CN113003864B - Improved sewage treatment device and method by nitrogen and phosphorus removal biomembrane method - Google Patents

Improved sewage treatment device and method by nitrogen and phosphorus removal biomembrane method Download PDF

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CN113003864B
CN113003864B CN202110219260.8A CN202110219260A CN113003864B CN 113003864 B CN113003864 B CN 113003864B CN 202110219260 A CN202110219260 A CN 202110219260A CN 113003864 B CN113003864 B CN 113003864B
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tank
biological reaction
micro
phosphorus
membrane
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CN113003864A (en
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朱晓楠
单昕
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Beijing Bailing Tiandi Environmental Protection Technology Co.,Ltd.
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Beijing Shouhe Environmental Protection Technology Co ltd
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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
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • 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
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes

Abstract

The invention relates to an improved nitrogen and phosphorus removal biomembrane process sewage treatment device and a method thereof, which comprises a pretreatment system, a biological reaction tank, an MBR membrane tank, a micro-aeration biological reaction tank, a clean water tank, a phosphorus-rich water tank, a phosphorus removal coagulating sedimentation high-density tank, a sludge treatment system and two sets of pipeline systems; in the first set of pipelines, the micro-aeration biological reaction tank is respectively connected with the biological reaction tank, the phosphorus-rich water tank and the MBR membrane tank, the MBR membrane tank is connected with the clean water tank, and the phosphorus removal coagulation sedimentation high-density tank is respectively connected with the MBR membrane tank, the phosphorus-rich water tank and the sludge treatment system; in the second set of pipeline, the micro-aeration biological reaction tank is connected with a clean water tank, the MBR membrane tank is respectively connected with the biological reaction tank, the micro-aeration biological reaction tank and the phosphorus-rich water tank, and the phosphorus removal coagulating sedimentation high-density tank is respectively connected with the phosphorus-rich water tank, the sludge treatment system and the micro-aeration biological reaction tank. The method can solve the problems that the granulation period of the granular sludge is long and the granular sludge is influenced by the flocculation capacity of a biological system.

Description

Improved sewage treatment device and method by nitrogen and phosphorus removal biomembrane method
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an improved sewage treatment device and method by a nitrogen and phosphorus removal biomembrane method.
Background
In the sewage treatment process, nitrogen and phosphorus removal is a problem to be considered by most of wastewater biochemical treatment technologies. The main domestic and foreign biochemical treatment technology for nitrogen and phosphorus removal is the activated sludge process. The biochemical sewage denitrifying process is to create aerobic nitrification and anoxic denitrification environment in time and space to convert nitrogen in water into nitrogen; the biochemical sewage dephosphorization process is characterized in that activated sludge is alternately operated in an anaerobic state and an aerobic state, phosphorus-accumulating bacteria in the sludge release phosphorus in the anaerobic state, the phosphorus is excessively taken in the aerobic state, and the discharge and removal of phosphorus in water are realized by discharging phosphorus-rich excess sludge.
With the improvement of water treatment standards and the promotion of energy conservation and emission reduction work in the water treatment industry, the prior art needs to be continuously improved to match with the actual high-requirement treatment requirements. The aerobic granular sludge process breaks through the characteristics of space-time partition of the traditional activated sludge, forms a biopolymer by the self-condensation of microorganisms in a special environment, realizes the coexistence of different functional bacteria (nitrobacteria, denitrifying bacteria, anaerobic ammonium oxidation bacteria and the like) due to the existence of aerobic, anaerobic and anoxic stepped partition of Dissolved Oxygen (DO) mass transfer resistance in granules, obviously enriches the denitrification approaches in the traditional single-stage system by the coupling of the functional bacteria, has the characteristics of high biological density, good sedimentation performance, high toxicity resistance, unique space layered structure and the like, and can simultaneously realize organic matter degradation and synchronous denitrification and dephosphorization. Meanwhile, the occupied area is saved, the investment cost is reduced, and the operation cost can also be reduced.
But the application has some defects which limit the wide application. The following were used:
1. sequencing batch process, large floor area
At present, most of the researches and applications of the aerobic granular sludge method are carried out in a sequencing batch reactor, intermittent water outlet or alternate water outlet is realized, so that the problem of interval time buffering needs to be considered when other continuous treatment processes are connected in series front and back, or a spare tank body is designed, occupies a large area, and is not suitable for a large-scale sewage treatment plant.
2. The granular sludge is disintegrated to influence the yielding water
When the granular sludge structure is unstable, the granules can be disintegrated and washed, and the particle size of the granules is rapidly reduced in a short time, so that the concentration of suspended solids in the effluent of the reactor is high, and the treatment performance is deteriorated. COD, BOD, TN, TP and the like carried in the effluent suspended substances can cause the effluent quality to exceed the standard.
3. Slow granulation of sludge, complex granulation process and need of human intervention with rich experience
The existing aerobic granular sludge formation can be divided into a self-flocculation hypothesis and a crystal nucleus hypothesis, which respectively represent that the physical flocculation is used for strengthening the microorganism proliferation self-flocculation and the artificial crystal nucleus is used for adding the artificial crystal nucleus to enable the microorganism to be attached and grow, the granular sludge culture period is longer, and a small amount of practical engineering reports show that the reactor has a long start-up period (5 months) and flocculent sludge with a certain proportion all the time.
4. Coping with the fluctuation difference of water quality and low risk of wind
The granular sludge method depends on the sludge property, and if the water quality and the water quantity of inlet water fluctuate greatly, the proportion of dominant bacteria is unbalanced, and the sludge disintegration risk is brought.
Therefore, the development of a complete and efficient denitrification and dephosphorization process route with guaranteed effluent quality is crucial to solving the contradiction between the current biological treatment capacity and the gradually improved effluent quality requirement, integrating the biochemical advantages of aerobic granular sludge, solving the problems of sludge aggregation and stable structure, improving the treatment effect of the wastewater biological treatment technology and popularizing and applying. The invention is provided based on the research background to meet the sewage treatment requirement.
Disclosure of Invention
Aiming at the defects in the denitrification and dephosphorization process in the prior art, the invention aims to: the improved sewage treatment device and method based on the nitrogen and phosphorus removal biomembrane method have the advantages of being reasonable in structural design, stable and reliable in operation, capable of solving the problems that the granular sludge granulation period is long and is affected by the flocculation capacity of a biological system, and capable of ensuring stable water quality of effluent and the like.
In order to achieve the purpose, the invention adopts the following technical scheme:
an improved sewage treatment device adopting a nitrogen and phosphorus removal biomembrane process comprises a pretreatment system, a biological reaction tank, an MBR membrane tank, a micro-aeration biological reaction tank, a clean water tank, a phosphorus-rich water tank, a phosphorus removal coagulating sedimentation high-density tank, a sludge treatment system and two sets of pipeline systems; wherein the pretreatment system is connected with the biological reaction tank; the two sets of pipeline systems comprise a first set of pipelines, a second set of pipelines and a pipeline switching component for alternately switching the first set of pipelines and the second set of pipelines; in the first set of pipelines, the micro-aeration biological reaction tank is respectively connected with a biological reaction tank, a phosphorus-rich water tank and an MBR membrane tank, the MBR membrane tank is connected with a clean water tank, and the phosphorus-removing coagulating sedimentation high-density tank is respectively connected with the MBR membrane tank, the phosphorus-rich water tank and a sludge treatment system; in the second set of pipeline, the micro-aeration biological reaction tank is connected with a clean water tank, the MBR membrane tank is respectively connected with the biological reaction tank, the micro-aeration biological reaction tank and a phosphorus-rich water tank, and the phosphorus removal coagulating sedimentation high-density tank is respectively connected with the phosphorus-rich water tank, a sludge treatment system and the micro-aeration biological reaction tank.
As a further optimization of the scheme, a coarse grating, a fine grating, an aeration grit chamber and a membrane grating are sequentially arranged in the pretreatment system from left to right, wherein the gap of the coarse grating is 10-20mm, the gap of the fine grating is 2-10mm, and the gap of the membrane grating is 0.5-2 mm. The pretreatment system is a treatment process before sewage to be treated enters the biochemical system during pretreatment. Aims to remove floating objects, oil and large-particle suspended matters which are harmful to a biological system and a membrane system. If the sewage is municipal sewage, the pretreatment comprises a coarse grating, a fine grating, an aeration grit chamber and a membrane grating; if the sewage is industrial sewage, the pretreatment is selected according to the characteristics of water quality and pollutants, so as to achieve the purpose of removing floaters, oil and large-particle suspended matters which are harmful to a biological system and a membrane system.
As a further optimization of the scheme, the biological reaction tank comprises a tank body, an aeration device, a flow impeller and a stirrer, wherein the aeration device, the flow impeller and the stirrer are arranged in the tank body; the biological reaction tank can be arranged into an anaerobic-anoxic-aerobic combined tank, an oxidation ditch, an aerobic tank and the like according to the water quality condition.
As a further optimization of the scheme, the micro-aeration biological reaction tank comprises a tank body, a membrane-loaded bioreactor arranged in the tank body, a vacuum ejector and a suction pump; the vacuum ejector is arranged at the highest point of the front pipeline of the suction pump; the suction pump and the vacuum ejector are matched with each other; the micro-aeration biological reaction tank utilizes the negative pressure of the hollow fiber membrane to suck the activated sludge and quickly and uniformly attaches the activated sludge to the surface of the membrane wire; the membrane-loaded bioreactor comprises a membrane frame, a membrane component arranged on the membrane frame, a micro aeration device and a large bubble aeration device, wherein the micro aeration device and the large bubble aeration device are arranged at the bottom of the membrane frame; the micro-aeration device air inlet pipeline is welded on the membrane frame and communicated with the micro-aeration device air inlet, and the membrane component comprises membrane filaments.
As a further optimization of the scheme, the structure of the micro-aeration biological reaction tank is the same as that of the MBR membrane tank; the pipeline switching component comprises a pneumatic valve, an MBR membrane pool, a micro-aeration biological reaction pool, a phosphorus-rich water pool, a pneumatic valve, a phosphorus-removing coagulating sedimentation high-density pool, a pneumatic valve and a pipeline switching component, wherein the pneumatic valve is arranged on the pipeline from the biological reaction pool to the MBR membrane pool and the micro-aeration biological reaction pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the clean water pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the phosphorus-rich water pool, and the pneumatic valve is arranged on the pipeline from the phosphorus-removing coagulating sedimentation high-density pool to the MBR membrane pool and the micro-aeration biological reaction pool; the phosphorus-rich water tank is connected with the phosphorus removal coagulating sedimentation high-density tank through a pipeline at the bottom of the tank wall, and is used for collecting phosphorus-rich water and balancing water quality and water quantity; the high-density dephosphorization coagulating sedimentation tank is mainly used for removing phosphate through coagulating sedimentation and comprises a coagulating stirring area, a flocculation stirring area and an inclined tube sedimentation area which are sequentially connected.
As a further optimization of the scheme, the device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, and a concentration sensor assembly, a pressure sensor assembly, a flow sensor assembly, a liquid level sensor assembly, a display assembly, an abnormality alarm assembly, an in-situ control station and a central monitoring station which are respectively connected with the programmable PLC controller; the concentration sensor assembly includes: the oxidation-reduction potential sensor, the dissolved oxygen concentration sensor and the sludge concentration sensor are distributed in the biological reaction tank; the system comprises an oxidation-reduction potential sensor, a dissolved oxygen concentration sensor and a sludge concentration sensor which are arranged in an MBR membrane tank and a micro-aeration biological reaction tank, as well as a total nitrogen concentration sensor, a total phosphorus concentration sensor, a COD concentration sensor, an ammonia nitrogen concentration sensor, an SS concentration sensor and a temperature/pH sensor, wherein the total nitrogen concentration sensor, the total phosphorus concentration sensor, the COD concentration sensor, the ammonia nitrogen concentration sensor, the SS concentration sensor and the temperature/pH sensor are arranged in a pretreatment water inlet and a clean water tank and are used for detecting total nitrogen concentration; the pressure sensor assembly includes: the system comprises a vacuum pressure sensor, a pressure sensor of an aeration pipeline, a pressure sensor of a compressed air pipeline and a pressure sensor, wherein the vacuum pressure sensor is arranged on a pipeline in front of a water producing pump in an MBR membrane tank and a micro-aeration biological reaction tank system; the flow sensor assembly includes: the system comprises a flow sensor behind a water production pump, a flow sensor behind a phosphorus-rich water pump and a sludge flow sensor of a residual sludge discharge pipeline which are arranged in an MBR membrane tank and a micro-aeration biological reaction tank system, and a flow sensor arranged in a reflux and sludge discharge pipeline of a phosphorus removal coagulation sedimentation high-density tank; the level sensor assembly includes: the liquid level sensors are arranged in front of and behind the pretreatment grating and in the biological reaction tank; liquid level sensors arranged in the MBR membrane tank and the micro-aeration biological reaction tank; a vacuum liquid level sensor of a front pipeline of a water producing pump and a vacuum liquid level sensor of a front pipeline of a phosphorus-rich water pump which are arranged in the MBR membrane tank and the micro-aeration biological reaction tank system; liquid level sensors distributed in the phosphorus-rich water tank and the clean water tank; the liquid level sensor and the mud level sensor are arranged in the dephosphorization coagulation sedimentation high-density tank; the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the concentration sensor assembly, the pressure sensor assembly, the flow sensor assembly and the liquid level sensor assembly to the field control station and the industrial personal computer; the display component comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button and a protection and safety interlocking device of the equipment, and the emergency stop button, the protection and safety interlocking device are all connected to the electric control loop by adopting hard wires; the field control station comprises an operation terminal control cabinet, and is used for manually controlling the equipment or adjusting the equipment to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen connected with the industrial personal computer.
The operation level of the equipment is divided into three levels, namely local operation, field control station operation and central monitoring station operation, and the priority level is decreased in turn. The on-site operation is the control of the equipment through an on-site button of the equipment; the operation of the field control station is that an operator controls the equipment manually through a terminal control cabinet or the adjustment is automatically controlled by a PLC program. The central monitoring station operation refers to the operation of field equipment through a mouse or a keyboard matched with the industrial personal computer.
The controlled equipment is provided with an automatic/manual/stop mode selection switch, and when the switch is in an automatic position, the equipment is controlled by the output of the PLC (namely, the operation mode of the field control station). When the switch is in the 'manual' position, the equipment is controlled by an on-site button (namely, an on-site operation mode), and an emergency stop button, a protection and safety interlocking device of the equipment are connected to an electric control loop by hard wires and are not limited by a mode selection switch. When the switch is in the "off" position, the device is off-line and cannot be controlled at all.
The field control station has a manual/automatic mode selection function, and in the manual mode, the equipment is manually controlled by function keys on an operator terminal or on a touch screen, and in the automatic mode, the equipment is controlled by a PLC according to a pre-programmed program.
All control is realized by feedback of the control command, when the control command is inconsistent with the feedback information, an alarm is given, and a fault processing program is executed.
The treatment method of the improved nitrogen and phosphorus removal biomembrane process sewage treatment device comprises the following steps:
1) first stage
Preprocessing: pretreating the sewage to be treated in a pretreatment system;
processing in a biological reaction tank: feeding the sewage pretreated in the first step into a biological reaction tank;
processing in a micro-aeration biological reaction tank: the water treated in the biological reaction tank in the step two enters a micro-aeration biological reaction tank for treatment;
and fourthly, MBR membrane pool treatment: water treated in the micro-aeration biological reaction tank in the step three enters an MBR membrane tank for treatment;
treating the phosphorus-rich water pool: discharging membrane permeate of the micro-aeration biological reaction tank in the step (III) to a phosphorus-rich water tank for treatment, and collecting effluent of the phosphorus-rich water tank into an MBR membrane tank after dephosphorization in a dephosphorization coagulating sedimentation high-density tank; under the negative pressure suction effect of a water production pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank through a pipeline, and sludge enters a sludge treatment system for treatment and is discharged;
2) second stage
Closing a water inlet valve from a biological reaction tank to a micro-aeration biological reaction tank, opening a water pipeline valve from the biological reaction tank to an MBR membrane tank, and converting the MBR membrane tank into the micro-aeration biological reaction tank;
discharging membrane permeate of the micro-aeration biological reaction tank to a phosphorus-rich water tank, and enabling effluent of the phosphorus-rich water tank to be subjected to phosphorus removal by a phosphorus removal coagulating sedimentation high-density tank and then to flow into the original micro-aeration biological reaction tank;
thirdly, the effluent of the micro-aeration biological reaction tank enters an original micro-aeration biological reaction tank, and the original micro-aeration biological reaction tank is adjusted into an MBR membrane tank through backwashing and aeration; under the negative pressure suction action of a water production pump suction pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank, and sludge enters a sludge treatment system for treatment and is discharged;
3) the third stage
The first stage and the second stage are alternately operated to complete the nitrogen and phosphorus removal of all the sewage to be treated.
As a further optimization of the above scheme, the alternating interval between the first stage and the second stage is 10-15 days in summer and 15-20 days in winter.
The improved sewage treatment device and method by the nitrogen and phosphorus removal biomembrane method have the following beneficial effects:
1) by utilizing the negative-pressure suction effect of the membrane, sludge enrichment power is artificially provided, the formation of a biological reaction subarea is accelerated, and the problems that the granulation period of granular sludge is long and the granular sludge is limited by the flocculation capacity of a biological system are solved; provides sludge disintegration resistance and solves the problem of granular sludge disintegration.
2) The double-membrane system conversion utilizes the membrane load bioreactor to remove COD and denitrogenate, realizes sludge desorption through backwashing and large bubble stirring, converts the membrane load bioreactor into an MBR membrane reactor, and utilizes membrane filtration to guarantee that the quality of the effluent water is stable.
3) The anaerobic zone of the membrane-supported bioreactor is attached to the surface of the membrane, phosphate generated by anaerobic phosphorus release is collected in a centralized manner, the limitation of biological phosphorus removal capability is broken through by combining a chemical phosphorus removal method, the different index requirements of the total phosphorus in the effluent are realized by adjusting the dosage of a phosphorus removal medicament, and the total phosphorus content in the effluent is controllable.
4) The process route has the advantages of nitrogen and phosphorus removal, complete and continuous flow and solves the problem of sequencing batch intermittent reaction of an aerobic granular sludge method.
Drawings
FIG. 1 is a process flow diagram of the improved nitrogen and phosphorus removal biomembrane process for sewage treatment of the invention.
FIG. 2 is a process flow diagram of the first stage of the present invention.
FIG. 3 is a process flow diagram of the second stage of the present invention.
FIG. 4 is a schematic view of the operation principle of the membrane-supported bioreactor of the present invention.
FIG. 5 is a schematic diagram of the operating principle of the MBR membrane group device of the present invention.
FIG. 6 is a schematic structural diagram of the membrane-supported bioreactor (or MBR membrane module) of the present invention, and only one of the membrane-supported bioreactor is shown because the structure of the membrane-supported bioreactor is the same as that of the MBR membrane module.
FIG. 7 is a structural schematic diagram of sewage treatment by an improved denitrification and dephosphorization biofilm process.
Detailed Description
The following describes the improved denitrification and dephosphorization biofilm process sewage treatment device and method of the invention in detail with reference to the attached drawings 1-7.
An improved sewage treatment device adopting a nitrogen and phosphorus removal biomembrane process comprises a pretreatment system, a biological reaction tank, an MBR membrane tank, a micro-aeration biological reaction tank, a clean water tank, a phosphorus-rich water tank, a phosphorus removal coagulating sedimentation high-density tank, a sludge treatment system and two sets of pipeline systems; wherein the pretreatment system is connected with the biological reaction tank; the two sets of pipeline systems comprise a first set of pipelines, a second set of pipelines and a pipeline switching component for alternately switching the first set of pipelines and the second set of pipelines; in the first set of pipelines, the micro-aeration biological reaction tank is respectively connected with a biological reaction tank, a phosphorus-rich water tank and an MBR membrane tank, the MBR membrane tank is connected with a clean water tank, and the phosphorus-removing coagulating sedimentation high-density tank is respectively connected with the MBR membrane tank, the phosphorus-rich water tank and a sludge treatment system; in the second set of pipeline, the micro-aeration biological reaction tank is connected with a clean water tank, the MBR membrane tank is respectively connected with the biological reaction tank, the micro-aeration biological reaction tank and a phosphorus-rich water tank, and the phosphorus removal coagulating sedimentation high-density tank is respectively connected with the phosphorus-rich water tank, a sludge treatment system and the micro-aeration biological reaction tank.
The pretreatment system is a treatment process before sewage to be treated enters the biochemical system during pretreatment. Aims to remove floating objects, oil and large-particle suspended matters which are harmful to a biological system and a membrane system. If the sewage is municipal sewage, the pretreatment comprises a coarse grating, a fine grating, an aeration grit chamber and a membrane grating; if the sewage is industrial sewage, the pretreatment is selected according to the characteristics of water quality and pollutants, so as to achieve the purpose of removing floaters, oil and large-particle suspended matters which are harmful to a biological system and a membrane system.
The pretreatment system is internally provided with a coarse grating, a fine grating, an aeration grit chamber and a membrane grating from left to right in sequence, wherein the gap of the coarse grating is 10-20mm, the gap of the fine grating is 2-10mm, and the gap of the membrane grating is 0.5-2 mm. The biological reaction tank comprises a tank body, an aeration device, a flow impeller and a stirrer, wherein the aeration device, the flow impeller and the stirrer are arranged in the tank body, and the biological reaction tank can be an anaerobic-anoxic-aerobic combined tank, an oxidation ditch, an aerobic tank and the like according to the water quality condition. The micro-aeration biological reaction tank comprises a tank body, a membrane-loaded bioreactor arranged in the tank body, a vacuum ejector and a suction pump; the vacuum ejector is arranged at the highest point of the front pipeline of the suction pump; the suction pump and the vacuum ejector are matched with each other; the micro-aeration biological reaction tank utilizes the negative pressure of the hollow fiber membrane to suck the activated sludge and quickly and uniformly attaches the activated sludge to the surface of the membrane wire; the membrane-loaded bioreactor comprises a membrane frame, a membrane assembly arranged on the membrane frame, a micro aeration device and a large bubble aeration device, wherein the micro aeration device and the large bubble aeration device are arranged at the bottom of the membrane frame, the large bubble aeration device is arranged at the bottom of the membrane frame, the lower part of the membrane frame where the micro aeration device is arranged at the upper part of the large bubble aeration device, a water production port of the membrane assembly is connected with the membrane frame in a socket joint mode and is arranged at the upper part of the micro aeration device, a water production pipeline is welded on the membrane frame and is communicated with a water production port of the membrane assembly, an air inlet pipeline of the large bubble aeration device is welded on the membrane frame and is communicated with an air inlet of the large bubble aeration device, an air inlet pipeline of the micro aeration device is welded on the membrane frame and is communicated with the air inlet of the micro aeration device, and the membrane assembly contains membrane filaments.
The structure of the micro-aeration biological reaction tank is the same as that of the MBR membrane tank; the pipeline switching component comprises a pneumatic valve, an MBR membrane pool, a micro-aeration biological reaction pool, a phosphorus-rich water pool, a pneumatic valve, a phosphorus-removing coagulating sedimentation high-density pool, a pneumatic valve and a pipeline switching component, wherein the pneumatic valve is arranged on the pipeline from the biological reaction pool to the MBR membrane pool and the micro-aeration biological reaction pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the clean water pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the phosphorus-rich water pool, and the pneumatic valve is arranged on the pipeline from the phosphorus-removing coagulating sedimentation high-density pool to the MBR membrane pool and the micro-aeration biological reaction pool; the phosphorus-rich water tank and the phosphorus removal coagulation sedimentation high-density tank are connected through a pipeline at the bottom of the tank wall, see the attached figure 7 in detail, and the main function of the phosphorus-rich water tank is to collect phosphorus-rich water and balance water quality and water quantity; the dephosphorization coagulation sedimentation high-density tank is mainly used for removing phosphate through coagulation sedimentation, and structurally comprises a coagulation stirring area, a flocculation stirring area and an inclined tube sedimentation area.
The device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, a concentration sensor assembly, a pressure sensor assembly, a flow sensor assembly, a liquid level sensor, a display assembly, an abnormal alarm assembly, an in-situ control station and a central monitoring station, which are respectively connected with the programmable PLC controller; the concentration sensor assembly includes: the oxidation-reduction potential sensor, the dissolved oxygen concentration sensor and the sludge concentration sensor are distributed in the biological reaction tank; the oxidation-reduction potential sensor, the dissolved oxygen concentration sensor and the sludge concentration sensor are arranged in the MBR membrane tank and the micro-aeration biological reaction tank; the sensor is arranged at the pretreatment water inlet and the clean water tank and used for detecting the total nitrogen concentration, the sensor is used for detecting the total phosphorus concentration, the sensor is used for detecting the COD concentration, the sensor is used for detecting the ammonia nitrogen concentration, the sensor is used for detecting the SS concentration and the sensor is used for detecting the temperature/pH; the pressure sensor assembly includes: the vacuum pressure sensor is arranged on a pipeline in front of a water producing pump in the MBR membrane tank and the micro-aeration biological reaction tank system, the vacuum pressure sensor is arranged on a pipeline in front of a phosphorus-rich water pump, the pressure sensor is arranged on an aeration pipeline, and the pressure sensor is arranged on a compressed air pipeline; the pressure sensor is arranged on an aeration pipeline of the biological reaction tank; the flow sensor assembly includes: a post-water pump flow sensor, a phosphorus-rich water pump flow sensor and a sludge flow sensor of a residual sludge discharge pipeline which are arranged in the MBR membrane tank and the micro-aeration biological reaction tank system; the flow sensor is arranged on a reflux and sludge discharge pipeline of the dephosphorization coagulation sedimentation high-density tank; the level sensor assembly includes: the liquid level sensors are arranged in front of and behind the pretreatment grating and in the biological reaction tank; liquid level sensors arranged in the MBR membrane tank and the micro-aeration biological reaction tank; a vacuum liquid level sensor of a front pipeline of a water producing pump and a vacuum liquid level sensor of a front pipeline of a phosphorus-rich water pump which are arranged in the MBR membrane tank and the micro-aeration biological reaction tank system; liquid level sensors distributed in the phosphorus-rich water tank and the clean water tank; the liquid level sensor and the mud level sensor are arranged in the dephosphorization coagulation sedimentation high-density tank; the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the concentration sensor assembly, the pressure sensor assembly, the flow sensor assembly and the liquid level sensor assembly to the field control station and the industrial personal computer; the display component comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button, a protection and safety interlocking device of the equipment; the emergency stop button, the protection and safety interlocking device are all connected to an electrical control loop by hard wires; the field control station comprises an operation terminal control cabinet, and is used for manually controlling the equipment or adjusting the equipment to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen. As for the types of the single sensors in the concentration sensor assembly, the pressure sensor assembly, the flow sensor assembly and the liquid level sensor assembly, the selection thereof is common in the prior art, and the details are not repeated herein.
The operation level of the equipment is divided into three levels, namely local operation, field control station operation and central monitoring station operation, and the priority level is decreased in turn. The on-site operation is the control of the equipment through an on-site button of the equipment; the operation of the field control station is that an operator controls the equipment manually through a terminal control cabinet or the adjustment is automatically controlled by a PLC program. The central monitoring station operation refers to the operation of field equipment through a mouse or a keyboard matched with the industrial personal computer.
The controlled equipment is provided with an automatic/manual/stop mode selection switch, and when the switch is in an automatic position, the equipment is controlled by the output of the PLC (namely, the operation mode of the field control station). When the switch is in the 'manual' position, the equipment is controlled by an on-site button (namely, an on-site operation mode), and an emergency stop button, a protection and safety interlocking device of the equipment are connected to an electric control loop by hard wires and are not limited by a mode selection switch. When the switch is in the "off" position, the device is off-line and cannot be controlled at all.
The field control station has a manual/automatic mode selection function, and in the manual mode, the equipment is manually controlled by function keys on an operator terminal or on a touch screen, and in the automatic mode, the equipment is controlled by a PLC according to a pre-programmed program.
All control is realized by feedback of the control command, when the control command is inconsistent with the feedback information, an alarm is given, and a fault processing program is executed.
The pretreatment system is a treatment process before sewage to be treated enters the biochemical system during pretreatment. Aims to remove floating objects, oil and large-particle suspended matters which are harmful to a biological system and a membrane system. If the sewage is municipal sewage, the pretreatment comprises a coarse grating, a fine grating, an aeration grit chamber and a membrane grating; if the sewage is industrial sewage, the pretreatment is selected according to the characteristics of water quality and pollutants, so as to achieve the purpose of removing floaters, oil and large-particle suspended matters which are harmful to a biological system and a membrane system.
The biological reaction tank can be arranged into an anaerobic-anoxic-aerobic combined tank, an oxidation ditch, an aerobic tank and the like according to the water quality condition. The microorganism is mainly used for metabolizing pollutants such as COD, BOD, ammonia nitrogen and the like. Which comprises a tank body, an aeration pipe, a flow impeller and a stirrer which are arranged in the tank body.
The micro-aeration biological reaction tank utilizes the negative pressure suction effect of the hollow fiber membrane to ensure that the activated sludge is quickly and uniformly attached to the surface of the membrane wire to form the membrane-loaded bioreactor. Due to the negative pressure suction effect, the biological activated sludge forms a sludge enrichment layer on the surface of the membrane wire, a sludge dense area is formed near the membrane wire area due to the concentration gradient principle, a sludge loose area is formed at the periphery of the membrane wire area, and a sludge expansion area is formed at the outermost layer due to the diffusion of floras such as filamentous fungi in the sludge. Because dissolved oxygen mass transfer resistance forms aerobic, anaerobic and anoxic stepped partitions in each area of the sludge, coexistence of different functional bacteria (nitrobacteria, denitrifying bacteria, anaerobic ammonium oxidation bacteria and the like) can be realized, and the denitrification function can be efficiently completed. The negative pressure effect is provided and maintained by a vacuum ejector at the water producing side of the membrane, and the effluent enters a phosphorus-rich water pool in a self-flowing or pumping mode. The negative pressure suction process is mainly realized by a vacuum ejector and a suction pump. The vacuum ejector is arranged at the highest point of a pipeline in front of the suction pump, compressed air generates vacuum in the vacuum ejector through the action of jet flow in the vacuum ejector, and air in a sucked space is sucked and taken away through the pipeline. Under the condition of good sealing, the vacuum value can reach-70 kpa at most. The auxiliary suction pump is started for the first time, and the suction pump can continuously and stably produce water after the pipeline is full of water. When the water production is influenced by the pipeline gas accumulation due to the problems of sealing leakage, dissolved gas dissolution and the like, the vacuum ejector controls the valve of the compressed air pipeline to open and work, and the valve is closed after the pipeline is full of water.
The denitrification principle of the membrane-supported bioreactor is similar to that of a well-maintained granular sludge method, but the phosphorus release and absorption reactions of the well-maintained granular sludge method are in the same granules, the total phosphorus can only be internally circulated, and the phosphorus removal is realized by discharging residual sludge. In the membrane-supported bioreactor, the anaerobic zone is arranged in the center of the membrane-supported bioreactor, namely on the surface of the membrane filaments. Through the negative pressure suction effect, phosphate released by anaerobic reaction can enter the inside of the membrane filaments through the membrane, and then is conveyed to the phosphorus-rich water pool through the pump, so that the total phosphorus is discharged.
The micro-aeration biological reaction tank achieves the purposes of removing COD, nitrogen and phosphorus by forming an aerobic, anaerobic and anoxic integration, can realize the symbiotic ecological environment of autotrophic and heterotrophic microorganisms, improves the proportion of short-range nitrification and denitrification and anaerobic ammoxidation, and has small loss because the aeration quantity is comprehensively determined according to organic load and ammonia nitrogen load. Meanwhile, in order to ensure the stability of a sludge layer and reduce water flow scouring turbulence, microbubble aeration is adopted in the micro-aeration biological reaction tank, and the microbubble aeration is favorable for oxygen transfer due to large specific surface area, so that the aeration quantity is further reduced, and the operating cost is saved.
The method utilizes the membrane negative pressure suction effect to artificially provide sludge enrichment power, quickens the formation of biological reaction subareas, and solves the problems that the granulation period of the granular sludge is long and is limited by the flocculation capacity of a biological system; provides the flocculent resistance of sludge disintegration and solves the problem of granular sludge disintegration.
The MBR membrane tank provides driving force by using a water production suction pump or liquid level difference, and realizes solid-liquid separation by using 0.01-0.1 micron micropores uniformly distributed on the membrane surface for physical interception, wherein suspended matters larger than membrane pores are intercepted by 100%, and the stability of the effluent quality is ensured. The MBR system adopts high-efficiency large-bubble aeration to accelerate the turbulent flow of sludge on the surface of the membrane, prevent the sludge from being enriched on the surface of the membrane and maintain high-flux operation.
Because the sludge is combined and enriched in the micro-aeration biological reaction tank, the sewage and sludge entering the MBR system have low dispersion density, and the MBR system can maintain high flux (average flux is 30-40L/m)2H) operation, more typical MBR system (average flux 10-20L/m)2H), the membrane consumption is reduced 1/2, the floor area and the investment cost are reduced 1/2, and the operation cost is reduced 1/3-1/2 compared with the typical MBR system.
The structure of the micro-aeration biological reaction tank is the same as that of an MBR membrane tank, and the micro-aeration biological reaction tank is arranged into a plurality of series of small tanks, a single tank body is provided with 1-10 membrane group devices, and the number of the series is more than or equal to 3. When a single series is alternated or overhauled, the water inlet load is uniformly distributed to other series and is in a bearable load range, and continuous and stable water inlet and outlet are realized.
The treatment method of the improved nitrogen and phosphorus removal biomembrane process sewage treatment device comprises the following steps:
1) first stage
Preprocessing: pretreating the sewage to be treated in a pretreatment system;
processing in a biological reaction tank: feeding the sewage pretreated in the first step into a biological reaction tank;
processing in a micro-aeration biological reaction tank: the water treated in the biological reaction tank in the step two enters a micro-aeration biological reaction tank for treatment;
and fourthly, MBR membrane pool treatment: water treated in the micro-aeration biological reaction tank in the step three enters an MBR membrane tank for treatment;
treating the phosphorus-rich water pool: discharging membrane permeate of the micro-aeration biological reaction tank in the step (III) to a phosphorus-rich water tank for treatment, and collecting effluent of the phosphorus-rich water tank into an MBR membrane tank after dephosphorization in a dephosphorization coagulating sedimentation high-density tank; under the negative pressure suction effect of a water production pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank through a pipeline, and sludge enters a sludge treatment system for treatment and is discharged;
2) second stage
Closing a water inlet valve from a biological reaction tank to a micro-aeration biological reaction tank, opening a water pipeline valve from the biological reaction tank to an MBR membrane tank, and converting the MBR membrane tank into the micro-aeration biological reaction tank;
discharging membrane permeate of the micro-aeration biological reaction tank to a phosphorus-rich water tank, and enabling effluent of the phosphorus-rich water tank to be subjected to phosphorus removal by a phosphorus removal coagulating sedimentation high-density tank and then to flow into the original micro-aeration biological reaction tank;
thirdly, the effluent of the micro-aeration biological reaction tank enters an original micro-aeration biological reaction tank, and the original micro-aeration biological reaction tank is adjusted into an MBR membrane tank through backwashing and aeration; under the negative pressure suction action of a water production pump suction pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank, and sludge enters a sludge treatment system for treatment and is discharged;
3) the third stage
The first stage and the second stage are alternately operated to complete the nitrogen and phosphorus removal of all the sewage to be treated.
In the alternative process, the change period is related to the sludge age, when the sludge is aged and needs to be discharged and updated, the series of micro-aeration biological reaction tanks and the MBR membrane tank are closed, the MBR membrane group device in the MBR membrane tank stops large-bubble aeration, the vacuum ejector is started to form negative pressure, so that the activated sludge is quickly and uniformly attached to the surface of the membrane wires to form a sludge layer, the micro-aeration device is started, dissolved oxygen is provided by the micro-aeration, and a slight turbulent flow is gradually formed into a sludge dense area, a sludge loose area and an expansion area to form a membrane-loaded biological reactor. Opening a large bubble aeration device of an MBR membrane group device in the micro-aeration biological reaction tank, scrubbing the surface of membrane filaments by strong turbulent flow and shearing force, simultaneously opening a backwashing pump, injecting clear water from the interior of the membrane filaments into the clear water tank, and allowing backwashing water to pass through the membrane filaments from inside to outside to realize the desorption of a sludge layer; and opening an emptying valve of the micro-aeration biological reaction tank to thoroughly empty the sludge mixed liquid in the tank, and discharging the sludge mixed liquid to the biological reaction tank and the sludge treatment system. Adjusting a valve, wherein effluent of the pretreatment system enters an original MBR membrane tank, effluent of the original MBR membrane tank enters an original micro-aeration biological reaction tank, effluent of a membrane of the original micro-aeration biological reaction tank enters a clean water tank, namely, the original MBR membrane tank is adjusted into the micro-aeration biological reaction tank, and the original micro-aeration biological reaction tank is adjusted into the MBR membrane tank. All the series are alternately carried out, and in the single-series alternating process, the water inlet load is uniformly distributed to other series, so that continuous and stable water inlet and outlet are realized. The whole water inlet and water production of the system are not affected. The alternating interval between the first stage and the second stage is 10-15 days in summer and 15-20 days in winter.
The treatment method of the present invention is further described in detail below with reference to a specific example of application.
Taking the sewage of a certain municipal sewage treatment plant as an example, the water volume scale is 15000m3And d. The quality of the inlet water is as follows:
Figure BDA0002953882270000131
the effluent standard requires execution of the B standard in the Beijing landmark DB 11/890-. The main indexes are as follows:
Figure BDA0002953882270000132
according to the route of the treatment method, the specific treatment process is as follows:
sewage enters the coarse grating, and the specific technological parameters of the coarse grating are as follows: the thick grating channels are 2 rows, the channel width is 1m, the channel depth is 5.5m, the water depth before grating is 1m, and the grating flow speed is 0.6 m/s.
The effluent of the coarse grid enters a lifting pump room, and the lifting pump room increases the potential energy of the sewage to a height which can flow through each treatment process by means of gravity. The parameters of the specific lift pump house are as follows: pump house size: and L multiplied by B multiplied by H is 13.0m multiplied by 8.4m multiplied by 5.7m, a submersible sewage pump is arranged as a lifting pump, 3 submersible sewage pumps are selected, 2 submersible sewage pumps work, and 1 submersible sewage pump is used for standby.
The lift pump pumps water into the fine grid, the specific technological parameters of the fine grid are as follows: the fine grid ditch 2 row, the liquid level 900mm in front of the grid, the channel width 1500mm, the ditch depth 1500mm, the grid gap 5mm, the flow rate of passing the grid is 0.5m/s, the fine grid matches shaftless screw conveyor, screw press and grid slag car, these parts all belong to common part, the concrete connection and layout mode all belong to prior art, will not be repeated here.
And (3) enabling the effluent of the fine grid to enter an aeration grit chamber, and removing inorganic grit with the specific gravity of more than 2.65 and the particle size of more than 0.2mm in the sewage so as to ensure the normal operation of a subsequent treatment system.
The water discharged from the fine grid enters a membrane grid, and the membrane grid is a fine grid with a grid gap of 1mm and is used for further effectively removing solid substances, hairs and fiber substances with a size larger than 1mm in the water, so that the operation reliability of a subsequent device (a membrane filtration system) is improved. The membrane grid sets up 2 galleries, establishes 1 platform of meticulous grid in every gallery, respectively sets up a channel gate around every meticulous grid, and the supporting shaftless screw conveyer of meticulous grid, screw press and grid slag car, these parts all belong to common part, and concrete connection and the mode of laying all belong to prior art, just do not give unnecessary details here.
The effluent of the membrane grid enters a biological reaction tank, the effluent of the biological reaction tank enters a micro-aeration biological reaction tank, and the total retention time of the biological reaction tank is 9 hours, including an anaerobic tank (the retention time is 1.5 hours), an anoxic tank (the retention time is 2.5 hours), and an aerobic tank (the retention time is 2.5 hours)Time 5h), sludge concentration of 5000-. The membrane-loaded bioreactor in the micro-aeration biological reaction tank integrates anaerobic phosphorus release reaction, aerobic nitrification reaction, anoxic denitrification reaction, short-range nitrification denitrification reaction and anaerobic ammonia oxidation reaction, and compared with the traditional AAO system, the total tank volume is reduced by 1250m3The land occupation is saved by 192m according to the calculation of the pool depth of 7m and the effective water depth of 6.5m2And the civil engineering cost is saved by 100 ten thousand.
The micro-aeration biological reaction tank utilizes the negative pressure suction of the hollow fiber membrane to ensure that the activated sludge is quickly and uniformly attached to the surface of the membrane wire to form the membrane-loaded bioreactor. Due to the negative pressure suction effect, the biological activated sludge forms a sludge enrichment layer on the surface of the membrane wire, a sludge dense area is formed near the membrane wire area due to the concentration gradient principle, a sludge loose area is formed at the periphery of the membrane wire area, and a sludge expansion area is formed at the outermost layer due to the diffusion of floras such as filamentous fungi in the sludge. Because dissolved oxygen mass transfer resistance forms aerobic, anaerobic and anoxic stepped partitions in each area of the sludge, coexistence of different functional bacteria (nitrobacteria, denitrifying bacteria, anaerobic ammonium oxidation bacteria and the like) can be realized, and the denitrification function can be efficiently completed.
Phosphate released by anaerobic reaction can enter the inside of the membrane filaments through the membrane under the action of negative pressure suction in the membrane-supported bioreactor, and then is conveyed to a phosphorus-rich water pool through a pump, so that the discharge of total phosphorus is realized. Compared with the traditional AAO process, the total phosphorus can be reduced to 0.4mg/L by biological phosphorus removal, and the total phosphorus can hardly reach 0.3mg/L required by the effluent index, so that the traditional AAO process needs to be provided with a chemical phosphorus removal measure, and a chemical phosphorus removal agent is directly added into an aeration tank. If an MBR process is adopted, a phosphorus removal agent directly enters a membrane tank, so that the agent blocks MBR membrane pores and is difficult to clean and restore to an initial value. If the traditional secondary sedimentation tank process is adopted, the dephosphorization agent can also form an accumulative effect in the biological tank body, and the long-term accumulative effect influences the balance of a biological system.
The micro-aeration biological reaction tank achieves the purposes of removing COD, nitrogen and phosphorus by forming an aerobic, anaerobic and anoxic integration, can realize the symbiotic ecological environment of autotrophic and heterotrophic microorganisms, improves the proportion of short-range nitrification and denitrification and anaerobic ammoxidation, and has small loss because the aeration quantity is comprehensively determined according to organic load and ammonia nitrogen load.
Meanwhile, in order to ensure the stability of a sludge layer and reduce the water flow scouring turbulence, microbubble aeration is adopted in the micro-aeration biological reaction tank, the microbubble aeration is favorable for oxygen transfer due to large specific surface area, the aeration amount is further reduced, the dissolved oxygen in the tank is controlled to be 0.2-1mg/L, and compared with the traditional aerobic tank which is 2-2.5mg/L, the power consumption required by aeration is reduced by 30-50%.
The negative pressure effect is provided and maintained by a vacuum ejector on the water producing side of the membrane, the outlet water enters a phosphorus-rich water pool in a pumping mode, and the flow rate of the vacuum ejector is as follows: 7NL/s, maximum vacuum: -70KPa, design of phosphorus-rich permeate flow rate of 1.5-15L/m2H. By utilizing the negative-pressure suction effect of the membrane, sludge enrichment power is artificially provided, the formation of a biological reaction subarea is accelerated, and the problems that the granulation period of granular sludge is long and the granular sludge is limited by the flocculation capacity of a biological system are solved; provides the flocculent resistance of sludge disintegration and solves the problem of granular sludge disintegration.
And the effluent of the micro-aeration biological reaction tank enters an MBR membrane tank. The micro-aeration biological reaction tank and the MBR membrane tank are provided with 6 series, the same type of membrane group device is adopted, 3 groups of membrane group devices are arranged on a single micro-aeration biological reaction tank (MBR membrane tank), 60 membrane components are arranged on each membrane group device, and the membrane filament surface area of each membrane component is 20m2The surface area of the membrane filaments of the single-set membrane module device is 1200m2. The conversion and the regeneration of the membrane load bioreactor are realized by adjusting a water inlet valve and a water outlet valve through the process control alternate change function. The regeneration process of the membrane-loaded bioreactor ensures the sludge age and also has the function of removing phosphorus from activated sludge.
And the sludge mixed liquor in the MBR membrane tank flows back to the biological reaction tank through a reflux pump.
The operation was as follows:
the first stage is as follows: the sewage enters a micro-aeration biological reaction tank, and the effluent of the micro-aeration biological reaction tank enters an MBR membrane tank; and the membrane permeate of the micro-aeration biological reaction tank is pumped and discharged to a phosphorus-rich water tank through a phosphorus-rich water pump, and the effluent of the phosphorus-rich water tank is subjected to phosphorus removal by a phosphorus removal coagulating sedimentation high-density tank and then flows into an MBR membrane tank. Under the negative pressure suction action of a water production pump suction pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments, mud-water separation is realized, and the clear water enters a clear water tank. And the sludge mixed liquor in the MBR membrane tank flows back to the biological reaction tank through a reflux pump.
And a second stage: and closing a water inlet valve of the micro-aeration biological reaction tank, opening a water pipeline valve from the biological reaction tank to the MBR membrane tank, and converting the MBR membrane tank into the micro-aeration biological reaction tank. And (3) discharging the membrane permeate of the micro-aeration biological reaction tank to a phosphorus-rich water tank, and leading the effluent of the phosphorus-rich water tank to be subjected to phosphorus removal by a phosphorus removal coagulating sedimentation high-density tank and then to be merged into the original micro-aeration biological reaction tank. The effluent of the micro-aeration biological reaction tank enters an original micro-aeration biological reaction tank, and the original micro-aeration biological reaction tank is adjusted into an MBR membrane tank through backwashing and aeration stirring. And under the negative pressure suction action of the water production pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments, the sludge-water separation is realized, and the clear water enters the clear water tank. And the sludge mixed liquor in the MBR membrane tank flows back to the biological reaction tank through a reflux pump.
The first stage and the second stage operate alternately, the summer alternate interval is 10-15 days, and the winter alternate interval is 15-20 days.
The total phosphorus of inlet water of the biological reaction tank is about 6mg/L, the total phosphorus of outlet water of the biological reaction tank is 0.4-0.6mg/L, membrane permeate in the micro-aeration biological reaction tank is anaerobic phosphorus release permeate, the concentration of the total phosphorus is increased to 12-14mg/L, the membrane permeate is discharged to a phosphorus-rich water tank through a phosphorus-rich water suction pump, and the outlet water of the phosphorus-rich water tank is added with a phosphorus removal coagulant and a flocculating agent, passes through a phosphorus removal coagulating sedimentation high-density tank, flocculates the total phosphorus into sludge and is discharged to a sludge treatment system. The phosphorus removal coagulant is PAC, the dosage of PAC is 50-120ppm, the flocculant is PAM, the dosage of PAM is 1-3ppm, and the total phosphorus in effluent is 0.01-0.05 ppm.
The water discharged from the high-density tank for dephosphorization and coagulation sedimentation enters the MBR membrane tank, on one hand, the sludge concentration in the membrane tank is diluted, the high-flux operation of the MBR membrane tank can be ensured, on the other hand, the sewage after dephosphorization is subjected to membrane filtration, and the water quality of the discharged water is ensured.
3 groups of MBR membrane group devices are arranged on a single MBR membrane tank, 60 membrane assemblies are arranged on each MBR membrane group device, and the area of each membrane assembly is 20m2Single set MBR membrane group device membrane area 1200m2Average membrane flux: 28.9L/m2h。The MBR design flux is improved by 30-50% compared with the traditional MBR process. The project can meet the aim of denitrification without designing carbon source addition, compared with the traditional AAO biochemical system, 40mg of sodium acetate can be saved per liter, the market price of 58-60% of sodium acetate is 3500 yuan/ton, the annual saving of the operating cost is 128 plus 132 thousands, and the project has considerable economic benefit.
The embodiments described above are intended to facilitate one of ordinary skill in the art in understanding and using the present invention. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the embodiments described herein, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.

Claims (3)

1. An improved sewage treatment device by a nitrogen and phosphorus removal biomembrane method is characterized in that: the device comprises a pretreatment system, a biological reaction tank, an MBR membrane tank, a micro-aeration biological reaction tank, a clean water tank, a phosphorus-rich water tank, a phosphorus-removing coagulating sedimentation high-density tank, a sludge treatment system and two sets of pipeline systems; wherein the pretreatment system is connected with the biological reaction tank; the two sets of pipeline systems comprise a first set of pipelines, a second set of pipelines and a pipeline switching component for alternately switching the first set of pipelines and the second set of pipelines; in the first set of pipelines, the micro-aeration biological reaction tank is respectively connected with a biological reaction tank, a phosphorus-rich water tank and an MBR membrane tank, the MBR membrane tank is connected with a clean water tank, and the phosphorus-removing coagulating sedimentation high-density tank is respectively connected with the MBR membrane tank, the phosphorus-rich water tank and a sludge treatment system; in the second set of pipelines, the micro-aeration biological reaction tank is connected with a clean water tank, the MBR membrane tank is respectively connected with the biological reaction tank, the micro-aeration biological reaction tank and a phosphorus-rich water tank, and the phosphorus removal coagulating sedimentation high-density tank is respectively connected with the phosphorus-rich water tank, a sludge treatment system and the micro-aeration biological reaction tank;
the micro-aeration biological reaction tank comprises a tank body, a membrane-loaded bioreactor arranged in the tank body, a vacuum ejector and a suction pump; the vacuum ejector is arranged at the highest point of the front pipeline of the suction pump; the suction pump and the vacuum ejector are matched with each other; the micro-aeration biological reaction tank utilizes the negative pressure of the hollow fiber membrane to suck the activated sludge and quickly and uniformly attaches the activated sludge to the surface of the membrane wire; the membrane-loaded bioreactor comprises a membrane frame, a membrane component arranged on the membrane frame, a micro aeration device and a large bubble aeration device, wherein the micro aeration device and the large bubble aeration device are arranged at the bottom of the membrane frame; the micro-aeration device air inlet pipeline is welded on the membrane frame and is communicated with the micro-aeration device air inlet, and the membrane component comprises membrane filaments;
the structure of the micro-aeration biological reaction tank is the same as that of the MBR membrane tank; the pipeline switching component comprises a pneumatic valve, an MBR membrane pool, a micro-aeration biological reaction pool, a phosphorus-rich water pool, a pneumatic valve, a phosphorus-removing coagulating sedimentation high-density pool, a pneumatic valve and a pipeline switching component, wherein the pneumatic valve is arranged on the pipeline from the biological reaction pool to the MBR membrane pool and the micro-aeration biological reaction pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the clean water pool, the pneumatic valve is arranged on the pipeline from the MBR membrane pool and the micro-aeration biological reaction pool to the phosphorus-rich water pool, and the pneumatic valve is arranged on the pipeline from the phosphorus-removing coagulating sedimentation high-density pool to the MBR membrane pool and the micro-aeration biological reaction pool; the phosphorus-rich water tank is connected with the phosphorus removal coagulating sedimentation high-density tank through a pipeline at the bottom of the tank wall, and is used for collecting phosphorus-rich water and balancing water quality and water quantity; the high-density dephosphorization coagulating sedimentation tank is mainly used for removing phosphate through coagulating sedimentation and comprises a coagulating stirring area, a flocculation stirring area and an inclined tube sedimentation area which are sequentially connected;
the device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, a concentration sensor assembly, a pressure sensor assembly, a flow sensor assembly, a liquid level sensor assembly, a display assembly, an abnormality alarm assembly, an in-situ control station and a central monitoring station which are respectively connected with the programmable PLC controller; the concentration sensor assembly includes: the oxidation-reduction potential sensor, the dissolved oxygen concentration sensor and the sludge concentration sensor are distributed in the biological reaction tank; the system comprises an oxidation-reduction potential sensor, a dissolved oxygen concentration sensor and a sludge concentration sensor which are arranged in an MBR membrane tank and a micro-aeration biological reaction tank, as well as a sensor which is arranged in a pretreatment water inlet and a clean water tank and is used for detecting the total nitrogen concentration, a total phosphorus concentration sensor for detecting the total phosphorus concentration, a COD concentration sensor for detecting the COD concentration, an ammonia nitrogen concentration sensor for detecting the ammonia nitrogen concentration, an SS concentration sensor for detecting the SS concentration and a temperature/pH sensor for detecting the temperature/pH; the pressure sensor assembly includes: the system comprises a vacuum pressure sensor, a pressure sensor of an aeration pipeline, a pressure sensor of a compressed air pipeline and a pressure sensor, wherein the vacuum pressure sensor is arranged on a pipeline in front of a water producing pump in an MBR membrane tank and a micro-aeration biological reaction tank system; the flow sensor assembly includes: the system comprises a flow sensor behind a water production pump, a flow sensor behind a phosphorus-rich water pump and a sludge flow sensor of a residual sludge discharge pipeline which are arranged in an MBR membrane tank and a micro-aeration biological reaction tank system, and a flow sensor arranged in a reflux and sludge discharge pipeline of a phosphorus removal coagulation sedimentation high-density tank; the level sensor assembly includes: the liquid level sensors are arranged in front of and behind the pretreatment grating and in the biological reaction tank; liquid level sensors arranged in the MBR membrane tank and the micro-aeration biological reaction tank; a vacuum liquid level sensor of a front pipeline of a water producing pump and a vacuum liquid level sensor of a front pipeline of a phosphorus-rich water pump which are arranged in the MBR membrane tank and the micro-aeration biological reaction tank system; the liquid level meters are distributed in the phosphorus-rich water tank and the clean water tank; the liquid level sensor and the mud level sensor are arranged in the dephosphorization coagulation sedimentation high-density tank; the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the concentration sensor assembly, the pressure sensor assembly, the flow sensor assembly and the liquid level sensor assembly to the field control station and the industrial personal computer; the display component comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button and a protection and safety interlocking device of the equipment, and the emergency stop button, the protection and safety interlocking device are all connected to the electric control loop by adopting hard wires; the field control station comprises an operation terminal control cabinet, and is used for manually controlling the equipment or adjusting the equipment to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen connected with the industrial personal computer;
the treatment method of the improved nitrogen and phosphorus removal biomembrane process sewage treatment device comprises the following steps:
1) first stage
Preprocessing: pretreating the sewage to be treated in a pretreatment system;
processing in a biological reaction tank: feeding the sewage pretreated in the first step into a biological reaction tank;
processing in a micro-aeration biological reaction tank: the water treated in the biological reaction tank in the step two enters a micro-aeration biological reaction tank for treatment;
and fourthly, MBR membrane pool treatment: water treated in the micro-aeration biological reaction tank in the step three enters an MBR membrane tank for treatment;
treating the phosphorus-rich water pool: discharging membrane permeate of the micro-aeration biological reaction tank in the step (III) to a phosphorus-rich water tank for treatment, and collecting effluent of the phosphorus-rich water tank into an MBR membrane tank after dephosphorization in a dephosphorization coagulating sedimentation high-density tank; under the negative pressure suction effect of a water production pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank through a pipeline, and sludge enters a sludge treatment system for treatment and is discharged;
2) second stage
Closing a water inlet valve from a biological reaction tank to a micro-aeration biological reaction tank, opening a water pipeline valve from the biological reaction tank to an MBR membrane tank, and converting the MBR membrane tank into the micro-aeration biological reaction tank;
discharging membrane permeate of the micro-aeration biological reaction tank to a phosphorus-rich water tank, and enabling effluent of the phosphorus-rich water tank to be subjected to phosphorus removal by a phosphorus removal coagulating sedimentation high-density tank and then to flow into the original micro-aeration biological reaction tank;
thirdly, the effluent of the micro-aeration biological reaction tank enters an original micro-aeration biological reaction tank, and the original micro-aeration biological reaction tank is adjusted into an MBR membrane tank through backwashing and aeration; under the negative pressure suction action of a water production pump suction pump, clear water enters the inside of the membrane filaments, suspended matter flocs are retained outside the membrane filaments to realize mud-water separation, the clear water enters a clear water tank, and sludge enters a sludge treatment system for treatment and is discharged;
3) the third stage
The first stage and the second stage are alternately operated to complete the nitrogen and phosphorus removal of all the sewage to be treated.
2. The sewage treatment device by the improved nitrogen and phosphorus removal biomembrane method according to claim 1, characterized in that: the pretreatment system is internally provided with a coarse grating, a fine grating, an aeration grit chamber and a membrane grating from left to right in sequence, wherein the gap of the coarse grating is 10-20mm, the gap of the fine grating is 2-10mm, and the gap of the membrane grating is 0.5-2 mm.
3. The sewage treatment device by the improved nitrogen and phosphorus removal biomembrane method according to claim 1, characterized in that: the alternating interval between the first stage and the second stage is 10-15 days in summer and 15-20 days in winter.
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