CN111392966A - Electrochemical system and method for MBR membrane pollution control - Google Patents
Electrochemical system and method for MBR membrane pollution control Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F3/00—Biological treatment of water, waste water, or sewage
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- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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- C02F3/00—Biological treatment of water, waste water, or sewage
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- C02F3/12—Activated sludge processes
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- C02F3/1268—Membrane bioreactor systems
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- C02F2201/46—Apparatus for electrochemical processes
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- C02F2201/46105—Details relating to the electrolytic devices
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Abstract
The invention discloses an electrochemical system and method for MBR membrane pollution control, which comprises an anoxic reaction tank and an aerobic reaction tank which are separated by a partition plate, wherein the anoxic reaction tank is connected with a water pump through a pipeline, a stirrer is arranged in the anoxic reaction tank, the aerobic reaction tank is connected with an air blower, the aerobic reaction tank is provided with a membrane unit, the aerobic reaction tank is connected with an electrochemical reaction system through a circulating pump, the lower part of the aerobic reaction tank is provided with a sludge port, the upper part of the aerobic reaction tank is connected with a self-priming pump, and the bottom of the aerobic reaction tank is connected with the bottom of the anoxic reaction tank. The invention has the beneficial effects that: the electrochemical method is combined with the MBR process, and the electrochemical oxidation and the electric field effect are utilized to accelerate the degradation of organic matters, promote the metabolism of microbial cells and inhibit the membrane pollution problem to a certain extent; the electrochemical method is clean, efficient, stable in process, green and economical; the electrochemical process does not need civil engineering, can be directly embedded into a module, and is an effective and convenient membrane pollution control method.
Description
Technical Field
The invention belongs to the technical field of MBR membrane pollution control, and particularly relates to an electrochemical system for MBR membrane pollution control and a method thereof.
Background
A Membrane Bioreactor (MBR) is a new sewage treatment process that has been rapidly developed in recent years, and the treatment objects include domestic sewage, refractory organic sewage, industrial sewage, and the like. The process combines the membrane separation unit with the traditional biological treatment unit, so that the membrane separation and the biodegradation are organically combined, thereby realizing high-efficiency solid-liquid separation and sludge concentration, and being one of the technologies with the most development potential in the field of water treatment. However, the defects of high operation cost, poor stability and the like limit the further popularization and application of the MBR process, and the main reason is the membrane pollution problem in the MBR process. In the operation process of the MBR process, particles, colloids and soluble substances generated by microorganisms in sewage mixed liquor have physical, chemical or mechanical action with a membrane to cause adsorption and deposition in the membrane surface or membrane pores, so that the membrane pore size is reduced or blocked, the permeation flow and the separation characteristic of the membrane are irreversibly changed, and membrane pollution is caused.
The membrane pollution can affect the operation stability of the MBR process, the service life of the membrane is reduced, the operation energy consumption and the operation difficulty are increased, and the effluent can not reach the standard in serious cases. Current membrane fouling control technologies are mainly chemical, biological and physical methods. The chemical method for controlling membrane pollution mainly comprises the steps of adding a chemical agent into an MBR (membrane bioreactor) to improve the sludge property in the operation process, or soaking a polluted membrane module in an oxidant (such as hydrogen peroxide) or an acid-base solution (such as sodium hypochlorite, citric acid and hydrogen peroxide) for cleaning. The chemical method has good cleaning effect on membrane pollution, but the added medicament can increase the operation cost and cause secondary pollution, and meanwhile, frequent chemical cleaning can also influence the service life of the membrane; the biological method is characterized in that organic matters in predatory microorganisms or protozoa ingestion water are added into an MBR (membrane bioreactor) to control membrane pollution, but the growth and distribution of the microorganisms in the reactor are difficult to control, and soluble organic matters are secreted in the microbial metabolism process to accelerate the generation of membrane pollution; the physical method reduces the accumulation of pollutants in membrane pores and membrane surfaces through the action of external force and relieves membrane pollution. Generally, backwashing (water or gas), ultrasonic cleaning, and the like are used. The physical method is generally simple to operate and has no secondary pollution, but the cleaning effect is inferior to that of chemical cleaning, and the engineering application effect is poor. Therefore, a green and efficient membrane pollution control technology is urgently needed to be sought.
Research shows that the electrochemical method has potential advantages in delaying MBR process membrane biological pollution and can effectively control membrane pollution. The main reason is that on one hand, various substances with strong oxidizing property are generated in the electrochemical process to oxidize and degrade organic matters, so that the deposition of the organic matters on the membrane surface or pore canal is reduced; on the other hand, the electric field generated by the electrochemical method influences the activity of microorganisms, promotes the metabolism of microbial cells, accelerates the degradation of organic matters in water, and reduces membrane pollution. The electrochemical method has the advantages of good cleaning effect, stable process, no need of additional medicament, no secondary pollution, mild reaction condition and the like, and is a clean and efficient membrane pollution control method.
Disclosure of Invention
The invention aims to provide an electrochemical system for MBR membrane pollution control, which solves the problem of serious membrane pollution in an MBR process membrane separation unit in the prior art.
The invention adopts the technical scheme that an electrochemical system for MBR membrane pollution control comprises an anoxic reaction tank and an aerobic reaction tank, wherein the anoxic reaction tank and the aerobic reaction tank are separated by a partition plate, the anoxic reaction tank is connected with a water pump through a pipeline, a stirrer is arranged in the anoxic reaction tank, the aerobic reaction tank is connected with an air blower, the aerobic reaction tank is provided with a membrane unit, the aerobic reaction tank is connected with the electrochemical reaction system through a circulating pump, the lower part of the aerobic reaction tank is provided with a sludge port, the upper part of the aerobic reaction tank is connected with a self-priming pump, the bottom of the aerobic reaction tank is connected with a suction inlet of a peristaltic pump through a pipeline, and a discharge port of the peristaltic pump is connected with the; the electrochemical reaction system comprises an electrochemical reaction tank, wherein a cathode and an anode are arranged in the electrochemical reaction tank, and the cathode and the anode are respectively connected with two poles of a power supply.
The invention is also characterized in that:
the anode in the electrochemical reaction system adopts a DSA electrode, and the cathode is stainless steel or iron plate.
The power supply mode is low-voltage direct current or pulse electricity.
It is another object of the present invention to provide an electrochemical process for MBR membrane fouling control.
The invention adopts the technical scheme that sewage in a raw water area is pumped to an anoxic reaction tank through a water pump, the sewage flows to an aerobic reaction tank through an overflow port after reacting in the anoxic reaction tank, a membrane separation unit is arranged in the aerobic reaction tank, after separation, one part of the sewage directly flows back to the anoxic reaction tank through a peristaltic pump, one part of the sewage enters an electrochemical reaction system through a circulating pump for electrochemical treatment and then flows back to the anoxic reaction tank, and the third part of the sewage is directly pumped to a water outlet area through a self-priming pump.
The invention is also characterized in that:
sludge concentration X in electrochemical reaction tankTSS8 g/L-15 g/L.
The electrochemical treatment temperature is 5-50 ℃, and the current density range is 5mA/cm2～100mA/cm2The retention time is 30 min-180 min.
The distance between the anode and the cathode plate is 1.0 cm-4.5 cm.
The invention has the beneficial effects that: the electrochemical method is combined with the MBR process, and the electrochemical oxidation and the electric field effect are utilized to accelerate the degradation of organic matters, promote the metabolism of microbial cells and inhibit the membrane pollution to a certain extent. The electrochemical method disclosed by the invention is clean, efficient, stable in process, green and economical, does not need civil engineering, can be directly embedded into a module, and is an effective and convenient membrane pollution control method.
Drawings
FIG. 1 is a system diagram of an electrochemical system and method for MBR membrane fouling control, in accordance with the present invention;
FIG. 2 is a diagram of an electrochemical system and method for MBR membrane fouling control, according to the present invention;
FIG. 3 is a comparative illustration of an electrochemical system and method for MBR membrane fouling control of the present invention;
FIG. 4 is a SEM image of example 1 of an electrochemical system and method for MBR membrane fouling control according to the present invention;
FIG. 5 is a SEM image of example 2 of an electrochemical system and method for MBR membrane fouling control in accordance with the present invention;
FIG. 6 is a graph comparing the membrane cleaning times in different systems under the same water quality conditions for an electrochemical system and method for MBR membrane pollution control in accordance with the present invention.
In the figure, 1 is a water pump, 2 is a stirrer, 3 is a peristaltic pump, 4 is an electrochemical reaction system, 5 is a blower, 6 is a self-sucking pump, and 7 is a circulating pump.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
The invention relates to an electrochemical system for MBR membrane pollution control, which comprises an anoxic reaction tank and an aerobic reaction tank, wherein the anoxic reaction tank and the aerobic reaction tank are separated by a partition plate, the anoxic reaction tank is connected with a water pump 1 through a pipeline, a stirrer 2 is arranged in the anoxic reaction tank, sewage in the anoxic reaction tank overflows into the aerobic reaction tank through the partition plate, the aerobic reaction tank is connected with an air blower 5, the aerobic reaction tank is provided with a membrane unit, the aerobic reaction tank is connected with an electrochemical reaction system 4 through a circulating pump 7, the lower part of the aerobic reaction tank is provided with a sludge opening, the upper part of the aerobic reaction tank is connected with a self-priming pump 6, the bottom of the aerobic reaction tank is connected with a suction inlet of a peristaltic pump 3 through a pipeline, and a discharge outlet of the peristaltic pump.
As shown in fig. 2, the electrochemical reaction system 4 includes an electrochemical reaction cell, a cathode and an anode are disposed in the electrochemical reaction cell, and the cathode and the anode are respectively connected to two poles of a power supply; the anode material adopts DSA electrode (dimensionally stable anode), and the cathode is stainless steel or iron plate.
An electrochemical method for MBR membrane pollution control comprises the following process flows: sewage in a raw water area is pumped to an anoxic reaction tank through a water pump 1, anoxic conditions are guaranteed through a stirrer 2 in the anoxic reaction tank, the anoxic reaction tank and an aerobic reaction tank are separated through a partition plate, the sewage flows to the aerobic reaction tank through an overflow port after reacting in the anoxic reaction tank for a period of time, a membrane separation unit is arranged in the aerobic reaction tank, aeration is performed through an air blower 5 to maintain the aerobic conditions, after the aerobic reaction tank is treated, one part of the sewage directly flows back to the anoxic reaction tank through a peristaltic pump 3, one part of the sewage enters an electrochemical reaction system 4 through a circulating pump 7, is subjected to electrochemical treatment and then flows back to the anoxic reaction tank, and the third part of the sewage is directly pumped to a water outlet area through a self-sucking pump 6.
Sludge concentration X in electrochemical reaction tankTSS8g (TSS)/L-15 g (TSS)/L, the treatment temperature is 5-50 ℃, the temperature difference is greatly fluctuated along with the change of seasons, the temperature is low in winter and high in summer, meanwhile, the electrochemical reaction can release a part of heat, the temperature is also increased in the reaction process, and the current density range is 5mA/cm2～100mA/cm2The distance between the anode and the cathode is 1.0-4.5 cm, the retention time is 30-180 min, and the power supply is low-voltage direct current or pulse electricity.
In the electrochemical reaction system 4, the anode, i.e., the DSA electrode, degrades organic substances by generating a large amount of substances with strong oxidizing property in the electrochemical reaction, and simultaneously, the action of the electric field can stimulate microbial cells, promote the metabolism of the microbial cells, and enhance the adsorption and degradation of the organic substances.
The MBR membrane pollution is controlled by adopting an electrochemical method, so that the membrane flux can be improved by 20-60%, the TMP rising rate is reduced by 20-60%, the membrane pollution rate is obviously reduced, the cleaning frequency is reduced, the operation stability of the MBR process is improved to a certain extent, and the operation cost is reduced.
Example 1
By using Ti/PbO2The modified electrode is an anode and an iron plateIs used as a cathode, the distance between an anode and a cathode plate in the electrochemical reaction system is 4.5cm, and the current density is 30mA/cm2The retention time of the reflux in the electrochemical reaction system is 30min, and the sludge concentration of the reflux is 14.86 g/L.
Compared with a single MBR process, the TMP rising rate of the electrochemical-MBR process is reduced by 23.8%, the membrane flux is improved by 27.7%, FIG. 3 is an SEM picture of an MBR membrane without an electrochemical system, FIG. 4 is an SEM picture of the embodiment, and compared with FIG. 3, it can be seen from FIG. 4 that the deposition of particles on the surface of the EMBR membrane is less, and the membrane pollution degree is less.
Example 2
By using Ti/RuO2The electrode is an anode, the stainless steel is a cathode, the distance between the anode and the cathode plate in the electrochemical reaction system is 3.5cm, and the current density is 100mA/cm2The retention time of the reflux in the electrochemical reaction system is 60min, and the sludge concentration of the reflux is 12.53 g/L.
Compared with the MBR process only, the TMP rising rate of the electrochemical-MBR process is reduced by 48.1%, the membrane flux is improved by 54.5%, FIG. 5 is an SEM picture of the embodiment, and compared with FIG. 3, the content of pollutants in the filter layer on the membrane surface is less as seen from FIG. 5, and the pollutant layer on the membrane surface is easier to remove due to the action of the electric field.
Example 3
And (3) comparing the traditional MBR with the electrochemical-MBR under the same water quality condition. In the electrochemical-MBR coupling process, Ti/SnO is adopted2The electrode is an anode, the stainless steel is a cathode, the distance between the anode and the cathode in the electrochemical reaction system is 1cm, and the current density is 5mA/cm2The retention time of the reflux in the electrochemical reaction system is 180min, and the sludge concentration of the reflux is 10.17 g/L.
Compared with a single MBR process, the TMP rising rate of the electrochemical-MBR process is reduced by 56.2%, the membrane flux is improved by 60.5%, the service life of the membrane is prolonged, and the cleaning interval is reduced, as shown in FIG. 6, a comparison graph of the membrane cleaning times of different systems under the same water quality condition is shown, wherein in the electrochemical-MBR (EMBR) process, Ti/SnO2The electrode is an anode and the stainless steel is a cathode.
Example 4
And (3) comparing the traditional MBR with the electrochemical-MBR under the same water quality condition. In the electrochemical-MBR coupling process, Ti/MnO is adopted2The electrode is an anode, the stainless steel is a cathode, the distance between the anode and the cathode plate in the electrochemical reaction system is 3.5cm, and the current density is 20mA/cm2The retention time of the reflux in the electrochemical reaction system is 120min, and the sludge concentration of the reflux is 8.38 g/L.
Compared with a single MBR process, the TMP rising rate of the electrochemical-MBR process is reduced by 50.8%, the membrane flux is improved by 56.5%, the service life of the membrane is prolonged, and the cleaning interval is reduced
Example 5
And (3) comparing the traditional MBR with the electrochemical-MBR under the same water quality condition. In the electrochemical-MBR coupling process, Ti/IrO is adopted2The electrode is an anode, the stainless steel is a cathode, the distance between the anode and the cathode in the electrochemical reaction system is 4cm, and the current density is 60mA/cm2The retention time of the reflux in the electrochemical reaction system is 60min, and the sludge concentration of the reflux is 7.97 g/L.
Compared with a single MBR process, the TMP rising rate of the electrochemical-MBR process is reduced by 40.1%, the membrane flux is improved by 44.7%, the service life of the membrane is prolonged, and the cleaning interval is reduced.
Claims (7)
1. The electrochemical system for MBR membrane pollution control is characterized by comprising an anoxic reaction tank and an aerobic reaction tank, wherein the anoxic reaction tank and the aerobic reaction tank are separated by a partition plate, the anoxic reaction tank is connected with a water pump (1) through a pipeline, a stirrer (2) is arranged in the anoxic reaction tank, the aerobic reaction tank is connected with an air blower (5), the aerobic reaction tank is provided with a membrane unit, the aerobic reaction tank is connected with an electrochemical reaction system (4) through a circulating pump (7), the lower part of the aerobic reaction tank is provided with a sludge port, the upper part of the aerobic reaction tank is connected with a self-sucking pump (6), the bottom of the aerobic reaction tank is connected with a suction inlet of a peristaltic pump (3) through a pipeline, and a discharge port of the peristaltic pump (3) is connected;
the electrochemical reaction system (4) comprises an electrochemical reaction tank, wherein a cathode and an anode are arranged in the electrochemical reaction tank, and the cathode and the anode are respectively connected with two poles of a power supply.
2. The electrochemical system for MBR membrane pollution control according to claim 1, wherein the anode in the electrochemical reaction system (4) is DSA electrode, and the cathode is stainless steel or iron plate.
3. The electrochemical system for MBR membrane pollution control of claim 1, wherein the power supply mode is low voltage direct current or pulsed electricity.
4. An electrochemical method for MBR membrane pollution control according to claim 1, wherein the sewage in the raw water zone is pumped to an anoxic reaction tank by a water pump (1), the sewage flows to an aerobic reaction tank through an overflow port after the anoxic reaction tank reacts, a membrane separation unit is arranged in the aerobic reaction tank, after the separation is completed, a part of the sewage directly flows back to the anoxic reaction tank by a peristaltic pump (3), a part of the sewage enters an electrochemical reaction system (4) through a circulating pump (7) and flows back to the anoxic reaction tank after being subjected to electrochemical treatment, and a third part of the sewage is directly pumped to a water outlet zone by a self-priming pump (6).
5. The electrochemical method for MBR membrane pollution control according to claim 4, wherein the sludge concentration X in the electrochemical reaction tank isTSS8 g/L-15 g/L.
6. The electrochemical process for MBR membrane fouling control of claim 3, wherein the electrochemical treatment temperature is 5-50 ℃ and the current density is in the range of 5mA/cm2～100mA/cm2The retention time is 30 min-180 min.
7. The electrochemical process for MBR membrane fouling control of claim 3, wherein the spacing between the anode and cathode plates is 1.0 cm-4.5 cm.
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Cited By (2)
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| CN112142168A (en) * | 2020-09-18 | 2020-12-29 | 中国南方电网有限责任公司超高压输电公司天生桥局 | Anode material for improving membrane pollution of converter valve external cold water system and electrochemical method |
| CN114159974A (en) * | 2021-11-25 | 2022-03-11 | 西安理工大学 | High-voltage electrostatic field control MBR membrane pollution pretreatment device |
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| CN112142168B (en) * | 2020-09-18 | 2022-06-03 | 中国南方电网有限责任公司超高压输电公司天生桥局 | Anode material for improving membrane pollution of converter valve external cold water system and electrochemical method |
| CN114159974A (en) * | 2021-11-25 | 2022-03-11 | 西安理工大学 | High-voltage electrostatic field control MBR membrane pollution pretreatment device |
| CN114159974B (en) * | 2021-11-25 | 2024-04-30 | 西安理工大学 | High-voltage electrostatic field control MBR membrane pollution pretreatment device |
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