CN116477776A - Front-phosphorus-removal rear-endogenous denitrification coupling MBR sewage treatment system and technology - Google Patents
Front-phosphorus-removal rear-endogenous denitrification coupling MBR sewage treatment system and technology Download PDFInfo
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- 239000010865 sewage Substances 0.000 title claims abstract description 111
- 230000008878 coupling Effects 0.000 title claims abstract description 25
- 238000010168 coupling process Methods 0.000 title claims abstract description 25
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 25
- 238000005516 engineering process Methods 0.000 title abstract description 5
- 239000010802 sludge Substances 0.000 claims abstract description 130
- 239000012528 membrane Substances 0.000 claims abstract description 52
- 238000010992 reflux Methods 0.000 claims abstract description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000000034 method Methods 0.000 claims abstract description 35
- 230000008569 process Effects 0.000 claims abstract description 34
- 238000005189 flocculation Methods 0.000 claims abstract description 33
- 230000016615 flocculation Effects 0.000 claims abstract description 33
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 238000001556 precipitation Methods 0.000 claims abstract description 25
- 241000894006 Bacteria Species 0.000 claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000006228 supernatant Substances 0.000 claims abstract description 10
- 239000004576 sand Substances 0.000 claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 6
- 238000005273 aeration Methods 0.000 claims description 44
- 238000004062 sedimentation Methods 0.000 claims description 14
- 239000003795 chemical substances by application Substances 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 12
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 8
- 230000014759 maintenance of location Effects 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 6
- 230000003311 flocculating effect Effects 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 27
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 27
- 239000011574 phosphorus Substances 0.000 abstract description 27
- 238000001514 detection method Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 34
- 230000000694 effects Effects 0.000 description 19
- 229910052757 nitrogen Inorganic materials 0.000 description 17
- 230000001546 nitrifying effect Effects 0.000 description 12
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
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- 230000002035 prolonged effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000003851 biochemical process Effects 0.000 description 1
- 238000003426 chemical strengthening reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2209/22—O2
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
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Abstract
The invention provides a front-mounted dephosphorization and rear-mounted endogenous denitrification coupling MBR sewage treatment system and a technology, wherein the system mainly comprises a front-mounted dephosphorization unit, a rear-mounted endogenous denitrification unit and a sludge reflux unit, and effluent from a sand basin enters a flocculation precipitation dephosphorization basin to remove phosphorus; then the supernatant fluid enters a post-endogenous denitrification unit, denitrifying bacteria in an anaerobic tank absorb carbon sources, and dynamically and accurately nitrify in a dynamic aerobic tank in combination with a detection instrument and control equipment, and then perform post-endogenous denitrification in an anoxic tank, so that deep denitrification is achieved; the effluent and sludge from the anoxic tank enter the MBR membrane tank and the sludge reflux unit, and a double reflux system is adopted to realize the maximization of the anaerobic zone function, or a pre-anaerobic zone is arranged, water is shunted and fed, so that the influence of high-solubility oxygen of the MBR membrane tank on denitrifying bacteria is reduced. The system and the process solve the problems that the traditional pre-denitrification efficiency is low, the sludge age contradiction between post-biological dephosphorization and denitrification is high, the biochemical effluent suspended matters are high, and the sludge concentration can not be selectively increased in winter.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a front-phosphorus removal and rear-endogenous denitrification coupling MBR sewage treatment system and technology.
Background
The main current sewage treatment process is to perform pre-denitrification and biological dephosphorization combined post-chemical enhanced dephosphorization through microorganisms, namely, denitrification (mainly complete denitrification) is completed in the first half of the process, the later aerobic section is responsible for nitrification, a part of total phosphorus of sewage is removed by discharging phosphorus-rich sludge, and meanwhile, the total phosphorus is ensured to reach the standard by adding a dephosphorizing agent into biochemical effluent for enhanced dephosphorization, and part of suspended matters are removed.
The disadvantages of the above process are mainly: (1) The total nitrogen removal rate is low, the denitrification efficiency is controlled by controlling the reflux ratio, but the reflux ratio is generally less than 300%, so the total nitrogen removal rate of the pre-denitrification process is generally less than 80%. (2) Biochemical denitrification and dephosphorization are carried out simultaneously, so that the contradiction of sludge age is caused, a plurality of rows of sludge are beneficial to dephosphorization, but are unfavorable for denitrification, and a small number of sludge discharge are beneficial to denitrification but are unfavorable for dephosphorization, so that the contradiction of denitrification and dephosphorization is difficult to reconcile for some wastewater with high total phosphorus. (3) After the chemical strengthening dephosphorization, in order to ensure that suspended matters reach the standard, a filtering device is generally required to be added, so that the treatment process is complex, the investment is increased, and the operation is complicated. (4) The traditional secondary sedimentation tank is difficult to improve the sludge concentration, and when the water temperature in winter is low, the water quality of the effluent cannot be ensured by improving the sludge concentration. (5) If MBR effluent and traditional post-dephosphorization are adopted, the dephosphorization agent is unfavorable for playing the dephosphorization effect because the SS of the MBR effluent is very low.
Therefore, it is necessary to develop a sewage treatment system and process for deep denitrification and dephosphorization which can solve the problems of low efficiency of traditional pre-denitrification and denitrification, contradiction between post-biological dephosphorization and denitrification sludge age, high suspension of biochemical effluent, incapability of increasing sludge concentration at will in winter, and the like.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides a pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment system and a pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment process, which can solve the problems that the traditional pre-denitrification has low denitrification efficiency, the post-biological dephosphorization and denitrification sludge age contradiction exists, the biochemical effluent suspension is high, the sludge concentration cannot be increased at will in winter, and the like, and the specific technical scheme is as follows:
the invention firstly provides a prepositive dephosphorization postpositive endogenous denitrification sewage treatment system, which comprises a sand setting tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank;
the grit chamber, the flocculation precipitation dephosphorization tank, the anaerobic tank, the dynamic aerobic tanks, the anoxic tanks, the MBR membrane tank and the sludge concentration tank are sequentially communicated through pipelines;
the flocculation precipitation dephosphorization pond is communicated with the sludge concentration pond through a pipeline, and the pipeline is provided with a sludge pump.
The MBR membrane tank is connected with a sludge reflux system;
the anaerobic tank and the anoxic tank are respectively provided with a stirrer, and the dynamic aerobic tank is respectively provided with an aeration device and a stirrer.
In some embodiments of the invention, the sludge recirculation system comprises a pipeline connecting the MBR membrane tank and the front end of the dynamic aerobic tank and a sludge pump.
In some embodiments of the invention, the end of the anoxic tank is communicated with the front end of the anaerobic tank through a pipeline, and the pipeline is provided with a sludge reflux pump.
In some embodiments of the invention, the sludge reflux system comprises a pre-anaerobic tank which is respectively communicated with the MBR membrane tank and the flocculation precipitation dephosphorization tank through pipelines, and the pipelines are provided with sludge reflux pumps; the pre-anaerobic tank is communicated with the water inlet of the anaerobic tank through a pipeline.
In some embodiments of the invention, the dynamic aerobic tank and the anoxic tank are both provided with a PH detector and a DO detector.
In some embodiments of the invention, the system further comprises a PLC controller, wherein the PLC controller is respectively in communication connection with the PH detector, the DO detector, the aeration device and the stirrer.
The invention also provides a process for treating the sewage by pre-dephosphorization and post-endogenous denitrification, which comprises the following process steps:
s1: sewage is treated by a primary sedimentation tank and then enters a flocculation sedimentation dephosphorization tank, the sewage is mixed with a flocculation dephosphorization agent added into the flocculation sedimentation dephosphorization tank, mud-water separation is realized, supernatant fluid enters an anaerobic tank, and precipitated sludge enters a sludge concentration tank;
s2: after sewage enters an anaerobic tank for mixing, the anaerobic tank is stirred, denitrifying bacteria absorb carbon sources, and the retention time is T 1 Hours;
s3: the effluent of the anaerobic tank enters a plurality of dynamic aerobic tanks, and the retention time of each dynamic aerobic tank is T 2 The nitrification is carried out under the action of stirring aeration for hours, and ammonia nitrogen and residual organic matters in the sewage are degraded; when the last dynamic aerobic tank dissolved oxygen is detected to be lower than 30% of the normal aeration rate, and the dissolved oxygen is still higher than 4mg/L, under the condition that the pH value is increased at the moment, the dynamic aerobic tank and the subsequent dynamic aerobic tanks automatically close the aeration to become an anoxic tank, and the anoxic tank is only provided with a stirrer;
s4: sewage entering the anoxic tank, wherein the total residence time of the anoxic tank is T 3 For an hour, denitrification is realized by the endogenous denitrification of denitrifying bacteria;
s5: sewage in the anoxic tank enters the MBR membrane tank after being discharged, sludge-water separation is realized, the sludge flows back to the front end of the anaerobic tank or the dynamic aerobic tank through the sludge backflow system, the residual sludge is discharged into the sludge concentration tank, and the supernatant is discharged.
In some embodiments of the present invention, in step S5, the sludge in the MBR membrane tank is returned to the front end of the dynamic aerobic tank, and the return ratio is 50%; the tail end sludge of the anoxic tank flows back to the front end of the anaerobic tank, and the reflux ratio is 100%.
In some embodiments of the invention, 10% of the water from the flocculation precipitation dephosphorization tank enters the pre-anaerobic tank and the remaining water enters the anaerobic tank; in the step S5, the sludge in the MBR membrane pond flows back to the pre-anaerobic pond, and the backflow ratio is 100%; the effluent of the pre-anaerobic tank enters the anaerobic tank.
In some embodiments of the invention, the flocculating dephosphorizing agent is PAC or PFC, and the PAC or PFC is used in an amount of 50mg/L to 200mg/L.
In some embodiments of the invention, the T 1 0.5-2, said T 2 2-3, said T 3 8-12;
in some specific embodiments of the invention, the concentration of dissolved oxygen during aeration of the dynamic aerobic tank is controlled to be 2mg/L-4mg/L.
In some embodiments of the invention, a carbon source is added to the anaerobic tank when the carbon to nitrogen ratio of the inlet water of the anaerobic tank is less than 3.
The beneficial effects of the invention are as follows:
(1) the phosphorus removal is placed at the front end of the biochemical process, and the competition of the subsequent phosphorus removal bacteria for a carbon source is reduced through chemical phosphorus removal, meanwhile, the growth of nonfunctional bacteria is reduced, the sludge growth is reduced, and the enriched denitrifying bacteria are maximized;
(2) the mode operation of AOA is adopted, so that the total nitrogen can be deeply removed, and meanwhile, the MBR technology is combined, so that the sludge concentration can be flexibly controlled, the effluent suspended matters can be ensured to reach the standard, and a subsequent deep treatment system is omitted;
(3) through adopting two return flow systems, realize the maximize of anaerobism district function, perhaps set up the anaerobism district in advance, the reposition of redundant personnel is intake, reduces the influence of MBR membrane pond high-solubility oxygen to denitrifying bacteria.
(4) The pH and DO detectors are equipped, the PLC and the aeration equipment capable of automatically adjusting aeration quantity are combined, automatic switching and variable-frequency operation of the equipment can be realized, the labor cost is further reduced, the energy consumption is saved, and the double-carbon policy is assisted.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a sewage treatment system of a pre-dephosphorization post-endogenous denitrification coupling MBR provided by the invention;
FIG. 2 is a schematic diagram of a wastewater treatment system of a pre-dephosphorization post-endogenous denitrification coupling MBR provided by the invention;
FIG. 3 is a schematic diagram of a wastewater treatment system of the MBR coupled with the pre-dephosphorization and post-endogenous denitrification of the control group in the embodiment 5 of the invention;
FIG. 4 is the data of the removal effect of sewage COD by the sewage treatment system of three different sludge recirculation modes according to the embodiment 5 of the invention;
FIG. 5 is the data of the total nitrogen removal effect of the sewage treatment system of three different sludge recirculation modes according to example 5 of the present invention;
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it should be apparent that the described embodiments are only some of the embodiments of the present invention and should not be used to limit the protection scope of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, are intended to fall within the scope of the present invention.
Example 1: front-mounted dephosphorization rear-mounted endogenous denitrification coupling MBR sewage treatment system
As shown in FIG. 1, the sewage treatment system of the front-end dephosphorization and rear-end endogenous denitrification coupling MBR comprises a sand sedimentation tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank; the grit chamber, the flocculation precipitation dephosphorization tank, the anaerobic tank, the dynamic aerobic tanks, the anoxic tanks, the MBR membrane tank and the sludge concentration tank are communicated through pipelines; the flocculation precipitation dephosphorization pool is communicated with the sludge concentration pool through a pipeline, and the pipeline is provided with a sludge pump; the MBR membrane tank is connected with a sludge reflux system, and the sludge reflux system comprises a pipeline connected with the front ends of the MBR membrane tank and the dynamic aerobic tank and a sludge pump; the tail end of the anoxic tank is communicated with the front end of the anaerobic tank through a pipeline, and a sludge reflux pump is arranged on the pipeline; the anaerobic tank and the anoxic tank are respectively provided with a stirrer, the dynamic aerobic tank is respectively internally provided with a stirrer and an aeration device, the dynamic aerobic tank and the anoxic tank are respectively provided with a PH detector and a DO detector, and the PLC is respectively in communication connection with the PH detector, the DO detector, the aeration device and the stirrer.
The invention relates to a prepositive dephosphorization postpositive endogenous denitrification sewage treatment system which mainly comprises three main parts: the sewage treatment process of the front phosphorus removal part, the rear endogenous denitrification part, the MBR membrane tank and the sludge reflux part is as follows:
(1) front dephosphorization
The advanced dephosphorization fully utilizes the characteristic of high suspended matters in the water inlet of the primary sedimentation tank by adding the efficient dephosphorization agent, so that the materialized dephosphorization is performed to the maximum extent, the total phosphorus content of the water inlet of the biochemical section is reduced, and the subsequent denitrification effect is further ensured.
Through the treatment of the process section, the total phosphorus in the sewage can basically realize up-to-standard discharge, and the subsequent biochemical section only needs to treat COD and total nitrogen in the sewage.
(2) Post endogenous denitrification
The theoretical basis of post endogenous denitrification is that denitrifying bacteria have the characteristic of storing carbon sources, the endogenous denitrification potential of the denitrifying bacteria is huge, and the main factors influencing the endogenous denitrification effect are anaerobic stirring time after water inflow, dissolved oxygen concentration during aeration, nitrification time and the like. The anaerobic stirring time is generally controlled to about 1 hour, and generally not more than 2 hours. At this stage, the denitrifying bacteria can adsorb and absorb organic matters in the sewage.
The sewage enters a dynamic aerobic tank, the concentration of dissolved oxygen during aeration is controlled to be 2mg/L-4mg/L, and meanwhile, in order to shorten the nitrification time as much as possible, the time for over-aeration needs to be reduced. In order to realize accurate aeration of sewage, a plurality of relatively independent dynamic aerobic tanks (each dynamic aerobic tank is connected through a pipeline and is approximately and completely mixed) are arranged, a DO detector and a pH detector are arranged in each dynamic aerobic tank, whether the system is nitrified is finished or not can be judged by observing the change of the pH value and the DO of the dynamic aerobic tank (when the nitrifying is finished, the activity of nitrifying bacteria is reduced, the oxygen consumption is reduced, the Dissolved Oxygen (DO) of the sewage relatively rises, the alkalinity in the sewage is consumed due to the nitrifying effect, the pH value of the dynamic aerobic tanks gradually falls, the pH value gradually rises after the nitrifying is finished, and when one dynamic aerobic tank is detected that the dissolved oxygen is still higher than 4mg/L when the aeration amount is lower than 30% of the normal aeration amount, and under the condition that the pH value rises, the nitrifying of the system is finished, the dynamic aerobic tanks and the subsequent dynamic aerobic Chi Bianke can stop aeration, namely the energy is saved, and the nitrifying is ensured to be complete in the shortest time.
Enters an anoxic tank, and deep denitrification is realized through the endogenous denitrification of denitrifying bacteria.
(3) MBR membrane tank and sludge return part
In order to solve the problems that suspended matters in the effluent exceed standard and the concentration of the sludge cannot be adjusted, an MBR membrane tank is adopted to replace a traditional secondary sedimentation tank, so that suspended solids reach the standard, a subsequent filtering process is omitted, the sludge age of a sewage treatment system can be prolonged, and the denitrification effect of the sewage treatment system is improved. In order to ensure the effect of absorbing carbon sources by the anaerobic section, main sludge reflux is carried out from the tail end of the anoxic tank, and in order to maintain the sludge concentration of the MBR membrane tank, the sludge of the MBR membrane tank is refluxed to the forefront end of the dynamic aerobic tank without damaging the function of the anaerobic tank.
The COD, ammonia nitrogen, total phosphorus and suspended solids of the treated effluent of the sewage treatment system all reach the standard.
Example 2: front-phosphorus-removal rear-endogenous denitrification coupling MBR sewage treatment process
The process in the embodiment is based on the system in the embodiment 1, is mainly used for treating municipal sewage, and mainly adopts the water inflow index of COD2000 mg/L-2200 mg/L, ammonia nitrogen 360 mg/L-450 mg/L and total phosphorus 10 mg/L-20 mg/L. Sewage is treated by a grit chamber and then enters a flocculation precipitation dephosphorization tank, is mixed with a flocculation dephosphorization agent added into the tank, then mud-water separation is realized, supernatant fluid enters an anaerobic section of a biochemical stage, and precipitated sludge enters a sludge concentration tank. The flocculating dephosphorizing agent can use PAC or PFC, the dosage of the PAC or PFC is 50mg/L to 200mg/L according to the water quality condition, the total phosphorus removal rate of the process section is more than 90 percent, and the total phosphorus of the effluent is controlled to be 0.3mg/L to 1mg/L. After sewage enters the anaerobic tank, activated sludge is subjected to absorption of an internal carbon source, and only stirring is needed, so that the sewage stays for 6 hours. The aerobic tanks consist of a plurality of dynamic aerobic tanks, each dynamic aerobic tank is connected by a pipeline, the HRT of each dynamic aerobic tank is provided with aeration equipment, stirring equipment, a pH detector and a dissolved oxygen detector, the pH detector and the DO detector are connected with a PLC, and finally the aeration equipment is controlled by a computer. The dissolved oxygen of the dynamic aerobic tanks is controlled to be 2-4 mg/L, when one dynamic aerobic tank is detected that the dissolved oxygen is lower than 30% of the normal aeration amount, the dissolved oxygen is still higher than 4mg/L, and the condition that the pH value is increased at the moment indicates that the system nitrification is completed, and the dynamic aerobic tanks and the subsequent dynamic aerobic tanks automatically close the aeration. The HRT of all dynamic aerobic tanks is counted for 12 hours, and the retention time of the dynamic aerobic tanks is controlled to be 9-12 hours according to the needs. An anoxic tank is connected behind the dynamic aerobic tank, and is mainly used for completing endogenous denitrification for deep denitrification. The stay time of the anoxic tank is 12 hours, and only stirring is needed. The sludge at the tail end of the anoxic tank flows back to the anaerobic tank, and the sludge reflux ratio is 100%; the water conservancy residence time of the whole biochemical stage is 30 hours, sewage finally enters an MBR membrane tank for mud-water separation, supernatant fluid is discharged, sludge is pumped back to the forefront end of a dynamic aerobic tank through a sludge pump, the sludge reflux ratio is 50%, and residual sludge is discharged into a sludge concentration tank.
Example 3: front-mounted dephosphorization rear-mounted endogenous denitrification coupling MBR sewage treatment system
As shown in FIG. 1, the sewage treatment system of the front-end dephosphorization and rear-end endogenous denitrification coupling MBR comprises a sand sedimentation tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank; the grit chamber, the flocculation precipitation dephosphorization tank, the anaerobic tank, the dynamic aerobic tanks, the anoxic tanks, the MBR membrane tank and the sludge concentration tank are communicated through pipelines; the flocculation precipitation dephosphorization pool is communicated with the sludge concentration pool through a pipeline, and the pipeline is provided with a sludge pump; the MBR membrane pond is connected with a sludge reflux system, the sludge reflux system comprises a pre-anaerobic pond, the pre-anaerobic pond is respectively communicated with the MBR membrane pond and the flocculation precipitation dephosphorization pond through pipelines, the pipelines are all provided with sludge reflux pumps, the pre-anaerobic pond is simultaneously communicated with an anaerobic pond water inlet through the pipelines, stirrers and aeration equipment are respectively arranged in the anaerobic pond and the anoxic pond, the dynamic aerobic pond is respectively provided with a PH detector and a DO detector, and the PLC is respectively in communication connection with the PH detector, the DO detector, the aeration equipment and the stirrers.
The invention relates to a prepositive dephosphorization postpositive endogenous denitrification sewage treatment system which mainly comprises three main parts: the sewage treatment process of the front phosphorus removal part, the rear endogenous denitrification part, the MBR membrane tank and the sludge reflux part is as follows:
(1) front dephosphorization
The advanced dephosphorization fully utilizes the characteristic of high suspended matters in the water inlet of the primary sedimentation tank by adding the efficient dephosphorization agent, so that the materialized dephosphorization is performed to the maximum extent, the total phosphorus content of the water inlet of the biochemical section is reduced, and the subsequent denitrification effect is further ensured.
Through the treatment of the process section, the total phosphorus in the sewage can basically realize up-to-standard discharge, and the subsequent biochemical section only needs to treat COD and total nitrogen in the sewage.
(2) Post endogenous denitrification
The theoretical basis of post endogenous denitrification is that denitrifying bacteria have the characteristic of storing carbon sources, the endogenous denitrification potential of the denitrifying bacteria is huge, and the main factors influencing the endogenous denitrification effect are anaerobic stirring time after water inflow, dissolved oxygen concentration during aeration, nitrification time and the like. The anaerobic stirring time is generally controlled to about 1 hour, and generally not more than 2 hours. At this stage, the denitrifying bacteria can adsorb and absorb organic matters in the sewage.
The sewage enters a dynamic aerobic tank, the concentration of dissolved oxygen during aeration is controlled to be 2mg/L-4mg/L, and meanwhile, in order to shorten the nitrification time as much as possible, the time for over-aeration needs to be reduced. In order to realize accurate aeration of sewage, a plurality of relatively independent dynamic aerobic tanks (each dynamic aerobic tank is connected through a pipeline and is approximately and completely mixed) are arranged, a DO detector and a pH detector are arranged in each dynamic aerobic tank, whether the system is nitrified is finished or not can be judged by observing the change of the pH value and the DO of the dynamic aerobic tank (when the nitrifying is finished, the activity of nitrifying bacteria is reduced, the oxygen consumption is reduced, the Dissolved Oxygen (DO) of the sewage relatively rises, the alkalinity in the sewage is consumed due to the nitrifying effect, the pH value of the dynamic aerobic tanks gradually falls, the pH value gradually rises after the nitrifying is finished, and when one dynamic aerobic tank is detected that the dissolved oxygen is still higher than 4mg/L when the aeration amount is lower than 30% of the normal aeration amount, and under the condition that the pH value rises, the nitrifying of the system is finished, the dynamic aerobic tanks and the subsequent dynamic aerobic Chi Bianke can stop aeration, namely the energy is saved, and the nitrifying is ensured to be complete in the shortest time.
Enters an anoxic tank, and deep denitrification is realized through the endogenous denitrification of denitrifying bacteria.
(3) MBR membrane tank and sludge return part
In order to solve the problems that suspended matters in the effluent exceed standard and the concentration of the sludge cannot be adjusted, an MBR membrane tank is adopted to replace a traditional secondary sedimentation tank, so that suspended solids reach the standard, a subsequent filtering process is omitted, the sludge age of a sewage treatment system can be prolonged, and the denitrification effect of the sewage treatment system is improved. In order to ensure the effect of absorbing carbon sources by the anaerobic section, the sludge concentration of the MBR membrane tank is maintained, the function of the anaerobic tank is not destroyed, the sludge of the MBR membrane tank is returned to the pre-anaerobic tank, the water inflow of the pre-anaerobic tank is 10% of the total water amount, the purpose is to consume dissolved oxygen in the returned sludge of the MBR tank, and then the water outflow of the pre-anaerobic tank enters the anaerobic tank.
The COD, ammonia nitrogen, total phosphorus and suspended solids of the treated effluent of the sewage treatment system all reach the standard.
Example 4: front-phosphorus-removal rear-endogenous denitrification coupling MBR sewage treatment process
The process in the embodiment is based on the system in the embodiment 3, is mainly used for treating municipal sewage, and mainly adopts the water inflow index of COD2000 mg/L-2200 mg/L, ammonia nitrogen 360 mg/L-450 mg/L and total phosphorus 10 mg/L-20 mg/L. Sewage is treated by a grit chamber and then enters a flocculation precipitation dephosphorization tank, is mixed with a flocculation dephosphorization agent added into the tank, then mud-water separation is realized, 90% of supernatant enters an anaerobic section of a biochemical stage, 10% of supernatant enters a pre-anaerobic tank, and precipitated sludge enters a sludge concentration tank. The flocculating dephosphorizing agent can use PAC or PFC, the dosage of the PAC or PFC is 50mg/L to 200mg/L according to the water quality condition, the total phosphorus removal rate of the process section is more than 90 percent, and the total phosphorus of the effluent is controlled to be 0.3mg/L to 1mg/L. After sewage enters the anaerobic tank, activated sludge is subjected to absorption of an internal carbon source, and only stirring is needed, so that the sewage stays for 6 hours. The aerobic tanks consist of a plurality of dynamic aerobic tanks, each dynamic aerobic tank is connected by a pipeline, the HRT of each dynamic aerobic tank is provided with aeration equipment, stirring equipment, a pH detector and a dissolved oxygen detector, the pH detector and the DO detector are connected with a PLC, and finally the aeration equipment is controlled by a computer. The dissolved oxygen of the dynamic aerobic tanks is controlled to be 2-4 mg/L, when one dynamic aerobic tank is detected that the dissolved oxygen is lower than 30% of the normal aeration amount, the dissolved oxygen is still higher than 4mg/L, and the condition that the pH value is increased at the moment indicates that the system nitrification is completed, and the dynamic aerobic tanks and the subsequent dynamic aerobic tanks automatically close the aeration. The HRT of all dynamic aerobic tanks is counted for 12 hours, and the retention time of the dynamic aerobic tanks is controlled to be 9-12 hours according to the needs. An anoxic tank is connected behind the dynamic aerobic tank, and is mainly used for completing endogenous denitrification for deep denitrification. The stay time of the anoxic tank is 12 hours, and only stirring is needed. The water conservancy residence time of the whole biochemical stage is 30 hours, sewage finally enters an MBR membrane tank for mud-water separation, supernatant fluid is discharged, sludge is pumped back to a pre-anaerobic tank through a sludge pump, the sludge reflux ratio is 100%, and residual sludge is discharged into a sludge concentration tank.
Example 5: industrial sewage treatment based on front-end dephosphorization and rear-end endogenous denitrification coupling MBR sewage treatment system with different sludge backflow modes
The embodiment is provided with a control group, and the sewage treatment system of the control group is shown in figure 3, and specifically comprises a sand setting tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank which are communicated through pipelines in sequence; the flocculation precipitation dephosphorization pool is communicated with the sludge concentration pool through a pipeline, and the pipeline is provided with a sludge pump; the MBR membrane tank is communicated with the front end of the anaerobic tank through a pipeline and a sludge reflux pump; the anaerobic tank and the anoxic tank are respectively provided with a stirrer, the dynamic aerobic tank is respectively internally provided with a stirrer and an aeration device, the dynamic aerobic tank and the anoxic tank are respectively provided with a PH detector and a DO detector, and the PLC is respectively in communication connection with the PH detector, the DO detector, the aeration device and the stirrer.
To verify the technical effects of the sewage treatment system and process of the present invention, the sewage treatment process of the present invention was employed to test the sewage treatment effect based on the control group sewage treatment system and the sewage treatment systems of example 1 and example 3, respectively.
In this embodiment, the sewage treatment system of the control group and the sewage treatment systems of embodiment 1 and embodiment 3 are combined into one sewage treatment system, and the sewage treatment functions of the sewage treatment systems of the control group and the sewage treatment systems of embodiment 1 and embodiment 3 are realized by selecting different backflow modes. Namely, the sewage treatment system of the embodiment specifically comprises a sand setting tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank; the system comprises a grit chamber, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank; the MBR membrane tank is communicated with the front end of the anaerobic tank through a pipeline and a sludge reflux pump; the MBR membrane tank is also communicated with the forefront end of the dynamic aerobic tank through a pipeline and a sludge reflux pump, and meanwhile, the forefront end of the anoxic tank is communicated with the front end of the anaerobic tank through a pipeline, and the pipeline is provided with the sludge reflux pump; the anaerobic treatment device is characterized by further comprising a pre-anaerobic tank, wherein the pre-anaerobic tank is respectively communicated with the MBR membrane tank and the flocculation precipitation dephosphorization tank through pipelines, the pipelines are provided with sludge reflux pumps, and the pre-anaerobic tank is simultaneously communicated with a water inlet of the anaerobic tank through the pipelines; the anaerobic tank and the anoxic tank are respectively provided with a stirrer, the dynamic aerobic tank is respectively internally provided with a stirrer and an aeration device, the dynamic aerobic tank and the anoxic tank are respectively provided with a PH detector and a DO detector, and the PLC is respectively in communication connection with the PH detector, the DO detector, the aeration device and the stirrer. In this embodiment, by closing and opening different pipelines and sludge reflux pumps, the sewage treatment system is operated in three sludge reflux modes respectively, including the direct reflux of sludge from an MBR membrane tank to an anaerobic tank (a control group sewage treatment system, as shown in FIG. 3), the reflux of sludge from an MBR membrane tank to an aerobic tank and the reflux of sludge from an anoxic tank to an anaerobic section (an example 1 sewage reflux system, as shown in FIG. 1) and the reflux of sludge from an MBR membrane tank to a pre-anaerobic tank ((an example 3 sewage reflux system, as shown in FIG. 2))
By adopting the sewage treatment system and adopting the sewage treatment process disclosed by the invention to treat certain industrial sewage, the industrial sewage index is COD2000 mg/L-2200 mg/L, ammonia nitrogen is 360 mg/L-450 mg/L, and total phosphorus is 10 mg/L-20 mg/L. The hydraulic retention time of the anaerobic, aerobic and anoxic sections of the three groups of sewage treatment processes is the same and is 45 hours. Wherein, the group of pre-anoxic tanks is adopted, and the pre-anoxic residence time is 2 hours. After the sewage passes through the dephosphorization sedimentation tank, the total phosphorus concentration of the sewage is stabilized below 1mg/L, the removal rate reaches more than 95 percent, and the dephosphorization effect is very stable. The three operation modes have basically the same condition of removing the ammonia nitrogen in the sewage, the concentration of the ammonia nitrogen in the effluent is less than 1mg/L, and the removal rate reaches more than 99%. The removal rates of COD and total nitrogen are shown in fig. 4 and 5. As can be seen from FIG. 4, the three groups of systems have very similar removal rates of COD in sewage, the concentration of effluent is maintained at about 300mg/L, the removal rate is stabilized at more than 85%, and the three groups have no obvious difference. As can be seen from FIG. 5, in the first mode, the absorption effect of denitrifying bacteria on carbon sources is reduced due to too high dissolved oxygen in the sludge reflux liquid, the total nitrogen concentration of the final effluent of the system is kept to be about 90mg/L, and the total nitrogen removal rate is 72% -80%. And (3) changing a reflux mode from day 16, wherein the sludge in the MBR membrane tank is refluxed to the aerobic zone, and the sludge at the tail end of the anoxic zone is refluxed to the front end of the anaerobic tank. By changing reflux, denitrifying bacteria in the sludge can fully absorb organic matters in sewage, synchronous nitrification and denitrification and endogenous denitrification effects of the system are enhanced, total nitrogen concentration of effluent is gradually reduced, the final total nitrogen concentration of the effluent is stabilized to about 30mg/L, and the total nitrogen removal rate is stabilized to about 92%. From day 31, the return mode of the sludge is switched to return only from the MBR membrane tank, the sludge is completely returned to the pre-anaerobic tank, 10% of the inlet water enters the pre-anaerobic tank, and 90% enters the normal anaerobic tank. The data shows that after the operation mode is switched, the total nitrogen concentration of the effluent is not obviously changed, the effluent is stabilized at about 30mg/L, and the total nitrogen removal rate is more than 92%. Therefore, in the three sludge reflux modes, the denitrification effect of the sewage treatment system in which the sludge in the MBR membrane pond of the control group directly flows back to the anaerobic pond is the worst, and the total nitrogen removal rate of the effluent is lower than 80 percent, and the main reason is that after the direct reflux, a large amount of dissolved oxygen damages the anaerobic state of the anaerobic lattice of the system, and the absorption of denitrifying bacteria to carbon sources is influenced. Based on the prepositive dephosphorization postpositive endogenous denitrification sewage treatment system, the denitrification efficiency of the system can be effectively ensured by changing the reflux mode of sludge or changing the water inlet mode.
In summary, the two combined treatment processes designed by the invention are adopted to treat certain industrial sewage with COD of 2000-2200 mg/L, ammonia nitrogen of 360-450 mg/L and total phosphorus of 10-20 mg/L, and the removal rates of the effluent COD, total nitrogen and total phosphorus are about 300m/L, 30mg/L and 1mg/L respectively, and are respectively above 82%, 92% and 95%.
The foregoing embodiments are merely examples of the present invention, and the scope of the present invention includes, but is not limited to, the forms and styles of the foregoing embodiments, and any suitable changes or modifications made by those skilled in the art, which are consistent with the claims of the present invention, shall fall within the scope of the present invention.
Claims (10)
1. The utility model provides a leading post endogenous denitrification coupling MBR sewage treatment system of dephosphorization which characterized in that: comprises a sand setting tank, a flocculation precipitation dephosphorization tank, an anaerobic tank, a plurality of dynamic aerobic tanks, a plurality of anoxic tanks, an MBR membrane tank and a sludge concentration tank;
the grit chamber, the flocculation precipitation dephosphorization tank, the anaerobic tank, the dynamic aerobic tanks, the anoxic tanks, the MBR membrane tank and the sludge concentration tank are sequentially communicated through pipelines;
the flocculation precipitation dephosphorization pond is communicated with the sludge concentration pond through a pipeline, and the pipeline is provided with a sludge pump.
The MBR membrane tank is connected with a sludge reflux system;
the anaerobic tank and the anoxic tank are respectively provided with a stirrer, and the dynamic aerobic tank is respectively provided with an aeration device and a stirrer.
2. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment system according to claim 1, wherein the sludge recirculation system comprises a pipeline connected with the front ends of the MBR membrane tank and the dynamic aerobic tank and a sludge pump.
3. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment system according to claim 2, wherein the tail end of the anoxic tank is communicated with the front end of the anaerobic tank through a pipeline, and the pipeline is provided with a sludge reflux pump.
4. The prepositive dephosphorization post-endogenous denitrification coupling MBR sewage treatment system according to claim 1, wherein the sludge reflux system comprises a pre-anaerobic tank which is respectively communicated with an MBR membrane tank and a flocculation precipitation dephosphorization tank through pipelines, and the pipelines are provided with sludge reflux pumps; the pre-anaerobic tank is communicated with the water inlet of the anaerobic tank through a pipeline.
5. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment system according to any one of claims 1 to 4, wherein: the dynamic aerobic tank and the anoxic tank are respectively provided with a PH detector and a DO detector;
the sewage treatment system further comprises a PLC controller, and the PLC controller is respectively in communication connection with the PH detector, the DO detector, the aeration equipment and the stirrer.
6. A sewage treatment process of a prepositive dephosphorization postpositive endogenous denitrification coupling MBR is characterized in that:
s1: sewage is treated by a primary sedimentation tank and then enters a flocculation sedimentation dephosphorization tank, the sewage is mixed with a flocculation dephosphorization agent added into the flocculation sedimentation dephosphorization tank, mud-water separation is realized, supernatant fluid enters an anaerobic tank, and precipitated sludge enters a sludge concentration tank;
s2: after sewage enters an anaerobic tank for mixing, the anaerobic tank is stirred, denitrifying bacteria absorb carbon sources, and the retention time is T 1 Hours;
s3: the effluent of the anaerobic tank enters a plurality of dynamic aerobic tanks, and the retention time of each dynamic aerobic tankIs T 2 The nitrification is carried out under the action of stirring aeration for hours, and ammonia nitrogen and residual organic matters in the sewage are degraded; when the last dynamic aerobic tank dissolved oxygen is detected to be lower than 30% of the normal aeration rate, and the dissolved oxygen is still higher than 4mg/L, under the condition that the pH value is increased at the moment, the dynamic aerobic tank and the subsequent dynamic aerobic tanks automatically close the aeration to become an anoxic tank, and the anoxic tank is only provided with a stirrer;
s4: sewage entering the anoxic tank, wherein the total residence time of the anoxic tank is T 3 For an hour, denitrification is realized by the endogenous denitrification of denitrifying bacteria;
s5: sewage in the anoxic tank enters the MBR membrane tank after being discharged, sludge-water separation is realized, the sludge flows back to the front end of the anaerobic tank or the dynamic aerobic tank through the sludge backflow system, the residual sludge is discharged into the sludge concentration tank, and the supernatant is discharged.
7. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment process as recited in claim 6, wherein the process is characterized in that: in the step S5, the sludge in the MBR membrane pond flows back to the front end of the dynamic aerobic pond, and the reflux ratio is 50%; the tail end sludge of the anoxic tank flows back to the front end of the anaerobic tank, and the reflux ratio is 100%.
8. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment process as recited in claim 6, wherein the process is characterized in that: 10% of the water discharged from the flocculation precipitation dephosphorization tank enters a pre-anaerobic tank, and the rest of the water enters an anaerobic tank; in the step S5, the sludge in the MBR membrane pond flows back to the pre-anaerobic pond, and the backflow ratio is 100%; the effluent of the pre-anaerobic tank enters the anaerobic tank.
9. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment process according to any one of claims 6 to 8, wherein: the flocculating dephosphorizing agent is PAC or PFC, and the dosage of the PAC or PFC is 50 mg/L-200 mg/L; the T is 1 0.5-2, said T 2 2-3, said T 3 8-12; the concentration of dissolved oxygen in the aeration of the dynamic aerobic tank is controlled to be 2mg/L-4mg/L.
10. The pre-dephosphorization post-endogenous denitrification coupling MBR sewage treatment process as recited in claim 9, wherein the process is characterized in that: and when the carbon-nitrogen ratio of the inlet water of the anaerobic tank is less than 3, adding a carbon source into the anaerobic tank.
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