aerobic unit second area (4) is controlled to be 0.5-3 mg/L.
The anaerobic unit (3) is provided with a residual sludge discharge valve (12) to realize the periodic discharge of sludge, one period is from the beginning of one aeration to the beginning of the next aeration, and sludge is discharged once in 10-50 periods.
Example 1
The reactor is filled with moderate-intensity urban domestic sewage, the carbon source is mainly glucose, and the nitrogen source is mainly NH4Cl and urea, the phosphorus source is mainly KH2PO4And K2HPO4Alkalinity is mainly NaHCO3. The average COD concentration of the domestic sewage is 564mg/L, the average ammonia nitrogen concentration is 24.58mg/L, the average TN concentration is 39.5mg/L, and the average TP concentration is 5.96 mg/L.
Lack the interior bottom of (anaerobism) oxygen unit (3) and be equipped with symmetrical protruding form slope (7), the slope is 1: 1.
the effective volume ratio of the aerobic unit first zone (2), the anoxic (anaerobic) unit (3) and the aerobic unit second zone (4) is 3:2: 3.
the water inlet flow rate of the aerobic unit first area (2) and the aerobic unit second area (4) is 1: 1.
the ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit first area (2) to the aerobic unit second area (4) is 1:1, constant flow.
The aeration time of the aerobic unit first area (2) and the aerobic unit second area (4) is 40min, and the interval time between two times of aeration is 5 min.
The ratio of the height of the partition plates (5) and (6) to the depth of the sludge mixed liquor in the reaction tank is 1: 3.
the aeration intensity of the aerobic unit first area (2) and the aerobic unit second area (4) is controlled to be DO of 0.5 mg/L.
The sludge concentration of the mixed liquid in the reaction tank is 8000 mg/L.
The integral hydraulic retention time in the reaction tank is 8 h.
The sludge retention time in the reaction tank is 20 d.
The membrane module has a pore diameter of 0.22 μm and a membrane flux of 15L/(m)2·h)。
The transmembrane pressure difference of the membrane module is maintained within 40 kPa.
The reaction temperature is controlled to be about 22 ℃.
The pH value is controlled to be about 7.8.
The process runs for 100d, and the treatment results are as follows:
Figure BDA0003471445990000081
example 2
The reactor is filled with moderate-intensity urban domestic sewage, the carbon source is mainly glucose, and the nitrogen source is mainly NH4Cl and urea, the phosphorus source is mainly KH2PO4And K2HPO4Alkalinity is mainly NaHCO3. The average COD concentration of the domestic sewage is 564mg/L, the average ammonia nitrogen concentration is 24.58mg/L, the average TN concentration is 39.5mg/L, and the average TP concentration is 5.96 mg/L.
Lack the interior bottom of (anaerobism) oxygen unit (3) and be equipped with symmetrical protruding form slope (7), the slope is 1: 1.
the effective volume ratio of the aerobic unit first zone (2), the anoxic (anaerobic) unit (3) and the aerobic unit second zone (4) is 3:2: 3.
the water inlet flow rate of the aerobic unit first area (2) and the aerobic unit second area (4) is 1: 1.
the ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit first area (2) to the aerobic unit second area (4) is 1:1, constant flow.
The aeration time of the aerobic unit first area (2) and the aerobic unit second area (4) is 40min, and the interval time between two times of aeration is 5 min.
The ratio of the height of the partition plates (5) and (6) to the depth of the sludge mixed liquor in the reaction tank is 1: 3.
the aeration intensity of the aerobic unit first area (2) and the aerobic unit second area (4) is controlled to be 1 mg/L.
The sludge concentration of the mixed liquid in the reaction tank is 8000 mg/L.
The integral hydraulic retention time in the reaction tank is 8 h.
The sludge retention time in the reaction tank is 20 d.
The membrane module has a pore diameter of 0.22 μm and a membrane flux of 15L/(m)2·h)。
The transmembrane pressure difference of the membrane module is maintained within 40 kPa.
The reaction temperature is controlled to be about 22 ℃.
The pH value is controlled to be about 7.8.
The process runs for 100d, and the treatment results are as follows:
Figure BDA0003471445990000091
example 3
The reactor is filled with moderate-intensity urban domestic sewage, the carbon source is mainly glucose, and the nitrogen source is mainly NH4Cl and urea, the phosphorus source is mainly KH2PO4And K2HPO4Alkalinity is mainly NaHCO3. The average COD concentration of the domestic sewage is 564mg/L, the average ammonia nitrogen concentration is 24.58mg/L, the average TN concentration is 39.5mg/L, and the average TP concentration is 5.96 mg/L.
Lack the interior bottom of (anaerobism) oxygen unit (3) and be equipped with symmetrical protruding form slope (7), the slope is 1: 1.
the effective volume ratio of the aerobic unit first zone (2), the anoxic (anaerobic) unit (3) and the aerobic unit second zone (4) is 3:2: 3.
the water inlet flow rate of the aerobic unit first area (2) and the aerobic unit second area (4) is 1: 1.
the ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit first area (2) to the aerobic unit second area (4) is 1:1, constant flow.
The aeration time of the aerobic unit first area (2) and the aerobic unit second area (4) is 40min, and the interval time between two times of aeration is 5 min.
The ratio of the height of the partition plates (5) and (6) to the depth of the sludge mixed liquor in the reaction tank is 1: 3.
the aeration intensity of the aerobic unit first area (2) and the aerobic unit second area (4) is controlled to be 2 mg/L.
The sludge concentration of the mixed liquid in the reaction tank is 8000 mg/L.
The integral hydraulic retention time in the reaction tank is 8 h.
The sludge retention time in the reaction tank is 20 d.
The membrane module has a pore diameter of 0.22 μm and a membrane flux of 15L/(m)2·h)。
The transmembrane pressure difference of the membrane module is maintained within 40 kPa.
The reaction temperature is controlled to be about 22 ℃.
The pH value is controlled to be about 7.8.
The process runs for 100d, and the treatment results are as follows:
Figure BDA0003471445990000101
example 4
The reactor is filled with moderate-intensity urban domestic sewage, the carbon source is mainly glucose, and the nitrogen source is mainly NH4Cl and urea, the phosphorus source is mainly KH2PO4And K2HPO4Alkalinity is mainly NaHCO3. The average COD concentration of the domestic sewage is 564mg/L, the average ammonia nitrogen concentration is 24.58mg/L, the average TN concentration is 39.5mg/L, and the average TP concentration is 5.96 mg/L.
Lack the interior bottom of (anaerobism) oxygen unit (3) and be equipped with symmetrical protruding form slope (7), the slope is 1: 1.
the effective volume ratio of the aerobic unit first zone (2), the anoxic (anaerobic) unit (3) and the aerobic unit second zone (4) is 3:2: 3.
the water inlet flow rate of the aerobic unit first area (2) and the aerobic unit second area (4) is 1: 1.
the ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit first area (2) to the aerobic unit second area (4) is 1:1, constant flow.
The aeration time of the aerobic unit first area (2) and the aerobic unit second area (4) is 40min, and the interval time between two times of aeration is 5 min.
The ratio of the height of the partition plates (5) and (6) to the depth of the sludge mixed liquor in the reaction tank is 1: 3.
the aeration intensity of the aerobic unit first area (2) and the aerobic unit second area (4) is controlled to be DO at 3 mg/L.
The sludge concentration of the mixed liquid in the reaction tank is 8000 mg/L.
The integral hydraulic retention time in the reaction tank is 8 h.
The sludge retention time in the reaction tank is 20 d.
The membrane module has a pore diameter of 0.22 μm and a membrane flux of 15L/(m)2·h)。
The transmembrane pressure difference of the membrane module is maintained within 40 kPa.
The reaction temperature is controlled to be about 22 ℃.
The pH value is controlled to be about 7.8.
The process runs for 100d, and the treatment results are as follows:
Figure BDA0003471445990000102
Figure BDA0003471445990000111

Claims (10)

1. the integrated denitrification membrane bioreactor is characterized by comprising at least one reaction tank, wherein the reaction tank comprises an aerobic unit I area, an anoxic unit and an aerobic unit II area; partition plates are respectively arranged between the first aerobic unit area and the second anoxic unit area, and between the second anoxic unit area and the second aerobic unit area; the bottom of the anoxic unit is provided with a convex slope.
2. The reactor according to claim 1, wherein the bottom of the anoxic unit is preferably a symmetrical convex ramp; the gradient is preferably 1:0.5 to 1: 2.
3. The reactor as claimed in claim 1, wherein the inner bottom of the first zone of the aerobic unit is provided with an aerobic unit aeration and oxygenation device; and an aerobic unit aeration oxygenation device is arranged at the inner bottom of the aerobic unit zone II.
4. The reactor as claimed in claim 1, wherein the aerobic unit aeration and oxygenation device is connected with an oxygenation pump through a pipeline and an aerobic aeration check valve.
5. The reactor according to claim 1, wherein the anoxic unit is provided with a surplus sludge discharge valve.
6. The reactor of claim 1, wherein the first zone of the aerobic unit and the second zone of the aerobic unit are provided with membrane modules, respectively. When the reactor is in operation, sewage passes through the membrane module. The membrane component is a ceramic flat membrane; preferably, the pore diameter is 0.20-0.80 μm, and the membrane flux is 10-30L/(m)2·h)。
7. The partition plate is arranged between the first aerobic unit area and the second anoxic unit area, and the partition plate is connected to the control electric box; the control electric box controls the partition plate to move up and down; when the reactor runs, the ratio of the height of the partition plate to the depth of the sludge mixed liquid in the reaction tank is 1: 3-2: 3.
8. A sewage treatment method using the integrated denitrification membrane bioreactor of any one of claims 1-7, which is characterized by comprising the following treatment steps:
A. the domestic sewage is divided into two paths, is respectively output from two paths of pipelines of the water inlet tank, and respectively enters the aerobic unit first area and the aerobic unit second area through the water inlet valve and the water inlet pump;
B. the bottom parts of the first aerobic unit area and the second aerobic unit area are respectively provided with an aerobic unit aeration oxygenation device; air is respectively provided by an oxygenation pump and is respectively injected into the aerobic unit first area and the aerobic unit second area through a gas rotor flow meter, an aerobic aeration check valve and an aerobic unit aeration oxygenation device; the aeration intensity is respectively controlled and adjusted by a gas rotameter;
C. during the aeration work period of the first aerobic unit area and the second aerobic unit area, the partition plate is controlled by the control electric box and is in a putting down state (namely a closing state), so that three relatively independent units, namely the first aerobic unit area, the anoxic unit area and the second aerobic unit area, are formed in the reaction tank; activated sludge flocs in the sludge mixed liquor in the aerobic unit first area and the aerobic unit second area freely sink in the anoxic unit due to the aeration effect;
D. during the aeration work period of the first aerobic unit area and the second aerobic unit area, membrane components in the first aerobic unit area and the second aerobic unit area are respectively arranged above the aeration and oxygenation device of the aerobic unit, and air is respectively injected into the first aerobic unit area and the second aerobic unit area through the gas rotor flow meter, the aerobic aeration check valve and the aeration and oxygenation device of the aerobic unit; on one hand, necessary oxygen is improved for aerobic biochemical reaction, and on the other hand, the membrane pollution degree of the membrane component is controlled by utilizing the aeration scouring effect;
E. each membrane component is respectively connected with a water outlet pump through a water outlet valve, and the treated clean water is discharged through the suction of the water outlet pump;
F. the aeration of the first aerobic unit area and the second aerobic unit area is stopped, the water outlet pump stops pumping water, the water inlet pump stops feeding water, the partition plate is lifted up under the control of the control electric box, and the precipitated sludge in the anoxic unit slides down to the first aerobic unit area and the second aerobic unit area respectively through the convex slopes under the action of gravity; then the partition plate is put down under the control of the control electric box again, three relatively independent units are formed in the reaction tank again, and the aeration in the aerobic unit I area and the aerobic unit II area is in a working state again; the circulation is carried out in this way, and the domestic sewage treatment process is completed.
9. The method of claim 8, wherein the wastewater treatment process is operated such that the volume ratio of the first zone of the aerobic unit, the second zone of the anoxic unit and the aerobic unit is preferably 3:2: 3. The ratio of the water inlet flow rate of the aerobic unit first area to the aerobic unit second area is preferably 1: 1. The ratio of the water inlet flow rate to the water outlet flow rate of the aerobic unit I area to the aerobic unit II area is preferably 1: 1; a constant flow rate is preferred. The ratio of the hydraulic retention time of the aerobic unit first zone and the aerobic unit second zone to the hydraulic retention time of the anoxic unit is preferably 3: 1.
10. The method according to claim 9, wherein each aeration time of the first aerobic unit zone and the second aerobic unit zone is preferably 10-60min, and the interval time between two aerations is preferably 1-10 min. The aeration intensity of the aerobic unit first area and the aerobic unit second area is preferably controlled to be 0.5-3mg/L of DO. In order to realize the regular discharge of the sludge, the anoxic unit is provided with a residual sludge discharge valve; one period is formed between two times of aeration, and sludge is discharged once in 10-50 periods.
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2410293Y (en) * 2000-03-12 2000-12-13 陈漫漫 Integral synchronous denitrification biological treatment reactor
JP2004261711A (en) * 2003-02-28 2004-09-24 Yoshikimi Watanabe Membrane separation activated sludge treatment apparatus and membrane separation activated sludge treatment method
CN203173888U (en) * 2013-04-03 2013-09-04 中国水电顾问集团贵阳勘测设计研究院 Integrated anoxic and aerobic membrane bioreactor
CN203668118U (en) * 2014-01-16 2014-06-25 周长鑫 Integrated reclaimed water treatment equipment adopting compound circulating biochemical membrane
CN112794581A (en) * 2021-01-15 2021-05-14 上海电力大学 Concentric cylinder type sewage treatment device and process for synchronously realizing sludge in-situ reduction and pollutant removal

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2410293Y (en) * 2000-03-12 2000-12-13 陈漫漫 Integral synchronous denitrification biological treatment reactor
JP2004261711A (en) * 2003-02-28 2004-09-24 Yoshikimi Watanabe Membrane separation activated sludge treatment apparatus and membrane separation activated sludge treatment method
CN203173888U (en) * 2013-04-03 2013-09-04 中国水电顾问集团贵阳勘测设计研究院 Integrated anoxic and aerobic membrane bioreactor
CN203668118U (en) * 2014-01-16 2014-06-25 周长鑫 Integrated reclaimed water treatment equipment adopting compound circulating biochemical membrane
CN112794581A (en) * 2021-01-15 2021-05-14 上海电力大学 Concentric cylinder type sewage treatment device and process for synchronously realizing sludge in-situ reduction and pollutant removal

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