CN219991308U - Sewage treatment system of MBR (Membrane bioreactor) - Google Patents
Sewage treatment system of MBR (Membrane bioreactor) Download PDFInfo
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- CN219991308U CN219991308U CN202320584827.6U CN202320584827U CN219991308U CN 219991308 U CN219991308 U CN 219991308U CN 202320584827 U CN202320584827 U CN 202320584827U CN 219991308 U CN219991308 U CN 219991308U
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Abstract
The utility model discloses a sewage treatment system of an MBR (Membrane biological reactor), which comprises a water inlet area, a pre-anoxic area, an anaerobic area, a first low-oxygen aeration area, a second low-oxygen aeration area, a gas-water backwashing sedimentation area and an MBR membrane area, wherein gas stripping devices are arranged in the anoxic area, the anaerobic area and the MBR membrane area, and aeration devices are arranged in the first low-oxygen aeration area and the second low-oxygen aeration area; the sewage firstly enters a water inlet area, and is arranged in an anoxic area and an anaerobic areaUnder the action of the air stripping device, sewage enters the anoxic zone and the anaerobic zone through the pre-anoxic zone; then the sewage is converged and sequentially passes through the first low-oxygen aeration zone, the second low-oxygen aeration zone and the air-water backwashing precipitation zone; the utility model arranges the anaerobic zone and the anoxic zone in parallel rather than as in the conventional A 2 The O process adopts a serial design mode to prolong the reaction time of microorganisms in respective functional areas, thereby enhancing the biological denitrification and dephosphorization removal capacity and improving the removal efficiency.
Description
Technical Field
The utility model relates to the technical field of sewage treatment, in particular to a sewage treatment system of an MBR (Membrane bioreactor).
Background
At present, biological dephosphorization can be completed in an anaerobic and aerobic alternating environment, and biological denitrification can be performed in an anoxic and aerobic condition. Therefore, to achieve the aim of simultaneous dephosphorization and denitrification, three physiological environments of aerobic, anoxic and anaerobic needed by microorganisms must be created, thus forming an A/O (anaerobic/anoxic/aerobic) process for both dephosphorization and denitrification. At present, the process is applied to a plurality of sewage treatment plants around the world, but long-term operation results show that the denitrification effect is often poor when the dephosphorization effect is good; when the denitrification effect is good, the dephosphorization effect is not ideal, and the good dephosphorization effect cannot be achieved at the same time.
Disclosure of Invention
In order to overcome the defects in the prior art, the utility model provides a sewage treatment system of an MBR (Membrane bioreactor).
In order to achieve the above purpose, the utility model provides a sewage treatment system of an MBR membrane bioreactor, which comprises a water inlet area, a pre-anoxic area, an anaerobic area, a first low-oxygen aeration area, a second low-oxygen aeration area, a gas-water backwashing sedimentation area and an MBR membrane area, wherein gas stripping devices are arranged in the anoxic area, the anaerobic area and the MBR membrane area, and aeration devices are arranged in the first low-oxygen aeration area and the second low-oxygen aeration area;
the sewage firstly enters the water inlet area and eliminates oxygen in the sewage under the metabolism of microorganisms, the sewage enters the anoxic area and the anaerobic area through the pre-anoxic area respectively under the action of the gas stripping devices of the anoxic area and the anaerobic area, the pre-anoxic area carries out denitrification reaction, the anoxic area carries out denitrification reaction under the action of denitrifying bacteria, and the anaerobic area carries out phosphorus release reaction under the action of phosphorus release bacteria; and then the sewage is converged and sequentially passes through the first low-oxygen aeration zone, the second low-oxygen aeration zone and the gas-water backwashing precipitation zone, and is subjected to nitration reaction under the action of nitrifying bacteria in the first low-oxygen aeration zone and the second low-oxygen aeration zone, and is precipitated in the gas-water backwashing precipitation zone, so that mud-water separation can be realized. In the state that the air-washing backflushing device is not opened, the clean water flows into a subsequent membrane pool; and the sludge with weak sedimentation performance in the membrane tank can be washed out to the membrane tank under the state that the air-wash backflushing device is started, and then the sludge with good sedimentation performance after being modified in the membrane tank is pumped into the second hypoxia aeration zone again under the action of the air stripping device of the MBR membrane zone to participate in the whole-course reciprocating cycle treatment.
Preferably, the stripping device is also arranged in the MBR membrane area, the air-water backwashing precipitation area is provided with the air-water backwashing device, and the stripping device and the air-water backwashing device in the MBR membrane area are synchronously opened or closed.
Preferably, the sludge of the sedimentation zone is flowed into the water inlet zone.
Preferably, a stripping device is also arranged in the first low-oxygen aeration zone, and under the action of the gas device, the muddy water mixed solution in the second low-oxygen aeration zone is pumped into the first low-oxygen aeration zone again.
Preferably, the muddy water mixed solution in the second low-oxygen aeration zone can also flow into the water inlet zone.
Preferably, the muddy water mixed solution treated by the MBR membrane area is lifted to the second low-oxygen aeration area under the action of a gas stripping device in the MBR membrane area.
Compared with the prior art, the utility model has the beneficial effects that:
the anaerobic zone and the anoxic zone are arranged in parallel, so that the reaction time of microorganisms in the respective functions can be prolonged, and the improvement of the biological denitrification and dephosphorization removal capacity and the removal efficiency can be enhanced; the low-oxygen biochemical unit and the MBR membrane treatment unit can be independently operated in series, so that the two biochemical units can independently screen, domesticate and culture the respective characteristic flora aiming at the characteristic pollutants, and the purpose that the membrane tank can further remove the characteristic pollutants which cannot be removed by the low-oxygen biochemical treatment unit is achieved. It is thus possible to achieve a targeted maximum removal of the specific characteristic contaminants to be removed by the own processing unit. Thirdly, the membrane stripping device and the air washing backflushing device in the air washing sedimentation area can be simultaneously started to integrate the low-oxygen biochemical unit and the genus of the membrane treatment unit, so that the genus unification is realized, the biological metabolism reaction time of the incomplete pollutant removed by the low-oxygen biochemical treatment unit can be prolonged by the membrane pond, and the further enhancement of the low-oxygen biochemical removal effect and removal capacity can be achieved. The low-oxygen aeration biochemical reaction and the MBR membrane are organically combined, so that ammonia nitrogen, total nitrogen and organic matters can be removed at the same time, the operation energy consumption is reduced, and the carbon source addition amount is reduced; secondly, the membrane pool can be independently operated through the low-oxygen biochemical unit and the MBR membrane treatment unit to culture specific bacteria of the characteristic pollutants to be removed respectively, and the membrane pool can further remove the characteristic pollutants which cannot be removed by the low-oxygen biochemical treatment unit. Thirdly, the membrane stripping device and the air-water backwashing device can be combined together to realize integration and unification of microorganism metabolism bacteria, so that the membrane tank can prolong the biological metabolism reaction time of the pollutants which are not thoroughly removed by the low-oxygen biochemical treatment unit, the low-oxygen biochemical removal effect and the removal capacity can be further enhanced, the application range of the MBR is widened, and the membrane tank has higher research value and practical value.
Drawings
FIG. 1 is a block diagram of a sewage treatment system of an MBR membrane bioreactor of the present utility model.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more apparent, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments of the present utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The utility model is described in further detail below with reference to fig. 1:
referring to fig. 1, the utility model provides a sewage treatment system of an MBR membrane bioreactor, which comprises a water inlet area, a pre-anoxic area, an anaerobic area, a first low-oxygen aeration area, a second low-oxygen aeration area, a gas-water backwashing precipitation area and an MBR membrane area, wherein gas stripping devices are arranged in the anoxic area, the anaerobic area and the MBR membrane area, and aeration devices are arranged in the first low-oxygen aeration area and the second low-oxygen aeration area; a gas-water backwashing device is arranged in the gas-water backwashing precipitation area;
the sewage firstly enters a water inlet area and eliminates oxygen in the sewage under the metabolism of microorganisms, the sewage enters the anoxic area and the anaerobic area through a pre-anoxic area respectively under the action of a gas stripping device of the anoxic area and the anaerobic area, denitrification reaction is carried out in the pre-anoxic area, denitrification reaction is carried out under the action of denitrifying bacteria in the anoxic area, and phosphorus release reaction is carried out under the action of phosphorus release bacteria in anaerobic removal; and then the sewage is converged and sequentially passes through the first low-oxygen aeration zone, the second low-oxygen aeration zone and the air-water backwashing precipitation zone, the nitrifying reaction is carried out under the action of nitrifying bacteria in the first low-oxygen aeration zone and the second low-oxygen aeration zone, and the sludge-water separation is carried out by precipitation in the air-water backwashing precipitation zone. Under the operation condition that the gas-water backwashing device is not started and the gas stripping device in the MBR membrane area is not started, the effluent is clear liquid, and then enters the MBR membrane area to be subjected to strengthening treatment again by adopting corresponding special bacteria aiming at characteristic pollutants. The sludge in the MBR membrane area is filtered and intercepted by the membrane, clear water is discharged outside the membrane, and meanwhile, as the air stripping device in the MBR membrane area is not started, microorganisms in the MBR membrane area can not run off to the second hypoxia aeration area, so that the separation of the microorganisms in the MBR membrane area and the microorganisms of the hypoxia biochemical treatment unit at the front end of the air-water backwashing precipitation area can be realized, the respective independent domestication culture is realized, the competition is not realized, the respective independent screening and domestication of the microorganisms with the respective unique special advantages can be finally realized, and the respective specific removal of the respective characteristic pollutants is realized. In addition, the anaerobic reactor can wash flocculent sludge of the low-oxygen biochemical treatment unit with weak sedimentation performance to the MBR membrane area when the anaerobic reactor is started under the condition that the air stripping device in the MBR membrane area and the air-water backwashing device in the air-water backwashing precipitation area are started together, and the flocculent sludge with strong sedimentation performance is left, and the sludge with low SVI directly flows back to the front-end low-oxygen reaction area through the self sludge backflow device. The muddy water mixed liquid entering the MBR membrane area is lifted to a second low-oxygen aeration area through a gas stripping device in the MBR membrane area, so that the membrane treatment unit and the low-oxygen biochemical unit are integrated, the microbial genus is completely consistent, and the low-oxygen biochemical unit is a low-oxygen biochemical unit for short in total in other areas except the MBR membrane area.
Specifically, sewage firstly enters a water inlet area, the higher-concentration water is firstly subjected to the metabolism of microorganisms, free oxygen in the sewage is consumed completely, and the optimal metabolism operation conditions required by good biological anaerobic and anoxic reactions are provided for subsequent anaerobic and anoxic reactions.
Furthermore, the sludge-water mixed solution in the second low-oxygen aeration zone can also flow into the water inlet zone, and the sludge in the air-water backwashing precipitation zone can also flow into the water inlet zone. So that the sewage is mixed with the nitrifying liquid which flows back from the tail end of the second low-oxygen aeration zone and the return sludge of the air-water backwashing precipitation zone in the water inlet zone.
In this embodiment, the muddy water mixed solution after the mixed reaction in the water inlet zone is brought into the pre-anoxic zone thereof under the combined action of the gas stripping device in the anaerobic zone and the gas stripping device in the anoxic zone, and partial denitrification is realized by the denitrification of microorganisms in the anoxic environment, and meanwhile, the combined oxygen in the muddy water mixed solution can be further reduced, so that a stricter anaerobic phosphorus release environment is created for phosphorus release bacteria after the muddy water mixed solution enters the subsequent anaerobic zone, and the improvement of biological phosphorus removal efficiency is promoted.
Further, the sludge-water mixed liquid after partial denitrification in the pre-anoxic zone is respectively brought into a subsequent anoxic zone by a gas stripping device at the tail end of the anoxic zone and brought into an anaerobic zone by a gas stripping device at the tail end of the anaerobic zone; and (3) continuing denitrification of the muddy water mixed solution entering the anoxic zone under the action of denitrifying bacteria, thereby realizing standard discharge of total nitrogen. And the muddy water mixed solution entering the anaerobic zone finishes the release of phosphorus under the action of phosphorus release bacteria in the anaerobic zone, and creates an indispensable precondition for the excessive absorption of phosphorus entering the low-oxygen aeration zone and the MBR membrane zone. The sludge-water mixed liquor in the anaerobic zone is lifted to the front end of the first low-oxygen aeration zone through the anaerobic lifting device at the tail end of the sludge-water mixed liquor, the sludge-water mixed liquor in the anoxic zone is lifted to the front end of the first low-oxygen aeration zone through the gas lifting device at the tail end of the anaerobic zone, the sludge-water mixed liquor in the tail end of the second low-oxygen aeration zone is lifted to the front end of the first low-oxygen aeration zone through the gas lifting device at the front end of the first low-oxygen aeration zone, and all three sludge-water mixed liquor are oxygenated and aerated by utilizing the aeration device at the front end of the first low-oxygen aeration zone, so that an aerodynamic source is provided, the 'gas dual-purpose' in the true sense is realized, the nearly 'zero' energy consumption gas stripping reflux is realized, and a large amount of energy consumption required by internal and external reflux of sludge during denitrification and dephosphorization is greatly saved. When the actual operation condition is low load or ultra-low load, the mode of closing each stripping device and even the membrane area stripping device can realize that partial functional areas are directly surpassed by short flow and do not participate in the cyclic reaction, so that the effective reaction tank capacity actually participated in can be reduced, the sludge load or volume load can be indirectly improved, and the technical problem that the biochemical normal operation of low load or ultra-low load is difficult is effectively solved.
The three sludge-water mixed liquids are rapidly mixed and diluted at the front end of the first hypoxia aeration zone, and then are subjected to hypoxia control (DO at the tail end of the hypoxia zone is less than or equal to 1 mg/l), so that synchronous short-cut nitrification and denitrification can be realized, partial ammonia nitrogen and total nitrogen are removed, and meanwhile, phosphorus accumulating bacteria can synchronously complete excessive phosphorus absorption biological metabolism and organic biological carbonization reaction metabolism. And the other part of the muddy water mixed solution subjected to decarbonization, denitrification and dephosphorization through the second hypoxia aeration zone enters a subsequent gas-water backwashing precipitation zone to realize muddy water separation. The sludge after precipitation separation flows back to the water inlet area to continue to participate in reciprocating circulation metabolism, and the effluent flows into the subsequent MBR membrane area through the water collecting tank and the water outlet channel to participate in biological metabolism.
In the embodiment, the dissolved oxygen in the low-oxygen aeration zone needs to be controlled to be lower than 1mg/l, and the dissolved oxygen at the tail end is preferentially controlled to be lower than 0.3mg/l, so that synchronous short-cut nitrification and denitrification can be realized in the aerobic zone under the condition of microbial low oxygen, and a novel denitrification function of short-cut nitrification and denitrification can be realized in the aerobic zone; the MBR membrane area selects the traditional high dissolved oxygen operation (DO is more than or equal to 1 mg/l) so as to be beneficial to realizing the enhancement of the removal efficiency and the treatment capacity of organic matters and ammonia nitrogen, enhancing the excessive absorption of phosphorus by phosphorus releasing bacteria and improving the biological phosphorus removal efficiency.
Furthermore, the anaerobic zone and the anoxic zone in the utility model are in a parallel operation mode, and a traditional serial design mode is abandoned, so that the anaerobic sludge reflux and the anoxic nitrifying liquid reflux quantity are controlled by respective gas stripping devices, the metabolic reaction time of organisms in respective functional zones can be prolonged, the promotion of the enhanced biological denitrification and dephosphorization removal capacity and the removal efficiency can be achieved, meanwhile, the short-flow operation can be realized by controlling the on and off of the respective gas stripping devices, and the technical problem that the biochemical normal operation of a sewage treatment plant is difficult under low load and ultra-low load is solved.
Still further, the low oxygen aeration zone is not less than 2 groups, so that the low dissolved oxygen zone can realize self-internal circulation plug flow dilution through the gas stripping device thereof, and finally, the perfect flow state of the low oxygen zone which can realize the combination of plug flow and complete mixing is achieved. The flow state can create a low-matrix biological metabolism environment for nitrifying bacteria throughout the year, is beneficial to forming dominant bacterial groups by nitrifying bacteria, is beneficial to thoroughly performing nitrifying, and can greatly improve the removal efficiency and the treatment capacity of ammonia nitrogen and total nitrogen.
In this embodiment, the water inlet of the MBR membrane area comes from the water outlet of the air-water backwashing precipitation area, and compared with the traditional MBR process, the water inlet amount of the MBR membrane area is not only dependent on the actual water inlet amount of the front-end low-oxygen biological nitrogen and phosphorus removal process, but also increases the air-stripping lifting amount of the membrane circulation air-stripping device, which is beneficial to realizing the increase of the rising flow rate of precipitation by increasing the reflux amount of the membrane circulation air-stripping device on the premise of ensuring the design treatment scale and ensuring the stable and standard of the water quality of the water outlet, thereby preferentially washing flocculent activated sludge with poor sedimentation performance and high SVI value, and creating a very favorable precondition for the high-sludge concentration operation of the novel low-oxygen biological nitrogen and phosphorus removal process for the sedimentation interception of the flocculent activated sludge with good sedimentation performance and low SVI value. The method is based on the interception function of the subsequent membrane, so that the process can help to further directly raise the surface load of the traditional secondary sedimentation tank from the traditional common design value of 0.5-0.8 m3/m2.H to not lower than 0.8m3/m2.H, thereby greatly improving the surface load of the traditional sedimentation tank and reducing the investment of the traditional sedimentation tank. And flocculent activated sludge with high SVI value and poor sedimentation performance entering the membrane tank is subjected to nutrition and the like to modify the sedimentation performance, and then flows back to the novel low-oxygen biological nitrogen and phosphorus removal process again through the membrane circulation stripping reflux device, so that the sludge concentration can be further improved, the operation of maintaining the high sludge concentration of the low-oxygen biological nitrogen and phosphorus removal process throughout the year is facilitated, the treatment capacity and the removal efficiency are improved, and the aerobic granulation of the activated sludge under low oxygen is also facilitated. In addition, as the water coming from the MBR membrane area comes from the precipitated water, the winding and blocking of sundries in sewage to membrane wires can be prevented, the pollution degree of the membrane is further greatly reduced, the membrane flux is improved, and the service life of the membrane is prolonged.
Furthermore, the MBR membrane area can be operated independently according to actual operation conditions, and in the state that the membrane circulation stripping device is shut down, the activated sludge in the MBR membrane area does not participate in the circulation treatment of the novel low-oxygen biological denitrification and dephosphorization process, so that the independent operation of each membrane area can be realized, the independent operation is not interfered with each other, and the membrane area is converted into serial operation, which is equivalent to two-stage treatment. Therefore, aiming at characteristic pollutants which are difficult to biochemically degrade in the field of sewage industry, special strains can be introduced into a membrane pond by inoculating and expanding high-efficiency strains, and the special microorganisms can be utilized to strengthen and remove certain characteristic pollutants which are not biochemically degraded by the novel front-end low-oxygen biological denitrification and dephosphorization process, so that an independent optimal metabolism environment which is favorable for becoming dominant flora is provided, the characteristic pollutants which are difficult to biochemically degrade can be purposefully and efficiently removed, and an optimal short-flow biological metabolism technical solution is found out
In the embodiment, aiming at special fields of industries and aiming at characteristic pollutants which are difficult to be degraded by sewage biochemistry, the utility model can also realize that activated sludge in a membrane area does not participate in circulation treatment by closing the stripping device in the MBR membrane area, so that the activated sludge can be the characteristic pollutants which are difficult to be degraded by biochemically in the field of sewage industries, and the special strains can be purposefully introduced into the membrane area by inoculating and expanding high-efficiency strains, so that the specificity of the special strains can be utilized to strengthen certain characteristic pollutants which are not degraded by biochemically in the novel front-end low-oxygen biological denitrification and dephosphorization process, and finally the standard emission is realized. The design mode can be flexibly switched in series independently through one zone, and the optimal living and metabolism environment of organisms is created for culturing each dominant flora, so that the on-off of the stripping device in the MBR membrane can purposefully remove characteristic pollutants which are difficult to biochemically degrade according to the actual operating condition requirement, and an optimal short-flow biological metabolism technical solution is found.
According to the utility model, the MBR process of sludge reflux is realized by fully playing the synchronous short-cut nitrification and denitrification of the novel low-oxygen biological denitrification and dephosphorization process under low oxygen and combining with the near zero-consumption membrane gas stripping circulation device, so that the energy-saving low-carbon operation can be realized by the low-oxygen biological denitrification of the traditional MBR process, and the synergistic effect of precipitation filtration and membrane circulation large-scale gas stripping reflux flushing of the novel low-oxygen biological denitrification and dephosphorization process can be realized, so that the membrane flux is improved, the membrane pollution is reduced, the service life of the membrane is prolonged, and the membrane investment is reduced. The high sludge concentration, the short flow and the excellent water quality of the effluent of the traditional MBR membrane process can be fully exerted, and the sewage can be discharged stably and up to the standard throughout the year.
In addition, the utility model can also extend the introduction of special strains into the membrane pool through a serial operation mode, can play the technical advantage of degradation specificity of the special strains for characteristic pollution difficult to biochemically degrade, further degrade and improve the removal efficiency and the processing capacity of a biochemical system. Meanwhile, the biological filler, the adsorbent or the oxidant and other auxiliary technical means can be added into the membrane pool to act together, so that the effluent quality of the traditional MBR process is further improved, and zero emission, sewage recycling and the like are realized. Through the MBR combined process flow of the novel coupling low-oxygen biological denitrification and dephosphorization process, the technical problems of large investment of membrane components, high operation energy consumption, difficult membrane pollution control and the like which are difficult to solve in the wide popularization and application of engineering and the like can be thoroughly solved, the membrane technology can be really realized, the construction can be realized, the sustainable operation of energy-saving low-carbon operation is realized, and the membrane technology is promoted to be popularized and applied more rapidly in the sewage treatment industry.
The above is only a preferred embodiment of the present utility model, and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (6)
1. The MBR membrane bioreactor sewage treatment system is characterized by comprising a water inlet area, a pre-anoxic area, an anaerobic area, a first low-oxygen aeration area, a second low-oxygen aeration area, a gas-water backwashing sedimentation area and an MBR membrane area, wherein gas stripping devices are arranged in the anoxic area and the anaerobic area, and aeration devices are arranged in the first low-oxygen aeration area and the second low-oxygen aeration area;
the sewage firstly enters the water inlet area, and under the combined action of the air stripping devices of the anoxic area and the anaerobic area, the sewage continuously enters the pre-anoxic area, and the oxygen in the sewage is continuously digested by the microorganisms, and then enters the anoxic area and the anaerobic area respectively, wherein the pre-anoxic area is subjected to denitrification reaction, the denitrification bacteria in the anoxic area are subjected to denitrification reaction, and the anaerobic phosphorus-releasing bacteria in the anaerobic area are subjected to phosphorus-releasing reaction; then the sewage is converged and sequentially passes through the first low-oxygen aeration zone, the second low-oxygen aeration zone and the gas-water backwashing precipitation zone, and is subjected to nitration reaction under the action of nitrifying bacteria in the first low-oxygen aeration zone and the second low-oxygen aeration zone, and is precipitated in the gas-water backwashing precipitation zone to carry out mud-water separation; and the supernatant fluid of the air-water backwashing precipitation zone enters the MBR membrane zone for treatment.
2. The MBR membrane bioreactor sewage treatment system of claim 1, wherein a stripping device is also arranged in the MBR membrane area, a gas-water backwashing device is arranged in the gas-water backwashing precipitation area, and the stripping device and the gas-water backwashing device in the MBR membrane area are synchronously opened or closed.
3. The MBR membrane bioreactor sewage treatment system according to claim 1, wherein the sludge of the precipitation zone flows into the water inlet zone.
4. The MBR membrane bioreactor sewage treatment system according to claim 1, wherein a gas stripping device is also arranged in the first low-oxygen aeration zone, and the muddy water mixed liquid in the second low-oxygen aeration zone is pumped into the first low-oxygen aeration zone again under the action of the gas device.
5. The MBR membrane bioreactor sewage treatment system according to claim 1, wherein the sludge-water mixture in the second low oxygen aeration zone can also flow into the water inlet zone.
6. The MBR membrane bioreactor sewage treatment system of claim 2, wherein the sludge-water mixture treated by the MBR membrane zone is lifted to the second low oxygen aeration zone by a gas stripping device in the MBR membrane zone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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