CN119219199B

CN119219199B - Method for simultaneous biological nitrogen and phosphorus removal using MABR

Info

Publication number: CN119219199B
Application number: CN202411755201.2A
Authority: CN
Inventors: 杨海亮; 陆美杰; 周新宇; 李宇萌; 胡洋; 徐敏; 陆敏明
Original assignee: Suzhou Kete Environmental Protection Co ltd
Current assignee: Suzhou Kete Environmental Protection Co ltd
Priority date: 2024-12-03
Filing date: 2024-12-03
Publication date: 2025-03-21
Anticipated expiration: 2044-12-03
Also published as: CN119219199A

Abstract

The present invention discloses a method for synchronous biological denitrification and phosphorus removal using MABR, wherein the original wastewater is divided into two parts and respectively introduced into the denitrification zone and the dephosphorization zone in the sewage treatment system, and the amount of wastewater entering the denitrification zone is greater than the amount of wastewater entering the dephosphorization zone; the denitrification zone is provided with a plurality of MABR membrane modules, the dissolved oxygen concentration of the denitrification zone is monitored, and the dissolved oxygen concentration of the denitrification zone is maintained at 0.1mg/L to 0.3mg/L, and the effluent of the denitrification zone enters the dephosphorization zone; the dissolved oxygen concentration of the dephosphorization zone is monitored, and the dissolved oxygen concentration of the dephosphorization zone is maintained at 2mg/L to 4mg/L; the effluent of the dephosphorization zone enters the solid-liquid separation zone, and the supernatant of the solid-liquid separation zone is refluxed to the denitrification zone, and part of the sludge at the bottom of the solid-liquid separation zone is discharged from the system as residual sludge, and part of it is refluxed to the dephosphorization zone. The method for synchronous biological denitrification and phosphorus removal using MABR provided by the present invention can improve the efficiency of sewage treatment.

Description

Method for synchronous biological denitrification and dephosphorization by MABR

Technical Field

The invention relates to the technical field of sewage treatment, in particular to a method for synchronous biological denitrification and dephosphorization by adopting MABR.

Background

The nitrogen and phosphorus in sewage (waste) water are main elements affecting the quality of water, biological treatment is a low-cost and environment-friendly treatment method, various nitrogen and phosphorus removal processes are created, mainly including a Balatu synchronous nitrogen and phosphorus removal process, an A-A-O synchronous nitrogen and phosphorus removal process, a biological rotating disc synchronous nitrogen and phosphorus removal process and the like, and most of the biological treatment processes are single activated sludge method or biological membrane method.

As is known, the denitrifying microorganism needs long sludge age (20-25 d), while the dephosphorizing microorganism needs short sludge age (3-5 d), which causes contradiction between denitrification and dephosphorization, in general, the control condition of biological denitrification is relatively harsh and is relatively difficult to realize, and dephosphorization can be assisted by chemical agents, so that the conventional biological treatment mainly comprises biological denitrification, the sludge age of a biological treatment system is ensured to be longer, the biological dephosphorization effect is sacrificed, and chemical dephosphorization is adopted to assist in realizing high-standard emission requirements (the total phosphorus is less than 0.5mg/L or 0.3mg/L, even 0.1 mg/L).

Synchronous denitrification and dephosphorization are carried out by a single activated sludge method, the sludge age is long, the sludge concentration is high, more carbon sources are consumed, the carbon-nitrogen ratio is unbalanced, a certain additional carbon source is needed to be added for denitrification, the required operation condition is more severe, the operation and management are more complicated, the level required by a manager is higher, only part of phosphorus is removed by the assimilation of microorganisms, the biological dephosphorization effect is very low, and the removal rate is only 10% -20%.

The single biomembrane method is used for denitrification and dephosphorization, the sludge yield is low, the denitrification effect is good, but the total phosphorus is difficult to effectively remove in the form of sludge, so that the biological dephosphorization effect is still not high, the treatment load of the biomembrane method is low, the treatment scale is limited, and the method is not suitable for large-scale sewage treatment plants.

Disclosure of Invention

The invention aims to provide a method for synchronous biological nitrogen and phosphorus removal by MABR, which can relieve the contradiction between long sludge age required by biological nitrogen removal and short sludge age required by biological phosphorus removal, improve the effects of nitrogen removal and phosphorus removal, reduce the addition of carbon sources and phosphorus removal agents, and reduce the energy consumption and the sludge yield.

Based on the problems, the technical scheme provided by the invention is as follows:

adopts MABR to carry out synchronous biological denitrification and dephosphorization,

The method comprises the steps of respectively introducing wastewater raw water into a denitrification area and a dephosphorization area in a sewage treatment system in two parts, wherein the amount of wastewater entering the denitrification area is larger than that entering the dephosphorization area;

The denitrification region is provided with a plurality of MABR membrane components, the dissolved oxygen concentration of the denitrification region is monitored, the dissolved oxygen concentration of the denitrification region is kept to be 0.1 mg/L-0.3 mg/L, when the dissolved oxygen concentration does not meet the requirement, the air supply quantity of the plurality of MABR membrane components is regulated, and the effluent water of the denitrification region enters the dephosphorization region;

An aerator and a flow impeller are arranged in the dephosphorization region, the dissolved oxygen concentration of the dephosphorization region is monitored, the dissolved oxygen concentration of the dephosphorization region is kept to be 2 mg/L-4 mg/L, and when the dissolved oxygen concentration does not meet the requirement, the oxygen supply of the aerator is regulated;

The effluent of the dephosphorization zone enters a solid-liquid separation zone, supernatant fluid of the solid-liquid separation zone flows back to the denitrification zone, part of sludge at the bottom of the solid-liquid separation zone is discharged from a system by residual sludge, and the other part of sludge flows back to the dephosphorization zone;

monitoring the total nitrogen concentration of the discharged water of the solid-liquid separation zone, and increasing the reflux ratio of the supernatant to the denitrification zone when the total nitrogen concentration in the discharged water is greater than a discharge requirement value;

Monitoring the total phosphorus concentration of the discharged water of the solid-liquid separation zone, and increasing the sludge discharge amount when the total phosphorus concentration in the discharged water is greater than a discharge requirement value;

monitoring the sludge concentration of the dephosphorization zone, and controlling the sludge concentration by controlling the sludge reflux quantity;

and monitoring the COD concentration of the dephosphorization zone, and ensuring that the COD/TP in the dephosphorization zone is more than 17 by adjusting the amount of wastewater raw water entering the dephosphorization zone.

In some embodiments, the amount of wastewater entering the denitrification region is 80-90% of the total amount of wastewater raw water, and the amount of wastewater entering the dephosphorization region is 10-20% of the total amount of wastewater raw water.

In some embodiments, the sludge reflux ratio is 30% -50% of the total amount of the wastewater raw water.

In some embodiments, the supernatant reflux ratio is 20% -50% of the total amount of the wastewater raw water.

In some embodiments, the sewage treatment system comprises an MABR membrane pond, an aerobic pond and a solid-liquid separation pond which are communicated with each other;

the MABR membrane pond is the denitrification area, a plurality of MABR membrane modules and a first dissolved oxygen monitor are arranged in the MABR membrane pond, the MABR membrane modules are connected to a gas supply pipeline, and a process gas fan, a process gas flowmeter and a process gas regulating valve are sequentially arranged on the gas supply pipeline along the gas inlet direction;

The aerobic tank is the dephosphorization zone, the aerator and the impeller are arranged at the bottom of the aerobic tank, the aerator is connected to an aeration pipeline, an aeration fan, an aeration flowmeter and an aeration regulating valve are sequentially arranged on the aeration pipeline along the air inlet direction, and the dephosphorization zone is provided with a second dissolved oxygen monitor and a sludge concentration monitor;

Be equipped with total nitrogen on-line monitoring appearance and total phosphorus on-line monitoring appearance in the solid-liquid separation pond, solid-liquid separation pond upper portion is connected to through the supernatant back flow MABR membrane pond, be equipped with supernatant backwash pump and supernatant backwash valve on the supernatant back flow in proper order along the rivers direction, the solid-liquid separation pond bottom is connected with the mud back flow, be equipped with mud backwash pump and backward flow mud governing valve on the mud back flow in proper order along the mud discharge direction, the mud back flow still is connected with the mud drain pipe, be equipped with mud discharge governing valve on the mud drain pipe.

In some embodiments, the dephosphorization zone is provided with a COD on-line monitor.

In some embodiments, the denitrification area and the dephosphorization area are connected to a water inlet pipe, and a raw water regulating valve is arranged on a water inlet pipe section connected with the dephosphorization area.

In some embodiments, the MABR membrane tank and the aerobic tank are separated by a partition plate, and a through hole which is communicated with the denitrification area and the dephosphorization area is arranged at the bottom of the partition plate.

Compared with the prior art, the invention has the advantages that:

1. the denitrification area and the dephosphorization area respectively adopt a biological membrane method and an activated sludge method in an MABR (mechanical biological reactor) form, the biological denitrification and biological dephosphorization functions are basically independent, the long sludge age required by denitrification and the short sludge age required by dephosphorization can be controlled respectively, and the operation is simple;

2. the biological denitrification efficiency can reach more than 90%, the biological dephosphorization efficiency is 50% -70%, and is higher than 80% and 20% of that of a single activated sludge method or a single biological membrane method;

3. Multiple denitrification functions such as synchronous nitrification and denitrification, short-cut nitrification and denitrification, nitrosation-anaerobic ammoxidation and the like can be realized by controlling the oxygen supply quantity in the MABR membrane cavity, the denitrification removal efficiency is stable, the removal rate is high, and the impact of water quality, water quantity and water temperature can be treated;

4. The biological membrane has unique structure of internal nitrification and external denitrification of MABR, and oxygen, ammonia nitrogen and COD are reversely transferred, so that the self carbon source of the wastewater is fully utilized, and no additional carbon source is needed;

5. The COD removal rate of the MABR in the denitrification zone can reach 80% -90%, the COD entering the dephosphorization zone is low, and the sludge yield is low;

6. The phosphorus removal section has triple phosphorus removal functions of assimilation, sludge adsorption and phosphorus absorption of phosphorus accumulating bacteria, the biological phosphorus removal efficiency can reach 50% -70%, compared with a single activated sludge method or a single biological membrane method, the total phosphorus is removed by only assimilation, the biological phosphorus removal efficiency is improved by 30% -60%, and the adding amount of a phosphorus removal agent required by chemical phosphorus removal by 30% -60% and the sludge yield caused by the adding amount can be reduced;

7. The total nitrogen and total phosphorus concentration of the effluent are automatically monitored, the reflux proportion of supernatant or sludge is flexibly adjusted, the effluent quality is stable, and the standard guarantee rate is high.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described below, in which the drawings are only some embodiments of the present invention, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.

FIG. 1 is a schematic diagram of an embodiment of a wastewater treatment system according to the present invention employing MABR for simultaneous biological nitrogen and phosphorus removal;

Wherein:

1. The device comprises an MABR membrane pond, a2, an aerobic pond, a 3, a solid-liquid separation pond, a 4, an MABR membrane module, a 5, a water inlet pipe, a 6, a raw water regulating valve, a 7, a gas supply pipeline, a 8, a process gas fan, a 9, a process gas flowmeter, a 10, a process gas regulating valve, a 11, a first dissolved oxygen monitor, a 12, an aerator, a 13, a pusher, a 14, an aeration pipeline, a 15, an aeration fan, a 16, an aeration flowmeter, a 17, an aeration regulating valve, a 18, a second dissolved oxygen monitor, a 19, a COD on-line monitor, a 20, a sludge concentration monitor, a 21, a total nitrogen on-line monitor, a 22, a total phosphorus on-line monitor, a 23, a supernatant return pipe, a 24, a supernatant return pump, a 25, a supernatant return regulating valve, a 26, a return sludge, a 27, a sludge return pump, a 28, a return sludge regulating valve, a 29, a sludge discharge pipe, a 30, a sludge discharge regulating valve, a 31 and a partition plate.

Detailed Description

The above-described aspects are further described below in conjunction with specific embodiments. It should be understood that these examples are illustrative of the present invention and are not intended to limit the scope of the present invention. The implementation conditions used in the examples may be further adjusted according to the conditions of the specific manufacturer, and the implementation conditions not specified are generally those in routine experiments.

Referring to fig. 1, for a schematic structural diagram of an embodiment of the present invention, a sewage treatment system related to a method for performing synchronous biological denitrification and dephosphorization by using an MABR is provided, which includes an MABR membrane tank 1, an aerobic tank 2 and a solid-liquid separation tank 3 that are mutually communicated, wherein both the MABR membrane tank 1 and the aerobic tank 2 are connected to a water inlet pipe 5, i.e. wastewater and raw water enter the MABR membrane tank 1 and the aerobic tank 2 respectively in two parts.

The MABR membrane pond 1 is the denitrification region and is internally provided with a plurality of MABR membrane modules 4 and a first dissolved oxygen monitor 11, the plurality of MABR membrane modules 4 are connected to a gas supply pipeline 7, a process gas fan 8, a process gas flowmeter 9 and a process gas regulating valve 10 are sequentially arranged on the gas supply pipeline 7 along the gas inlet direction, oxygen is introduced into a membrane cavity of the MABR membrane module 4 by the process gas fan 8, the concentration of the dissolved oxygen in the MABR membrane pond 1 is monitored by the first dissolved oxygen monitor 11, and the gas inflow of the oxygen is regulated by the process gas regulating valve 10 so as to control the concentration of the dissolved oxygen in the MABR membrane pond 1.

The aerobic tank 2 and the MABR membrane tank 1 are separated by a baffle plate 31, a through hole for communicating the MABR membrane tank 1 and the aerobic tank 2 is arranged at the bottom of the baffle plate 31, and effluent treated by the MABR membrane tank 1 enters the aerobic tank 2.

The aerobic tank 2 is a dephosphorization zone, an aerator 12 and a flow impeller 13 are arranged at the bottom of the aerobic tank 2, so that a mud-water mixture is fully mixed in the horizontal direction and the vertical direction, the aerator 12 is connected to an aeration pipeline 14, an aeration fan 15, an aeration flowmeter 16 and an aeration regulating valve 17 are sequentially arranged on the aeration pipeline 14 along the air inlet direction, a second dissolved oxygen monitor 18 and a sludge concentration monitor 20 are arranged in the dephosphorization zone, the dissolved oxygen of the dephosphorization zone is monitored by the second dissolved oxygen monitor 18 so as to regulate the air quantity of the aerator 12, and the sludge concentration of the dephosphorization zone is monitored by the sludge concentration monitor 20 so as to regulate the sludge reflux quantity.

The solid-liquid separation tank 3 is connected with the aerobic tank 2 through a pipeline, a total nitrogen on-line monitor 21 and a total phosphorus on-line monitor 22 are arranged in the solid-liquid separation tank 3, the upper part of the solid-liquid separation tank 3 is connected with the MABR membrane tank 1 through a supernatant return pipe 23, a supernatant return pump 24 and a supernatant return regulating valve 25 are arranged on the supernatant return pipe 23 along the water flow direction, a sludge return pipe 26 is connected at the bottom of the solid-liquid separation tank 3, a sludge return pump 27 and a return sludge regulating valve 28 are sequentially arranged on the sludge return pipe 26 along the sludge discharge direction, a sludge discharge pipe 29 is further connected with the sludge return pipe 26, and a sludge discharge regulating valve 30 is arranged on the sludge discharge pipe 29.

In order to further optimize the implementation effect of the invention, the COD on-line monitor 19 is arranged in the phosphorus removal zone so as to ensure that the phosphorus removal zone has a certain concentration of organic matters, thereby meeting the growth requirement of phosphorus accumulating bacteria, and when the concentration of the organic matters can not meet the growth requirement of phosphorus accumulating bacteria, the wastewater inflow of the phosphorus removal zone can be increased. The denitrification area and the dephosphorization area are both connected to a water inlet pipe 5, a raw water regulating valve 6 is arranged on a water inlet pipe section connected with the dephosphorization area, and the wastewater inflow of the dephosphorization area is regulated by the raw water regulating valve 6 so as to meet the energy requirement of phosphorus accumulating bacteria.

The sewage treatment method of the sewage treatment system comprises the following steps:

The wastewater raw water is respectively introduced into a denitrification area and a dephosphorization area in a wastewater treatment system in two parts, and the wastewater amount entering the denitrification area is larger than that entering the dephosphorization area;

monitoring the dissolved oxygen concentration of the denitrification region, keeping the dissolved oxygen concentration of the denitrification region to be 0.1 mg/L-0.3 mg/L, and adjusting the air supply amount of the MABR membrane modules when the dissolved oxygen concentration does not meet the requirement;

Monitoring the dissolved oxygen concentration of the dephosphorization zone, keeping the dissolved oxygen concentration of the dephosphorization zone to be 2 mg/L-4 mg/L, and adjusting the oxygen supply of the aerator when the dissolved oxygen concentration does not meet the requirement;

The effluent of the dephosphorization zone enters a solid-liquid separation zone, supernatant fluid of the solid-liquid separation zone flows back to the denitrification zone, part of sludge at the bottom of the solid-liquid separation zone is discharged out of the system by residual sludge, and the other part flows back to the dephosphorization zone;

The amount of wastewater entering the denitrification zone is 80-90% of the total amount of raw wastewater, the amount of wastewater entering the dephosphorization zone is 10-20% of the total amount of raw wastewater, and the amounts of wastewater in the denitrification zone and the dephosphorization zone are regulated according to the COD concentration in the wastewater.

The MABR arrangement of the denitrification area adopts a whole membrane method, namely a whole biological membrane method, the suspended matters (SS) of the mixed solution are smaller than 200mg/L, the sludge age is 25-35 days, the Hydraulic Retention Time (HRT) is different according to the total nitrogen concentration of raw water, and the HRT of common municipal domestic sewage is 12-18 h. And (3) industrial wastewater, wherein the HRT is 24-96 h. The nitrifying rate of the MABR membrane component is kept at 2-5 g/(m 2. D), and the dissolved oxygen of the mixed solution is less than 0.3mg/L. The total nitrogen removal rate of the zone is 85% -90%, the ammonia nitrogen removal rate is more than 95%, and the COD removal rate is more than 90%. The MABR membrane component is provided with a gas stripping mixing unit, and utilizes the tail gas of the process gas as gas stripping power to carry out up-and-down circulation and mixing.

The dephosphorization area adopts an activated sludge process, for general municipal sewage, the sludge concentration MLSS is ensured to be 4000-5000 mg/L, a certain sludge adsorption dephosphorization effect is ensured, the sludge age is 2-4 days, and the sludge age is controlled specifically according to the total phosphorus concentration of the discharged water. The dissolved oxygen in the region is 2-4 mg/L, so that the aerobic environment required by phosphorus absorption of the phosphorus accumulating bacteria is ensured, meanwhile, COD/TP is ensured to be more than 17, and the energy required by phosphorus absorption of the phosphorus accumulating bacteria is prevented from being influenced by too low COD. The biological phosphorus removal rate of the zone is 50% -60%.

The sludge reflux ratio is 30% -50% of the total amount of the raw water of the wastewater, the supernatant reflux ratio is 20% -50% of the total amount of the raw water of the wastewater, and the sludge reflux ratio is regulated according to the total nitrogen concentration and the total phosphorus concentration in the discharged water.

The method can treat municipal sewage with low nitrogen and phosphorus concentration, and can also treat industrial wastewater (landfill leachate, kitchen waste liquid, cultivation wastewater, sludge press liquor, starch wastewater and the like) with high nitrogen and phosphorus concentration. Aiming at the high-concentration nitrogen and phosphorus concentration waste liquid, the nitrogen nitrification rate of the MABR membrane module can reach 5-10 g/(m 2. D), the sludge concentration in the phosphorus removal area can reach 6000-800 mg/L, the adsorption phosphorus removal effect is better, and the sludge age can be reduced to 1-3 days.

The phosphorus removal area can be added with a certain amount of microorganism carriers such as activated carbon, diatomite or magnetic powder, so that the adsorption phosphorus removal effect is improved, and an activated carbon, diatomite or magnetic powder recovery device is arranged.

The method is used for treating municipal sewage, the total nitrogen removal rate is greater than 85%, the ammonia nitrogen removal rate is greater than 95%, the back end does not need to be additionally provided with a deep denitrification unit such as a denitrification filter, the total phosphorus removal rate is 50% -60%, and the back end can achieve the emission standard through a deep chemical phosphorus removal unit such as a high-efficiency sedimentation tank. When various industrial wastewater with high nitrogen and phosphorus concentration is treated, the total nitrogen removal rate is 90% -95%, the ammonia nitrogen removal rate is more than 97%, the total phosphorus removal rate is 50% -60%, and a denitrification treatment unit is basically not required. The total phosphorus can reach the discharge standard of the municipal sewer after simple chemical phosphorus removal.

The following are specific examples:

Taking 10000 tons/day municipal sewage treatment as an example, the COD of the inflow water is 400mg/L, the ammonia nitrogen is 40mg/L, the total nitrogen is 45mg/L, and the total phosphorus is 5mg/L. The amount of wastewater raw water entering the denitrification zone and the dephosphorization zone is 85% and 15%, respectively, and the sizes and control parameters of structures of the zones are described below.

The retention time of the denitrification area is 12 hours, the MABR adopts a whole membrane method, the nitrogen nitrification rate is 4 g/(m 2. D), the membrane area is 100000m2, the single membrane module is 2400m2, the process gas consumption is 24Nm3/h, the gas stripping gas consumption is 10Nm3/h, the scrubbing gas consumption is 40Nm3/h, and 42 membrane modules are required. The mixed solution on the upper surface of the denitrification area is dissolved with 0.1-0.3 mg/L of oxygen, the concentration of sludge is less than 200mg/L, and the sludge age is 30 days. The total nitrogen removal rate of the zone is more than 85%, the ammonia nitrogen removal rate is more than 95%, and the COD removal rate is more than 90%. The total nitrogen of the effluent is less than 7mg/L, the ammonia nitrogen is less than 2mg/L, and the COD is less than 40mg/L.

The sludge concentration MLSS in the dephosphorization zone is 4000mg/L, the sludge age is 3 days, the dissolved oxygen is 4mg/L, the COD/TP is more than 17, and when the COD/TP is less than 17, the flow of raw water to the dephosphorization zone is properly increased, and the COD amount is supplemented. The biological phosphorus removal rate of the area is 50%, and the total phosphorus of the effluent is less than 2.5mg/L.

The sludge reflux ratio of the solid-liquid separation area is generally controlled to be 40% of the water inflow, the supernatant reflux ratio is 40% -50% of the total water inflow, and the supernatant reflux ratio is improved when the total nitrogen removal rate is reduced. The suspended matters in the effluent are smaller than 80mg/L, and the discharged water enters a rear-stage advanced treatment unit. When the total phosphorus in the effluent is increased, the discharge amount of residual sludge is increased, and the sludge age of the phosphorus removal area is shortened.

In conclusion, the denitrification and dephosphorization method can respectively control the long sludge age required by denitrification and the short sludge age required by dephosphorization, is simple to operate, has biological denitrification efficiency reaching more than 90 percent, has biological dephosphorization efficiency of 50-70 percent, and is higher than 80 percent and 20 percent of that of a single activated sludge method or a single biological membrane method, thereby improving the sewage treatment efficiency.

The above embodiments are provided to illustrate the technical concept and features of the present invention and are intended to enable those skilled in the art to understand the content of the present invention and implement the same, and are not intended to limit the scope of the present invention. All equivalent changes or modifications made according to the spirit of the present invention should be included in the scope of the present invention.

Claims

1. A method for simultaneous biological nitrogen and phosphorus removal using MABR, characterized in that:

The two parts of the original wastewater are respectively introduced into the denitrification zone and the dephosphorization zone in the sewage treatment system, wherein the amount of wastewater entering the denitrification zone is greater than the amount of wastewater entering the dephosphorization zone;

The denitrification zone is provided with a plurality of MABR membrane modules, and the dissolved oxygen concentration in the denitrification zone is monitored to maintain the dissolved oxygen concentration in the denitrification zone at 0.1 mg/L to 0.3 mg/L. When the dissolved oxygen concentration does not meet the requirement, the air supply of the plurality of MABR membrane modules is adjusted, and the effluent of the denitrification zone enters the dephosphorization zone;

The dephosphorization zone is provided with an aerator and a flow pusher to monitor the dissolved oxygen concentration in the dephosphorization zone and maintain the dissolved oxygen concentration in the dephosphorization zone at 2mg/L-4mg/L. When the dissolved oxygen concentration does not meet the requirement, the oxygen supply of the aerator is adjusted;

The effluent from the dephosphorization zone enters the solid-liquid separation zone, the supernatant from the solid-liquid separation zone is refluxed to the denitrification zone, part of the sludge at the bottom of the solid-liquid separation zone is discharged from the system as residual sludge, and part of it is refluxed to the dephosphorization zone, the sludge reflux ratio is 30% to 50% of the total amount of the wastewater raw water, and the supernatant reflux ratio is 20% to 50% of the total amount of the wastewater raw water;

Monitor the total nitrogen concentration of the discharged water from the solid-liquid separation zone, and when the total nitrogen concentration in the discharged water is greater than the required discharge value, increase the proportion of the supernatant refluxed to the denitrification zone;

Monitor the total phosphorus concentration of the discharged water from the solid-liquid separation zone, and when the total phosphorus concentration in the discharged water is greater than the required discharge value, increase the sludge discharge amount;

Monitoring the sludge concentration in the phosphorus removal zone, and controlling the sludge concentration by controlling the sludge return flow;

The COD concentration in the phosphorus removal zone is monitored, and the COD/TP in the phosphorus removal zone is ensured to be greater than 17 by adjusting the amount of wastewater raw water entering the phosphorus removal zone.

2. The method for simultaneous biological denitrification and phosphorus removal using MABR according to claim 1 is characterized in that the amount of wastewater entering the denitrification zone is 80-90% of the total amount of the wastewater raw water, and the amount of wastewater entering the phosphorus removal zone is 10-20% of the total amount of the wastewater raw water.

3. The method for simultaneous biological nitrogen removal and phosphorus removal using MABR according to claim 1, characterized in that: the sewage treatment system comprises a MABR membrane tank, an aerobic tank and a solid-liquid separation tank which are interconnected;

The MABR membrane pool is the denitrification zone and is provided with a plurality of MABR membrane modules and a first dissolved oxygen monitor inside. The plurality of MABR membrane modules are connected to a gas supply pipeline, and a process gas blower, a process gas flow meter and a process gas regulating valve are sequentially provided along the air inlet direction on the gas supply pipeline;

The aerobic tank is the dephosphorization zone, the aerator and the flow pusher are arranged at the bottom of the aerobic tank, the aerator is connected to the aeration pipeline, and the aeration fan, the aeration flow meter and the aeration regulating valve are arranged in sequence along the air inlet direction of the aeration pipeline, and the dephosphorization zone is provided with a second dissolved oxygen monitor and a sludge concentration monitor;

An online total nitrogen monitor and an online total phosphorus monitor are provided in the solid-liquid separation tank. The upper part of the solid-liquid separation tank is connected to the MABR membrane tank via a supernatant reflux pipe. A supernatant reflux pump and a supernatant reflux regulating valve are sequentially provided on the supernatant reflux pipe along the water flow direction. A sludge reflux pipe is connected to the bottom of the solid-liquid separation tank. A sludge reflux pump and a reflux sludge regulating valve are sequentially provided on the sludge reflux pipe along the sludge discharge direction. The sludge reflux pipe is also connected to a sludge discharge pipe, and a sludge discharge regulating valve is provided on the sludge discharge pipe.

4. The method for simultaneous biological denitrification and phosphorus removal using MABR according to claim 3, characterized in that: the phosphorus removal zone is provided with a COD online monitor.

5. The method for simultaneous biological denitrification and phosphorus removal using MABR according to claim 3 is characterized in that: the denitrification zone and the phosphorus removal zone are connected to the water inlet pipe, and a raw water regulating valve is provided on the water inlet pipe section connected to the phosphorus removal zone.

6. The method for simultaneous biological denitrification and phosphorus removal using MABR according to claim 3, characterized in that: the MABR membrane pool and the aerobic pool are separated by a partition, and a through hole connecting the denitrification zone and the phosphorus removal zone is provided at the bottom of the partition.