Oxygen group-hydrogen group double-membrane sewage ultimate denitrification and carbon reduction system and oxygen group-hydrogen group double-membrane sewage ultimate denitrification and carbon reduction method

Abstract

The invention discloses an oxygen group-hydrogen group double-membrane sewage ultimate denitrification and carbon reduction system and method, belongs to the field of sewage treatment, and particularly relates to an oxygen group-hydrogen group double-membrane sewage denitrification and carbon reduction system and method. The invention aims to solve the problems that the removal effect of total nitrogen in wastewater is poor due to the limitation of a carbon source under the condition of low carbon-nitrogen ratio in the traditional denitrification process, and the aeration bio-membrane reactor is difficult to realize stable and synchronous nitrification and denitrification. The oxygen group-hydrogen group double-membrane sewage ultimate denitrification and carbon reduction system consists of a membrane aeration biological membrane reaction system (MABR), a hydrogen group biological membrane reaction system (H2-MBfR) and a control system, and constructing an oxygen group-hydrogen group double-membrane system by using the hydrogen-based gas-permeable membrane reactor and the aeration bio-membrane reactor so as to realize deep removal of COD and TN in the wastewater with the low carbon-nitrogen ratio. The system disclosed by the invention can be formed by connecting an aeration biological membrane reaction system and a hydrogen-based biological membrane reaction system in series, can also be used for directly culturing oxygen-based and hydrogen-based biological membranes in one reaction system at the same time, and is suitable for different scenes.

Description

Technical Field

[0001] The invention belongs to the field of sewage treatment, and in particular relates to an oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system and method. Background Art

[0002] In the traditional activated sludge process of sewage denitrification, aerobic bacteria in the aerobic zone convert ammonia nitrogen into nitrate under aerobic conditions, and heterotrophic denitrifying bacteria in the anaerobic zone use organic matter in the sewage as a carbon source and energy to drive nitrate to be reduced to nitrogen (N2) to remove nitrogen from the sewage. However, in the low C / N sewage treatment process, additional carbon sources and energy are required to maintain denitrification. This process has problems such as high energy consumption, large sludge production, and easy impact on water quality and quantity. The membrane aerated biofilm reactor (MABR) is an efficient wastewater treatment system that integrates membrane separation technology and biofilm technology. Its main principle is to remove organic matter and nitrogen pollutants through the gas transfer characteristics and biodegradability of the membrane. The O2 inside the membrane cavity is quantitatively and accurately transported to the outer surface of the membrane under appropriate air pressure, realizing the supply of electron acceptors for microorganisms on demand. At the same time, wastewater pollutants penetrate from the surface of the biofilm to the inner layer, thus forming an efficient reverse diffusion mechanism that makes the theoretical oxygen utilization efficiency reach 100%. In addition, the membrane aeration method is conducive to the formation of a unique layered structure of the biofilm: the inner layer is an aerobic zone, which mainly carries out the oxidation and decomposition of organic matter and the nitrification reaction of ammonia nitrogen; the outer layer is an anoxic zone, where oxygen is limited, and the nitrification products are further converted into nitrogen gas emissions through denitrification, thereby achieving efficient removal of organic matter and nitrogen. Therefore, compared with traditional biofilm wastewater treatment technologies, such as moving bed biofilm reactors (MBBRs), MABRs have the advantages of high oxygen mass transfer efficiency and utilization, good ammonia nitrogen removal effect, small footprint, and low energy consumption. Different from traditional membrane bioreactors (MBRs) that mainly filter muddy water, this design method does not cause membrane pollution because of the use of a breathable membrane to diffuse gas from the inside of the membrane to the outside of the membrane for biofilm utilization. However, when MABR treats low-carbon and nitrogen wastewater, the nitrate concentration in the effluent is often high due to carbon source limitations, and thus it is impossible to achieve a more ideal complete denitrification.

[0003] Some existing processes generally adopt coupling processes to couple MABR with other denitrification processes to achieve efficient denitrification, but there are various barriers in actual engineering applications. For example, the HN-AD bacteria-Chlorella symbiotic system disclosed in CN118084210A strengthens the MABR method for treating biogas slurry, and couples Chlorella and denitrification functional bacteria to construct an oxygen circulation MABR of the bacteria-algae symbiotic system to achieve efficient removal of ammonia nitrogen, total nitrogen and total phosphorus. However, the optimal COD / TN of this system is 8, and the carbon-nitrogen ratio of the influent is relatively high, so it is not suitable for wastewater with a low carbon-nitrogen ratio.

[0004] Patent CN114751516A discloses a method for simultaneous denitrification and carbon removal of low carbon-nitrogen ratio sewage, which couples a membrane bioreactor (MBR) and a hydrogen matrix biofilm reactor (MBfR). In the MBR, ammonia nitrogen is mainly converted into nitrate nitrogen and nitrite nitrogen, and the subsequent MBfR converts nitrate nitrogen and nitrite nitrogen into nitrogen gas. However, there are the following barriers: 1) The nitrification in the MBR section mainly uses the activated sludge method, and the oxygen mass transfer and utilization efficiency are low; 2) The carbon-nitrogen ratio of sewage that can be treated during operation is 3.3-8.5, and only when the carbon-nitrogen ratio is higher than 5 can a high ammonia nitrogen removal rate be guaranteed, and deep denitrification and carbon removal under lower carbon-nitrogen ratio conditions cannot be achieved; (3) The system has the problem of MBR membrane pollution during long-term operation.

[0005] Patent CN118878088A discloses a method for treating sewage by using a membrane aerated biofilm reactor based on iron autotrophic coupled denitrification, which converts ammonia nitrogen in the influent into nitrate nitrogen through oxidation by aerobic microorganisms in the membrane aerated biofilm, and then converts nitrate nitrogen and unoxidized ammonia nitrogen into nitrogen gas through the action of iron-trophic denitrifying bacteria. Although this system can achieve good denitrification efficiency at a low C / N ratio, a large amount of suspended sludge is still required in the normal operation of MABR to cultivate iron-trophic denitrifying bacteria, and there are higher requirements for subsequent mud-water separation; and the growth cycle of iron-trophic denitrifying bacteria is about 50 days, which is not conducive to rapid startup during the startup phase or when it is affected by greater environmental conditions.

[0006] The integrated sewage denitrification system and method of sulfur-based fiber carrier coupled with membrane aeration biofilm reactor disclosed in patent CN118851429A converts nitrate nitrogen and nitrite nitrogen treated by membrane aeration biofilm reactor into nitrogen gas by cultivating sulfur autotrophic denitrifying bacteria. Although the system can achieve good denitrification efficiency at low C / N ratio, it has the problem of high cost of obtaining electron donor sulfur resources and the need for secondary treatment of the generated sulfate. Summary of the invention

[0007] The purpose of the present invention is to solve the problem that the traditional denitrification process has poor total nitrogen removal effect in wastewater due to carbon source limitation under low carbon-nitrogen ratio conditions, and it is difficult for an aerated biofilm reactor to achieve stable simultaneous nitrification and denitrification. A new oxygen-hydrogen-based double-membrane sewage extreme denitrification and carbon reduction system and method are provided, and an oxygen-hydrogen-based double-membrane system is constructed by a hydrogen-based breathable membrane reactor (H2-MBfR) and an aerated biofilm reactor (MABR), thereby achieving deep removal of COD and TN in wastewater. The system of the present invention can be a series connection of an aerated biofilm reaction system and a hydrogen-based biofilm reaction system, or oxygen-based and hydrogen-based biofilms can be directly cultured simultaneously in one reaction system, which is suitable for different scenarios.

[0008] The oxygen-hydrogen-based double membrane sewage extreme denitrification and carbon reduction system of the present invention is composed of a membrane aeration biofilm reactor system (MABR), a hydrogen-based biofilm reactor system (H2-MBfR) and a control system;

[0009] The membrane aeration biofilm reaction system is composed of a membrane aeration biofilm reaction tank (1), a water inlet system and an oxygen-based aeration membrane system;

[0010] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a membrane aeration biofilm reaction tank (1); the air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; the oxygen-based aeration membrane assembly (6) is a hollow fiber membrane assembly; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6); the hydrogen-based biofilm reaction system is composed of a hydrogen-based biofilm reaction tank (2), a hydrogen-based aeration membrane system and a drainage system; the hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a hydrogen-based biofilm reaction tank (2), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas delivery pipeline; the hydrogen-based aeration membrane assembly (16) is a hollow fiber membrane assembly; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are arranged on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0011] The water outlet of the membrane aerated biofilm reaction tank (1) is connected to the water inlet of the hydrogen-based biofilm reaction tank (2), and the water outlet of the membrane aerated biofilm reaction tank (1) is arranged at a height higher than the water inlet of the hydrogen-based biofilm reaction tank (2); water treated by the membrane aerated biofilm reaction system directly enters the hydrogen-based biofilm reaction system through overflow;

[0012] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10), a second dissolved oxygen sensor (14), a second pH sensor (15) and an electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) are arranged in a membrane aeration biofilm reaction tank (1); the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are arranged in a hydrogen-based biofilm reaction tank (2); the first dissolved oxygen sensor (5), the first pH sensor (7), the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are respectively connected to the electric control box (12).

[0013] The method for treating sewage using the above oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out according to the following steps:

[0014] 1. Sewage is introduced into the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2), oxygen or air is introduced into the membrane aerated biofilm reaction tank (1), hydrogen is introduced into the hydrogen-based biofilm reaction tank (2), sludge in the aerobic tank of the municipal sewage treatment plant is inoculated into the membrane aerated biofilm reaction tank (1), and sludge in the anaerobic tank of the municipal sewage treatment plant is inoculated into the hydrogen-based biofilm reaction tank (2); batch operation is performed for 7 to 10 days at an O2 partial pressure of 5-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent of the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is not more than 60 mg / L, and the TN of the effluent is not more than 5 mg / L, COD degrading bacteria and nitrifying bacteria are cultured in the membrane aerated biofilm reaction tank (1), and hydrogen autotrophic denitrifying bacteria are cultured in the hydrogen-based biofilm reaction tank (2);

[0015] The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L;

[0016] 2. The membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) are adjusted to continuous flow operation, until the ammonia nitrogen concentration of the effluent of the membrane aerated biofilm reaction tank (1) is ≤1 mg / L, and the nitrate nitrogen and nitrite nitrogen concentrations of the effluent of the hydrogen-based biofilm reaction tank (2) are ≤1 mg / L; at this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the membrane aerated biofilm reaction system and the hydrogen-based biofilm reaction system are started up;

[0017] 3. Connecting the water outlet of the membrane aerated biofilm reaction tank (1) to the water inlet of the hydrogen-based biofilm reaction tank (2), transporting the water treated by the membrane aerated biofilm reaction system to the hydrogen-based biofilm reaction system, and continuously introducing sewage into the membrane aerated biofilm reaction tank (1) to achieve continuous sewage treatment;

[0018] The hydraulic retention time of the sewage continuous treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi.

[0019] Compared with the prior art, the present invention has the following advantages:

[0020] 1. The aerated biofilm reaction system in the present invention can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. The present invention realizes green, efficient and complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantage of needing to supplement a large amount of carbon source when treating low C / N sewage in the past is avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment by the present invention, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0021] 2. The present invention couples the aerated biofilm reaction system with the hydrogen-based biofilm reaction system, achieving rapid supply of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0022] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of the present invention can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, thereby ensuring the stable operation of wastewater treatment.

[0023] Another oxygen-hydrogen-based double membrane sewage extreme denitrification and carbon reduction system of the present invention is composed of a reaction tank (18), an oxygen-based aeration membrane system, a hydrogen-based aeration membrane system, a water inlet system, a drainage system and a control system;

[0024] The drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage port provided at the bottom of the reaction tank (18) through the drainage pipeline; the water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet end of the water supply pump (3) is connected to the water inlet provided at the bottom of the reaction tank (18) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the reaction tank (18);

[0025] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6). The oxygen-based aeration membrane assembly (6) is arranged in a reaction tank (18). The air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline. A gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6). The gas electric regulating valve (13) can adjust the gas supply rate to save energy. In actual operation, a dense biofilm grows on the surface of the oxygen-based aeration membrane assembly (6), forming a "double membrane" structure consisting of a hollow fiber membrane and a biofilm.

[0026] The hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a reaction tank (18), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) via a gas delivery pipeline;

[0027] The oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16) are hollow fiber membrane assemblies; the hollow fiber membrane assembly is made of polyether ketone, polypropylene or polyurethane; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are provided on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0028] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10) and an electric control box (12); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are arranged in a reaction tank (18); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are connected to the electric control box (12) respectively; the first dissolved oxygen sensor (5) and the first pH sensor (7) can monitor the dissolved oxygen and pH in the water of the reaction tank (18) in real time, and the hydrogen sensor (10) can monitor the hydrogen concentration in the reaction tank (18) in real time. , making hydrogen self-oxygen denitrification more efficient and further improving the treatment efficiency of pollutants; the first dissolved oxygen sensor (5) monitors the dissolved oxygen concentration in the water phase in the reaction tank (18), and adjusts the amount of dissolved oxygen entering the inner cavity of the oxygen-based aeration membrane component (6) through the gas electric regulating valve (13), thereby achieving precise control of the amount of oxygen required for converting ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen; the hydrogen sensor (10) monitors the gaseous hydrogen concentration in the water phase, and then adjusts the amount of hydrogen entering the inner cavity of the hydrogen-based aeration membrane component (16) through the hydrogen pressure reducing table (8) and the hydrogen mass flow meter (17), thereby achieving precise control of the amount of hydrogen required for reducing nitrate nitrogen / nitrite nitrogen in the sewage into nitrogen.

[0029] The method for treating sewage using the above oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out according to the following steps:

[0030] 1. Sewage is introduced into the reaction tank (18), oxygen or air is introduced into the reaction tank (18) by using an aeration pump (4), hydrogen is introduced into the reaction tank (18) by using a hydrogen generator (11), sludge from the secondary sedimentation tank of a municipal sewage treatment plant is inoculated into the reaction tank (18), and batch operation is performed for 7 to 10 days at an O2 partial pressure of 2-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent from the reaction tank (18) is not more than 60 mg / L and the TN of the effluent is not more than 5 mg / L, and COD-degrading bacteria, nitrifying bacteria and hydrogen-autotrophic denitrifying bacteria are cultivated in the reaction tank (18);

[0031] The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L;

[0032] 2. The reaction tank (18) is adjusted to operate in a continuous flow mode until the concentrations of ammonia nitrogen, nitrate nitrogen and nitrite nitrogen in the effluent of the reaction tank (18) are all less than 1 mg / L. At this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the system is started;

[0033] 3. Continuously introducing sewage into the reaction tank (18) to achieve continuous sewage treatment;

[0034] The hydraulic retention time of the continuous sewage treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi;

[0035] Compared with the prior art, the present invention has the following advantages:

[0036] 1. The aerated biofilm reaction system in the present invention can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. The present invention realizes green, efficient and complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantage of needing to supplement a large amount of carbon source when treating low C / N sewage in the past is avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment by the present invention, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0037] 2. The present invention couples the oxygen-based aeration membrane system and the hydrogen-based aeration membrane system, achieving rapid permeation of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0038] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of the present invention can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, thereby ensuring the stable operation of wastewater treatment. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 This is a schematic diagram of the structure of the oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system (in series).

[0040] Figure 2 This is a schematic diagram of the structure of the oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system (parallel). DETAILED DESCRIPTION

[0041] The technical solution of the present invention is not limited to the specific implementation modes listed below, but also includes any reasonable combination of the specific implementation modes.

[0042] Specific implementation method 1: The oxygen-hydrogen-based double membrane sewage extreme nitrogen removal and carbon reduction system in this implementation method is composed of a membrane aerated biofilm reactor system (MABR), a hydrogen-based biofilm reactor system (H2-MBfR) and a control system;

[0043] The membrane aeration biofilm reaction system is composed of a membrane aeration biofilm reaction tank (1), a water inlet system and an oxygen-based aeration membrane system;

[0044] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a membrane aeration biofilm reaction tank (1); the air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; the oxygen-based aeration membrane assembly (6) is a hollow fiber membrane assembly; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6); the hydrogen-based biofilm reaction system is composed of a hydrogen-based biofilm reaction tank (2), a hydrogen-based aeration membrane system and a drainage system; the hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a hydrogen-based biofilm reaction tank (2), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas delivery pipeline; the hydrogen-based aeration membrane assembly (16) is a hollow fiber membrane assembly; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are arranged on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0045] The water outlet of the membrane aerated biofilm reaction tank (1) is connected to the water inlet of the hydrogen-based biofilm reaction tank (2), and the water outlet of the membrane aerated biofilm reaction tank (1) is arranged at a height higher than the water inlet of the hydrogen-based biofilm reaction tank (2); water treated by the membrane aerated biofilm reaction system directly enters the hydrogen-based biofilm reaction system through overflow;

[0046] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10), a second dissolved oxygen sensor (14), a second pH sensor (15) and an electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) are arranged in a membrane aeration biofilm reaction tank (1); the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are arranged in a hydrogen-based biofilm reaction tank (2); the first dissolved oxygen sensor (5), the first pH sensor (7), the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are respectively connected to the electric control box (12).

[0047] 1. In this embodiment, the aerated biofilm reaction system can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen gas, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. This embodiment realizes green and efficient complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantages of the need to supplement a large amount of carbon source when treating low C / N sewage in the past are avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment in this embodiment, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0048] 2. This embodiment couples the aerated biofilm reaction system and the hydrogen-based biofilm reaction system, achieving rapid supply of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0049] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of this embodiment can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, ensuring the stable operation of wastewater treatment.

[0050] Specific embodiment 2: This embodiment differs from specific embodiment 1 in that: the water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet end of the water supply pump (3) is connected to the water inlet arranged at the bottom of the membrane aerated biofilm reaction tank (1) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the membrane aerated biofilm reaction tank (1).

[0051] Specific embodiment three: This embodiment differs from specific embodiment one in that the drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage outlet arranged on the upper part of the hydrogen-based biofilm reaction tank (2) through the drainage pipeline.

[0052] Specific embodiment 4: This embodiment is different from specific embodiment 1 in that the material of the hollow fiber membrane component is polyether ketone, polypropylene or polyurethane.

[0053] Specific embodiment 5: In this embodiment, the method for treating sewage using an oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out according to the following steps:

[0054] 1. Sewage is introduced into the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2), oxygen or air is introduced into the membrane aerated biofilm reaction tank (1), hydrogen is introduced into the hydrogen-based biofilm reaction tank (2), sludge in the aerobic tank of the municipal sewage treatment plant is inoculated into the membrane aerated biofilm reaction tank (1), and sludge in the anaerobic tank of the municipal sewage treatment plant is inoculated into the hydrogen-based biofilm reaction tank (2); batch operation is performed for 7 to 10 days at an O2 partial pressure of 5-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent of the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is not more than 60 mg / L, and the TN of the effluent is not more than 5 mg / L, COD degrading bacteria and nitrifying bacteria are cultured in the membrane aerated biofilm reaction tank (1), and hydrogen autotrophic denitrifying bacteria are cultured in the hydrogen-based biofilm reaction tank (2);

[0055] The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L;

[0056] 2. The membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) are adjusted to continuous flow operation, until the ammonia nitrogen concentration of the effluent of the membrane aerated biofilm reaction tank (1) is ≤1 mg / L, and the nitrate nitrogen and nitrite nitrogen concentrations of the effluent of the hydrogen-based biofilm reaction tank (2) are ≤1 mg / L; at this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the membrane aerated biofilm reaction system and the hydrogen-based biofilm reaction system are started up;

[0057] 3. Connecting the water outlet of the membrane aerated biofilm reaction tank (1) to the water inlet of the hydrogen-based biofilm reaction tank (2), transporting the water treated by the membrane aerated biofilm reaction system to the hydrogen-based biofilm reaction system, and continuously introducing sewage into the membrane aerated biofilm reaction tank (1) to achieve continuous sewage treatment;

[0058] The hydraulic retention time of the sewage continuous treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi.

[0059] 1. In this embodiment, the aerated biofilm reaction system can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen gas, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. This embodiment realizes green and efficient complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantages of the need to supplement a large amount of carbon source when treating low C / N sewage in the past are avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment in this embodiment, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0060] 2. This embodiment couples the aerated biofilm reaction system and the hydrogen-based biofilm reaction system, achieving rapid supply of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0061] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of this embodiment can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, ensuring the stable operation of wastewater treatment.

[0062] Specific embodiment 6: The oxygen-hydrogen-based double membrane sewage extreme denitrification and carbon reduction system in this embodiment is composed of a reaction tank (18), an oxygen-based aeration membrane system, a hydrogen-based aeration membrane system, a water inlet system, a drainage system and a control system;

[0063] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a reaction tank (18); the gas outlet of the aeration pump (4) is connected to the gas inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the gas outlet of the aeration pump (4) and the gas inlet of the oxygen-based aeration membrane assembly (6);

[0064] The hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a reaction tank (18), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas delivery pipeline; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are arranged on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0065] The oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16) are hollow fiber membrane assemblies;

[0066] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10) and an electric control box (12); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are arranged in a reaction tank (18); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are respectively connected to the electric control box (12).

[0067] 1. In this embodiment, the aerated biofilm reaction system can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen gas, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. This embodiment realizes green and efficient complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantages of the need to supplement a large amount of carbon source when treating low C / N sewage in the past are avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment in this embodiment, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0068] 2. This embodiment couples the oxygen-based aeration membrane system and the hydrogen-based aeration membrane system, achieving rapid permeation of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0069] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of this embodiment can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, ensuring the stable operation of wastewater treatment.

[0070] Specific implementation method 7: This implementation method is different from specific implementation method 6 in that the material of the hollow fiber membrane component is polyether ketone, polypropylene or polyurethane.

[0071] Specific embodiment eight: This embodiment differs from specific embodiment six in that the drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage port provided at the bottom of the reaction tank (18) through the drainage pipeline.

[0072] Specific embodiment nine: This embodiment differs from specific embodiment six in that: the water inlet system is composed of a water supply pump (3) and a water inlet pipeline, the water outlet of the water supply pump (3) is connected to the water inlet arranged at the bottom of the reaction tank (18) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the reaction tank (18).

[0073] Specific embodiment 10: In this embodiment, the method for treating sewage using the above oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out according to the following steps:

[0074] 1. Sewage is introduced into the reaction tank (18), oxygen or air is introduced into the reaction tank (18) by using an aeration pump (4), hydrogen is introduced into the reaction tank (18) by using a hydrogen generator (11), sludge from the secondary sedimentation tank of a municipal sewage treatment plant is inoculated into the reaction tank (18), and batch operation is performed for 7 to 10 days at an O2 partial pressure of 5-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent from the reaction tank (18) is not more than 60 mg / L and the TN of the effluent is not more than 5 mg / L, and COD-degrading bacteria, nitrifying bacteria and hydrogen-autotrophic denitrifying bacteria are cultivated in the reaction tank (18);

[0075] The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L;

[0076] 2. The reaction tank (18) is adjusted to operate in a continuous flow mode until the concentrations of ammonia nitrogen, nitrate nitrogen and nitrite nitrogen in the effluent of the reaction tank (18) are all less than 1 mg / L. At this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the system is started;

[0077] 3. Continuously introducing sewage into the reaction tank (18) to achieve continuous sewage treatment;

[0078] The hydraulic retention time of the sewage continuous treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi.

[0079] 1. In this embodiment, the aerated biofilm reaction system can quickly oxidize ammonia nitrogen into nitrate nitrogen and nitrite nitrogen, and the hydrogen-based biofilm reaction system can use hydrogen as the only electron donor to efficiently reduce the remaining nitrate nitrogen / nitrite nitrogen in the effluent to nitrogen gas, and no additional organic carbon source is required in the whole process, thereby realizing the organic combination of nitrification, heterotrophic denitrification and hydrogen autotrophic denitrification, thereby realizing efficient denitrification under low C / N conditions. This embodiment realizes green and efficient complete denitrification under extremely low carbon-nitrogen ratio conditions. By using hydrogen and oxygen as electron donors, the disadvantages of the need to supplement a large amount of carbon source when treating low C / N sewage in the past are avoided, the denitrification cost of low C / N sewage is reduced, and the risk of secondary environmental pollution is also reduced. After treatment in this embodiment, the effluent COD and TN are reduced to below 30 mg / L and 2.0 mg / L respectively, meeting the Class V surface water standard.

[0080] 2. This embodiment couples the oxygen-based aeration membrane system and the hydrogen-based aeration membrane system, achieving rapid permeation of hydrogen and oxygen through the membrane to the biofilm on the membrane surface, with gas mass transfer and utilization rates approaching 100%. Compared with other existing coupling processes, the gas transmission efficiency is high and the cost is lower.

[0081] 3. Compared with the traditional MBR system, the aerated biofilm reaction system and the hydrogen-based biofilm reaction system of this embodiment can achieve rapid and efficient oxygen supply while avoiding membrane pollution problems, ensuring the stable operation of wastewater treatment.

[0082] Example 1

[0083] Combination Figure 1 This embodiment is described. The oxygen-hydrogen-based double membrane sewage extreme nitrogen removal and carbon reduction system of this embodiment is composed of a membrane aerated biofilm reactor system (MABR), a hydrogen-based biofilm reactor system (H2-MBfR) and a control system;

[0084] The membrane aeration biofilm reaction system is composed of a membrane aeration biofilm reaction tank (1), a water inlet system and an oxygen-based aeration membrane system;

[0085] The water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet of the water supply pump (3) is connected to the water inlet provided at the bottom of the membrane aerated biofilm reaction tank (1) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the membrane aerated biofilm reaction tank (1);

[0086] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a membrane aeration biofilm reaction tank (1); the air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; the oxygen-based aeration membrane assembly (6) is a hollow fiber membrane assembly; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6); the gas electric regulating valve (13) can adjust the gas supply rate to save energy consumption; in actual operation, a layer of dense biofilm grows on the surface of the oxygen-based aeration membrane assembly (6), forming a "double membrane" structure composed of a hollow fiber membrane and a biofilm;

[0087] The hydrogen-based biofilm reaction system is composed of a hydrogen-based biofilm reaction tank (2), a hydrogen-based aeration membrane system and a drainage system; the drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage outlet arranged on the upper part of the hydrogen-based biofilm reaction tank (2) through the drainage pipeline; the hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in the hydrogen-based biofilm reaction tank (2), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas transmission pipeline; the hydrogen-based aeration membrane assembly (16) is a hollow fiber membrane assembly;

[0088] A hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are provided on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0089] The water outlet of the membrane aerated biofilm reaction tank (1) is connected to the water inlet of the hydrogen-based biofilm reaction tank (2), and the water outlet of the membrane aerated biofilm reaction tank (1) is arranged at a height higher than the water inlet of the hydrogen-based biofilm reaction tank (2); water treated by the membrane aerated biofilm reaction system directly enters the hydrogen-based biofilm reaction system through overflow;

[0090] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10), a second dissolved oxygen sensor (14), a second pH sensor (15) and an electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) are arranged in a membrane aeration biofilm reaction tank (1); the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are arranged in a hydrogen-based biofilm reaction tank (2); the first dissolved oxygen sensor (5), the first pH sensor (7), the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are respectively connected to the electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) can monitor the dissolved oxygen and pH in the water of the membrane aeration biofilm reaction tank (1) in real time, and the hydrogen sensor (10) can monitor the dissolved oxygen and pH in the water of the membrane aeration biofilm reaction tank (1) in real time. The first dissolved oxygen sensor (10), the second dissolved oxygen sensor (14), and the second pH sensor (15) can monitor the dissolved oxygen, pH, and hydrogen concentration in the water in the hydrogen-based biofilm reaction tank (2) in real time, so that hydrogen self-oxygen denitrification is more efficient and the pollutant treatment efficiency is further improved; the first dissolved oxygen sensor (5) monitors the dissolved oxygen concentration in the water phase in the membrane aeration biofilm reaction tank (1), and adjusts the amount of dissolved oxygen entering the inner cavity of the oxygen-based aeration membrane component (6) through the gas electric regulating valve (13), thereby achieving precise control of the amount of oxygen required for converting ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen; the hydrogen sensor (10) monitors the gaseous hydrogen concentration in the water phase, and then adjusts the amount of hydrogen entering the inner cavity of the hydrogen-based aeration membrane component (16) through the hydrogen pressure reducing table (8) and the hydrogen mass flow meter (17), thereby achieving precise control of the amount of hydrogen required for reducing nitrate nitrogen / nitrite nitrogen in the sewage into nitrogen.

[0091] The hollow fiber membrane components are made of polyurethane;

[0092] The method for treating sewage using an oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out in the following steps:

[0093] 1. Sewage is introduced into the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2), air is introduced into the membrane aerated biofilm reaction tank (1), hydrogen is introduced into the hydrogen-based biofilm reaction tank (2), sludge (3000-5000 mg / L) from the aerobic tank of the municipal sewage treatment plant is inoculated into the membrane aerated biofilm reaction tank (1), and sludge from the anaerobic tank of the municipal sewage treatment plant is inoculated into the hydrogen-based biofilm reaction tank (2); batch operation is performed for 9 days at an O2 partial pressure of 3 psi and a H2 partial pressure of 10 psi until the COD of the effluent of the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is not more than 60 mg / L, and the TN of the effluent is not more than 5 mg / L, COD degrading bacteria and nitrifying bacteria are cultured in the membrane aerated biofilm reaction tank (1), and hydrogen autotrophic denitrifying bacteria are cultured in the hydrogen-based biofilm reaction tank (2);

[0094] The sewage is domestic sewage; the carbon-nitrogen ratio of the sewage is 1.7-3.0:1, the ammonia nitrogen concentration is 40-60 mg-N / L; COD: 100-120 mg / L;

[0095] 2. The membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) are adjusted to continuous flow operation for 2 weeks, the hydraulic retention time in the membrane aerated biofilm reaction tank (1) is gradually reduced from 24 hours to 12 hours, the ammonia nitrogen concentration of the effluent of the membrane aerated biofilm reaction tank (1) is ≤1 mg / L, and the nitrate nitrogen and nitrite nitrogen concentrations of the effluent of the hydrogen-based biofilm reaction tank (2) are ≤0.5 mg / L; at this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the membrane aerated biofilm reaction system and the hydrogen-based biofilm reaction system are started up;

[0096] 3. Connecting the water outlet of the membrane aerated biofilm reaction tank (1) to the water inlet of the hydrogen-based biofilm reaction tank (2), transporting the water treated by the membrane aerated biofilm reaction system to the hydrogen-based biofilm reaction system, and continuously introducing sewage into the membrane aerated biofilm reaction tank (1) to achieve continuous sewage treatment;

[0097] The hydraulic retention time of the sewage continuous treatment is 6h, the O2 partial pressure is 3psi, and the H2 partial pressure is 5psi;

[0098] The aeration flushing cycle of the membrane components in the membrane aeration biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is 60s / 30min, and the ambient temperature is 25-30°C.

[0099] The effluent concentration of the membrane aerated biofilm reactor (1) is shown in Table 1, and the effluent concentration of the hydrogen-based biofilm reactor (2) is shown in Table 2.

[0100] Table 1

[0101] Serial number index Influent (mg / L) MABR effluent (mg / L) 1 COD 100～120 27～30 2 <![CDATA[NH4 + -N]]> 40～60 0 3 <![CDATA[NO3 - -N]]> 2～3 15～28 4 <![CDATA[NO2 - -N]]> 0～1 1～2

[0102] Table 2

[0103] Serial number index Influent (mg / L) H2-MBfR effluent (mg / L) 1 COD 27～30 25～30 2 <![CDATA[NH4 + -N]]> 0 0 3 <![CDATA[NO3 - -N]]> 15～28 ≤0.5 4 <![CDATA[NO2 - -N]]> 0～1 0 5 TN 15～30 ≤1.0

[0104] It can be seen from the concentration of various forms of nitrogen in the effluent that the MABR and H2-MBfR in series can achieve rapid nitrification-denitrification, at which time the effluent COD concentration is ≤30mg / L and the effluent NH4 + -N concentration is close to 0mg / L, and effluent TN≤1.0mg / L, which meets the surface water Class IV standard.

[0105] Example 2

[0106] Combination Figure 1 To illustrate this embodiment, the oxygen-hydrogen-based double membrane sewage extreme denitrification and carbon reduction system of this embodiment is composed of a membrane aerated biofilm reactor system (MABR), a hydrogen-based biofilm reactor system (H2-MBfR) and a control system;

[0107] The membrane aeration biofilm reaction system is composed of a membrane aeration biofilm reaction tank (1), a water inlet system and an oxygen-based aeration membrane system;

[0108] The water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet of the water supply pump (3) is connected to the water inlet provided at the bottom of the membrane aerated biofilm reaction tank (1) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the membrane aerated biofilm reaction tank (1);

[0109] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a membrane aeration biofilm reaction tank (1); the air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; the oxygen-based aeration membrane assembly (6) is a hollow fiber membrane assembly; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6); the gas electric regulating valve (13) can adjust the gas supply rate to save energy consumption; in actual operation, a layer of dense biofilm grows on the surface of the oxygen-based aeration membrane assembly (6), forming a "double membrane" structure composed of a hollow fiber membrane and a biofilm;

[0110] The hydrogen-based biofilm reaction system is composed of a hydrogen-based biofilm reaction tank (2), a hydrogen-based aeration membrane system and a drainage system; the drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage outlet arranged on the upper part of the hydrogen-based biofilm reaction tank (2) through the drainage pipeline; the hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in the hydrogen-based biofilm reaction tank (2), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas transmission pipeline; the hydrogen-based aeration membrane assembly (16) is a hollow fiber membrane assembly;

[0111] A hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are provided on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0112] The water outlet of the membrane aerated biofilm reaction tank (1) is connected to the water inlet of the hydrogen-based biofilm reaction tank (2), and the water outlet of the membrane aerated biofilm reaction tank (1) is arranged at a height higher than the water inlet of the hydrogen-based biofilm reaction tank (2); water treated by the membrane aerated biofilm reaction system directly enters the hydrogen-based biofilm reaction system through overflow;

[0113] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10), a second dissolved oxygen sensor (14), a second pH sensor (15) and an electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) are arranged in a membrane aeration biofilm reaction tank (1); the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are arranged in a hydrogen-based biofilm reaction tank (2); the first dissolved oxygen sensor (5), the first pH sensor (7), the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are respectively connected to the electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) can monitor the dissolved oxygen and pH in the water of the membrane aeration biofilm reaction tank (1) in real time, and the hydrogen sensor (10) can monitor the dissolved oxygen and pH in the water of the membrane aeration biofilm reaction tank (1) in real time. The first dissolved oxygen sensor (10), the second dissolved oxygen sensor (14), and the second pH sensor (15) can monitor the dissolved oxygen, pH, and hydrogen concentration in the water in the hydrogen-based biofilm reaction tank (2) in real time, so that hydrogen self-oxygen denitrification is more efficient and the pollutant treatment efficiency is further improved; the first dissolved oxygen sensor (5) monitors the dissolved oxygen concentration in the water phase in the membrane aeration biofilm reaction tank (1), and adjusts the amount of dissolved oxygen entering the inner cavity of the oxygen-based aeration membrane component (6) through the gas electric regulating valve (13), thereby achieving precise control of the amount of oxygen required for converting ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen; the hydrogen sensor (10) monitors the gaseous hydrogen concentration in the water phase, and then adjusts the amount of hydrogen entering the inner cavity of the hydrogen-based aeration membrane component (16) through the hydrogen pressure reducing table (8) and the hydrogen mass flow meter (17), thereby achieving precise control of the amount of hydrogen required for reducing nitrate nitrogen / nitrite nitrogen in the sewage into nitrogen.

[0114] The hollow fiber membrane components are made of polyurethane;

[0115] The method for treating sewage using an oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out in the following steps:

[0116] 1. Sewage is introduced into the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2), air is introduced into the membrane aerated biofilm reaction tank (1), hydrogen is introduced into the hydrogen-based biofilm reaction tank (2), sludge (3000-5000 mg / L) from the aerobic tank of the municipal sewage treatment plant is inoculated into the membrane aerated biofilm reaction tank (1), and sludge from the anaerobic tank of the municipal sewage treatment plant is inoculated into the hydrogen-based biofilm reaction tank (2); batch operation is performed for 9 days at an O2 partial pressure of 3 psi and a H2 partial pressure of 10 psi until the COD of the effluent of the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is not more than 60 mg / L, and the TN of the effluent is not more than 5 mg / L, COD degrading bacteria and nitrifying bacteria are cultured in the membrane aerated biofilm reaction tank (1), and hydrogen autotrophic denitrifying bacteria are cultured in the hydrogen-based biofilm reaction tank (2);

[0117] The sewage is domestic sewage; the carbon-nitrogen ratio of the sewage is 0.8-1.1:1, the ammonia nitrogen concentration is 90-100 mg-N / L; COD: 80-100 mg / L;

[0118] 2. The membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) are adjusted to continuous flow operation for 2 weeks, the hydraulic retention time in the membrane aerated biofilm reaction tank (1) is gradually reduced from 24 hours to 12 hours, the ammonia nitrogen concentration of the effluent of the membrane aerated biofilm reaction tank (1) is ≤1 mg / L, and the nitrate nitrogen and nitrite nitrogen concentrations of the effluent of the hydrogen-based biofilm reaction tank (2) are ≤0.5 mg / L; at this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the membrane aerated biofilm reaction system and the hydrogen-based biofilm reaction system are started up;

[0119] 3. Connecting the water outlet of the membrane aerated biofilm reaction tank (1) to the water inlet of the hydrogen-based biofilm reaction tank (2), transporting the water treated by the membrane aerated biofilm reaction system to the hydrogen-based biofilm reaction system, and continuously introducing sewage into the membrane aerated biofilm reaction tank (1) to achieve continuous sewage treatment;

[0120] The hydraulic retention time of the sewage continuous treatment is 8h, the O2 partial pressure is 5psi, and the H2 partial pressure is 10psi;

[0121] The aeration flushing cycle of the membrane components in the membrane aeration biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is 60s / 30min, and the ambient temperature is 25-30°C.

[0122] The effluent concentration of the membrane aerated biofilm reactor (1) is shown in Table 3, and the effluent concentration of the hydrogen-based biofilm reactor (2) is shown in Table 4.

[0123] Table 3

[0124] Serial number index Influent (mg / L) MABR effluent (mg / L) 1 COD 80～100 25～30 2 <![CDATA[NH4 + -N]]> 90～100 0.5～1.0 3 <![CDATA[NO3 - -N]]> 2～3 80～85 4 <![CDATA[NO2 - -N]]> 0～1 3～4

[0125] Table 4

[0126]

[0127]

[0128] It can be seen from the concentration of various forms of nitrogen in the effluent that the MABR and H2-MBfR in series can achieve rapid nitrification-denitrification, at which time the effluent COD concentration is ≤30mg / L and the effluent NH4 + -N concentration is 0.5~1.0mg / L, and effluent TN≤2.0mg / L, which can meet the surface water Class V standard.

[0129] Example 3

[0130] Combination Figure 2 This embodiment is described. The oxygen-hydrogen-based double membrane sewage extreme denitrification and carbon reduction system of this embodiment is composed of a reaction tank (18), an oxygen-based aeration membrane system, a hydrogen-based aeration membrane system, a water inlet system, a drainage system and a control system;

[0131] The drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to the drainage port provided at the bottom of the reaction tank (18) through the drainage pipeline; the water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet end of the water supply pump (3) is connected to the water inlet provided at the bottom of the reaction tank (18) through the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the reaction tank (18);

[0132] The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6). The oxygen-based aeration membrane assembly (6) is arranged in a reaction tank (18). The air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline. A gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6). The gas electric regulating valve (13) can adjust the gas supply rate to save energy. In actual operation, a dense biofilm grows on the surface of the oxygen-based aeration membrane assembly (6), forming a "double membrane" structure consisting of a hollow fiber membrane and a biofilm.

[0133] The hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a reaction tank (18), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) via a gas delivery pipeline;

[0134] The oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16) are hollow fiber membrane assemblies; the hollow fiber membrane assembly is made of polyurethane; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are provided on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16);

[0135] The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10) and an electric control box (12); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are arranged in a reaction tank (18); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are connected to the electric control box (12) respectively; the first dissolved oxygen sensor (5) and the first pH sensor (7) can monitor the dissolved oxygen and pH in the water of the reaction tank (18) in real time, and the hydrogen sensor (10) can monitor the hydrogen concentration in the reaction tank (18) in real time. , making hydrogen self-oxygen denitrification more efficient and further improving the treatment efficiency of pollutants; the first dissolved oxygen sensor (5) monitors the dissolved oxygen concentration in the water phase in the reaction tank (18), and adjusts the amount of dissolved oxygen entering the inner cavity of the oxygen-based aeration membrane component (6) through the gas electric regulating valve (13), thereby achieving precise control of the amount of oxygen required for converting ammonia nitrogen in the sewage into nitrate nitrogen and nitrite nitrogen; the hydrogen sensor (10) monitors the gaseous hydrogen concentration in the water phase, and then adjusts the amount of hydrogen entering the inner cavity of the hydrogen-based aeration membrane component (16) through the hydrogen pressure reducing table (8) and the hydrogen mass flow meter (17), thereby achieving precise control of the amount of hydrogen required for reducing nitrate nitrogen / nitrite nitrogen in the sewage into nitrogen.

[0136] The method for treating sewage using an oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system is carried out in the following steps:

[0137] 1. Sewage is introduced into the reaction tank (18), air is introduced into the reaction tank (18) by using an aeration pump (4), hydrogen is introduced into the reaction tank (18) by using a hydrogen generator (11), sludge (3000-5000 mg / L) from the secondary sedimentation tank of a municipal sewage treatment plant is inoculated into the reaction tank (18), and batch operation is performed for 10 days at an O2 partial pressure of 3 psi and a H2 partial pressure of 3 psi until the COD of the effluent from the reaction tank (18) is not more than 60 mg / L and the TN of the effluent is not more than 5 mg / L, and COD-degrading bacteria, nitrifying bacteria and hydrogen-autotrophic denitrifying bacteria are cultivated in the reaction tank (18);

[0138] The sewage is domestic sewage configured in the laboratory; the carbon-nitrogen ratio of the sewage is 0.05-0.1:1, the ammonia nitrogen concentration is 180-200 mg-N / L; COD: 15-20 mg / L;

[0139] 2. The reaction tank (18) is adjusted to operate in continuous flow for 2 weeks, and the hydraulic retention time in the reaction tank (18) is gradually reduced from 24 hours to 12 hours, until the concentrations of ammonia nitrogen, nitrate nitrogen and nitrite nitrogen in the effluent of the reaction tank (18) are all less than 0.5 mg / L. At this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the system is started;

[0140] 3. Continuously introducing sewage into the reaction tank (18) to achieve continuous sewage treatment;

[0141] The hydraulic retention time of the continuous sewage treatment is 10h, the O2 partial pressure is 7psi, and the H2 partial pressure is 15psi; the aeration flushing cycle of the membrane module is 60s / 30min, and the effluent concentration of the reaction tank (18) is shown in Table 5;

[0142] Table 5

[0143] Serial number index Influent (mg / L) Outlet water (mg / L) 1 COD 20～25 10～15 2 <![CDATA[NH4 + -N]]> 180～200 0.5～1.0 3 <![CDATA[NO3 - -N]]> 0 ≤0.5 4 <![CDATA[NO2 - -N]]> 0 ≤0.5 5 TN 180～200 ≤2.0

[0144] It can be seen from the concentration of various forms of nitrogen in the effluent that the parallel connection of MABR and H2-MBfR can achieve rapid nitrification-denitrification, at which time the effluent COD concentration is ≤30mg / L and the effluent NH4 + -N concentration is 0.5~1.0mg / L, and effluent TN≤2.0mg / L, which can meet Class V surface water standards.

Claims

1. An oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system, characterized by: The oxygen-hydrogen-based double membrane wastewater extreme nitrogen removal and carbon reduction system consists of a membrane aerated biofilm reactor system (MABR), a hydrogen-based biofilm reactor system (H2-MBfR) and a control system; The membrane aeration biofilm reaction system is composed of a membrane aeration biofilm reaction tank (1), a water inlet system and an oxygen-based aeration membrane system; The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a membrane aeration biofilm reaction tank (1); the air outlet of the aeration pump (4) is connected to the air inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; the oxygen-based aeration membrane assembly (6) is a hollow fiber membrane assembly; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the air outlet of the aeration pump (4) and the air inlet of the oxygen-based aeration membrane assembly (6); the hydrogen-based biofilm reaction system is composed of a hydrogen-based biofilm reaction tank (2), a hydrogen-based aeration membrane system and a drainage system; the hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a hydrogen-based biofilm reaction tank (2), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas delivery pipeline; the hydrogen-based aeration membrane assembly (16) is a hollow fiber membrane assembly; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are arranged on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16); The water outlet of the membrane aerated biofilm reaction tank (1) is connected to the water inlet of the hydrogen-based biofilm reaction tank (2), and the water outlet of the membrane aerated biofilm reaction tank (1) is arranged at a height higher than the water inlet of the hydrogen-based biofilm reaction tank (2); water treated by the membrane aerated biofilm reaction system directly enters the hydrogen-based biofilm reaction system through overflow; The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10), a second dissolved oxygen sensor (14), a second pH sensor (15) and an electric control box (12); the first dissolved oxygen sensor (5) and the first pH sensor (7) are arranged in a membrane aeration biofilm reaction tank (1); the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are arranged in a hydrogen-based biofilm reaction tank (2); the first dissolved oxygen sensor (5), the first pH sensor (7), the hydrogen sensor (10), the second dissolved oxygen sensor (14) and the second pH sensor (15) are respectively connected to the electric control box (12).

2. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 1 is characterized in that: The water inlet system is composed of a water supply pump (3) and a water inlet pipeline, and the water outlet end of the water supply pump (3) is connected to the water inlet provided at the bottom of the membrane aerated biofilm reaction tank (1) through the water inlet pipeline; The water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the membrane aeration biofilm reaction tank (1).

3. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 1 is characterized in that: The drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to a drainage outlet arranged at the top of the hydrogen-based biofilm reaction tank (2) through the drainage pipeline.

4. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 1 is characterized in that: The hollow fiber membrane component is made of polyether ketone, polypropylene or polyurethane.

5. A method for treating sewage using the oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system as claimed in claim 1, characterized in that: The method proceeds as follows:

1. Sewage is introduced into the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2), respectively, oxygen or air is introduced into the membrane aerated biofilm reaction tank (1), hydrogen is introduced into the hydrogen-based biofilm reaction tank (2), and then the sludge in the aerobic tank of the municipal sewage treatment plant is inoculated into the membrane aerated biofilm reaction tank (1), and the sludge in the anaerobic tank of the municipal sewage treatment plant is inoculated into the hydrogen-based biofilm reaction tank (2); batch operation is performed for 7 to 10 days at an O2 partial pressure of 2-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent of the membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) is not more than 60 mg / L, and the TN of the effluent is not more than 5 mg / L, COD degrading bacteria and nitrifying bacteria are cultured in the membrane aerated biofilm reaction tank (1), and hydrogen autotrophic denitrifying bacteria are cultured in the hydrogen-based biofilm reaction tank (2); The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L; 2. The membrane aerated biofilm reaction tank (1) and the hydrogen-based biofilm reaction tank (2) are adjusted to continuous flow operation, until the ammonia nitrogen concentration of the effluent of the membrane aerated biofilm reaction tank (1) is ≤1 mg / L, and the nitrate nitrogen and nitrite nitrogen concentrations of the effluent of the hydrogen-based biofilm reaction tank (2) are ≤1 mg / L; at this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the membrane aerated biofilm reaction system and the hydrogen-based biofilm reaction system are started up; 3. Connecting the water outlet of the membrane aerated biofilm reaction tank (1) to the water inlet of the hydrogen-based biofilm reaction tank (2), transporting the water treated by the membrane aerated biofilm reaction system to the hydrogen-based biofilm reaction system, and continuously introducing sewage into the membrane aerated biofilm reaction tank (1) to achieve continuous sewage treatment; The hydraulic retention time of the sewage continuous treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi.

6. An oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system, characterized by: The oxygen-hydrogen-based double membrane wastewater extreme denitrification and carbon reduction system is composed of a reaction tank (18), an oxygen-based aeration membrane system, a hydrogen-based aeration membrane system, a water inlet system, a drainage system and a control system; The oxygen-based aeration membrane system is composed of an aeration pump (4) and an oxygen-based aeration membrane assembly (6); the oxygen-based aeration membrane assembly (6) is arranged in a reaction tank (18); the gas outlet of the aeration pump (4) is connected to the gas inlet of the oxygen-based aeration membrane assembly (6) via a gas delivery pipeline; a gas electric regulating valve (13) is arranged on the gas delivery pipeline between the gas outlet of the aeration pump (4) and the gas inlet of the oxygen-based aeration membrane assembly (6); The hydrogen-based aeration membrane system is composed of a hydrogen-based aeration membrane assembly (16) and a hydrogen generator (11); the hydrogen-based aeration membrane assembly (16) is arranged in a reaction tank (18), and the gas outlet of the hydrogen generator (11) is connected to the gas inlet of the hydrogen-based aeration membrane assembly (16) through a gas delivery pipeline; a hydrogen pressure reducing gauge (8) and a hydrogen mass flow meter (17) are arranged on the gas delivery pipeline between the gas outlet of the hydrogen generator (11) and the gas inlet of the hydrogen-based aeration membrane assembly (16); The oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16) are hollow fiber membrane assemblies; The control system is composed of a first dissolved oxygen sensor (5), a first pH sensor (7), a hydrogen sensor (10) and an electric control box (12); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are arranged in a reaction tank (18); the first dissolved oxygen sensor (5), the first pH sensor (7) and the hydrogen sensor (10) are respectively connected to the electric control box (12).

7. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 6 is characterized by: The hollow fiber membrane component is made of polyether ketone, polypropylene or polyurethane.

8. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 6 is characterized by: The drainage system is composed of a drainage pump (9) and a drainage pipeline, and the water inlet end of the drainage pump (9) is connected to a drainage outlet arranged at the bottom of the reaction tank (18) through the drainage pipeline.

9. The oxygen-hydrogen double membrane wastewater extreme denitrification and carbon reduction system according to claim 6, characterized in that: The water inlet system is composed of a water supply pump (3) and a water inlet pipeline, wherein the water outlet of the water supply pump (3) is connected to a water inlet provided at the bottom of the reaction tank (18) via the water inlet pipeline; the water inlet system adjusts the water inlet flow rate according to the required hydraulic retention time in the reaction tank (18).

10. A method for treating sewage using the oxygen-hydrogen double membrane sewage extreme denitrification and carbon reduction system as claimed in claim 6, characterized in that: The method proceeds as follows:

1. Sewage is introduced into the reaction tank (18), oxygen or air is introduced into the reaction tank (18) by using an aeration pump (4), hydrogen is introduced into the reaction tank (18) by using a hydrogen generator (11), sludge from the secondary sedimentation tank of a municipal sewage treatment plant is inoculated into the reaction tank (18), and batch operation is performed for 7 to 10 days at an O2 partial pressure of 2-10 psi and a H2 partial pressure of 5-10 psi until the COD of the effluent from the reaction tank (18) is not more than 60 mg / L and the TN of the effluent is not more than 5 mg / L, and COD-degrading bacteria, nitrifying bacteria and hydrogen-autotrophic denitrifying bacteria are cultivated in the reaction tank (18); The sewage is domestic sewage, food wastewater, livestock and poultry wastewater or mineral processing wastewater; the carbon-nitrogen ratio of the sewage is lower than 5:1, and the ammonia nitrogen concentration is 1 to 200 mg-N / L; 2. The reaction tank (18) is adjusted to operate in a continuous flow mode until the concentrations of ammonia nitrogen, nitrate nitrogen and nitrite nitrogen in the effluent of the reaction tank (18) are all less than 1 mg / L. At this time, biofilm enrichment is completed on the oxygen-based aeration membrane assembly (6) and the hydrogen-based aeration membrane assembly (16), and the system is started; 3. Continuously introducing sewage into the reaction tank (18) to achieve continuous sewage treatment; The hydraulic retention time of the sewage continuous treatment is 4-24h, the O2 partial pressure is 2-10psi, and the H2 partial pressure is 5-15psi.

Images