CN113354068A - Conductive medium assisted double-biological-chamber electrochemical membrane bioreactor and application method thereof - Google Patents
Conductive medium assisted double-biological-chamber electrochemical membrane bioreactor and application method thereof Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/005—Combined electrochemical biological processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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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
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/20—Total organic carbon [TOC]
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
Abstract
The invention belongs to the field of water treatment application, and particularly relates to a water treatment reactor and a method for treating sewage by using the same. The invention is characterized in that: the conductive medium is introduced into the electrochemical bioreactor, so that reactive active sites are increased, the electron transfer efficiency and the pollutant degradation efficiency are accelerated, the DIET is enhanced, the reaction time can be greatly shortened, and the volume and the occupied area of the reactor are reduced in practical application; and a double-biological-chamber reaction system is creatively constructed, the volume utilization rate is improved on the basis of fully exerting the advantages of electrochemistry and biological methods, and a new idea is provided for the treatment of organic wastewater which is difficult to degrade or toxic.
Description
Technical Field
The invention belongs to the field of water treatment application, and particularly relates to a water treatment reactor and a method for treating sewage by using the same.
Background
Electrochemical bioreactors, which are commonly used to treat refractory organic wastewater, enhance the breaking of chemical bonds and mineralization of organic matter by the addition of an electric field. The electrochemical bioreactor forms a conductive path by adding electrolyte, and realizes electron transfer and organic matter degradation. Therefore, if a certain conductive medium can be added into the reactor, the electron transfer rate can be effectively improved, and the reaction process is accelerated. Meanwhile, the introduction of the conductive medium provides more reactive sites for the reactor, and the conductive medium is equivalent to countless micro batteries, has the effect of enhancing the degradation of organic matters, and can also enhance the direct inter-inoculation electron transfer (DIET) of microorganisms.
At present, a common electrochemical bioreactor generally uses an ion exchange membrane to divide the reactor into a cathode chamber and an anode chamber, the two chambers respectively play a role, pollutant degradation can be effectively realized, but the problem that pH is not easy to control exists in the double-chamber reactor. The existing double-chamber electrochemical bioreactor usually only uses one reaction chamber (cathode chamber or anode chamber) as a microorganism reaction chamber, only controls the pH value of one reaction chamber under the condition, is relatively easy to operate, and has the problem of low volume utilization rate of the reactor. At the same time, the method is only suitable for substances such as phenol (only oxidation can be mineralized into CO completely)2And H2O), nitrate nitrogen (convertible to N by reduction only)2) And the like. If the pollutant itself needs two ways of oxidation and reduction to be degraded, byproducts are generated, which causes secondary pollution. In the case of aniline, the effluent contains nitrate nitrogen as a by-product when only the oxidation route is used, and the effluent contains nitrate nitrogen when only the reduction route is usedComplete mineralization of the organic matter cannot be achieved.
The invention aims to provide a novel electrochemical membrane bioreactor, wherein a cathode chamber and an anode chamber are jointly used and are used as reaction chambers of microorganisms to form a double-biological-chamber electrochemical membrane bioreactor, and the microorganisms utilize hydrogen in the cathode chamber and oxygen in the anode chamber to realize complete degradation of pollutants through oxidation and reduction reactions so as to achieve the aim of zero-pollution discharge. Meanwhile, a conductive medium is added into the system to serve as a biological carrier, so that the electron transfer efficiency in the electrochemical process and the DIET of microorganisms are accelerated, and the efficiency of the reactor is enhanced.
Disclosure of Invention
Aiming at the defects of the existing electrochemical bioreactor and combining the background technology, the invention provides a novel reactor, which mainly comprises the following components: a conductive medium assisted double-biological-chamber electrochemical membrane bioreactor and a method for treating sewage by applying the same.
The technical scheme of the invention is as follows:
a conductive medium assisted double-biological-chamber electrochemical membrane bioreactor comprises a direct-current power supply, a power line, an electrode plate, a cathode chamber and an anode chamber, wherein the cathode chamber and the anode chamber are separated by an ion exchange membrane. The treatment process of the reactor comprises the following steps: sewage firstly enters a cathode chamber to generate a reduction reaction, then flows into an anode chamber to generate an oxidation reaction, and is discharged from the anode chamber after pollutants are completely degraded; the sewage in the anode chamber flows back to the cathode chamber at a certain reflux ratio to realize the complete degradation of pollutants; the cathode chamber and the anode chamber are both provided with hydraulic self-circulation to ensure uniform mixing.
The cathode chamber and the anode chamber are filled with a certain conductive medium, the conductive medium is preferably one or more of granular activated carbon, graphite granules, conductive metal granules, granules loaded with conductive materials on the surfaces and the like, and the filling rate is 10-70%;
the ion exchange membrane can be an anion exchange membrane, a cation exchange membrane and a proton exchange membrane, and can be properly selected according to different pollutants.
Adding electrolyte and buffer system with proper concentration according to the sewage conductivity and buffer capacity, wherein the electrolyte is preferably sodium sulfate with the concentration of 0.1-15 mM; the buffer system is preferably carbonate buffer system, and ensures that the pH value of the two chambers is controlled between 6 and 9.
The current intensity and the current density applied by the power supply are set according to the concentration of the pollutants and the size of the electrode plate, the current intensity is usually 5-50mA, and the current density is 0.5-5A/square meter.
The reflux ratio from the anode chamber to the cathode chamber is usually 100-600% according to the concentration of the pollutants and the water inlet flow rate, so as to ensure the stable pH value of the two chambers and the normal running of the biological reaction.
And adjusting the self-circulation flow of the cathode chamber and the anode chamber according to the simulation result of Fluent hydraulic simulation software, and ensuring uniform mass transfer of the system.
The invention has the advantages that: a novel electrochemical bioreactor is constructed for the first time, a cathode chamber and an anode chamber are jointly used as a microbial reaction chamber, and the electrochemical bioreactor is an innovation of only using a single biological reaction chamber in the traditional process and greatly improves the volume utilization rate; the system can degrade pollutants through double paths of oxidation and reduction, and can remove total nitrogen while mineralizing organic matters, so that the problem of secondary pollution is avoided, and the application range is wider; meanwhile, the addition of the conductive medium can accelerate the electron transfer efficiency in the reactor, accelerate the reaction process, provide more reaction active sites for the reactor, construct countless tiny batteries and strengthen the degradation of organic matters; in addition, the conductive medium can be used as a carrier of the microorganism, functional strains are reserved, the DIET process of the microorganism is enhanced, and the efficiency of the reactor is improved; if the carbon-based material is used as a conductive medium, the carbon-based material also has the function of adsorbing pollutants; in addition, the pH value of the system is controlled by utilizing the internal circulation and the ion exchange membrane together, so that the adding amount of the buffer solution can be reduced, and certain medicament adding cost is saved; meanwhile, in the invention, hydraulic simulation is used as a reference index for self-circulation regulation and control, which is beneficial to accurate control of mass transfer of a system.
The invention is characterized in that: the conductive medium is introduced into the electrochemical bioreactor, so that reactive active sites are increased, the electron transfer efficiency and the pollutant degradation efficiency are accelerated, the DIET is enhanced, the reaction time can be greatly shortened, and the volume and the occupied area of the reactor are reduced in practical application; and a double-biological-chamber reaction system is creatively constructed, the volume utilization rate is improved on the basis of fully exerting the advantages of electrochemistry and biological methods, and a new idea is provided for the treatment of organic wastewater which is difficult to degrade or toxic.
Drawings
FIG. 1 is a schematic diagram of a conductive medium assisted double-chamber electrochemical membrane bioreactor
FIG. 2 is a schematic diagram of a conventional dual-chamber (single-bio-chamber) electrochemical membrane bioreactor in comparative example 1
FIG. 3 is a schematic diagram of a twin-chambered electrochemical membrane bioreactor without the addition of a conductive medium in comparative example 2
Reference numerals
1-water inlet end; 2-self circulation of the cathode chamber; 3-a cathode chamber; 4-1# magnetic pump; 5-a metering pump; 6-anode chamber; 7-2# magnetic pump; 8-self circulation of the anode chamber; 9-a conductive medium; 10-a cathode plate; 11-ion exchange membranes; 12-an anode plate; 13-water outlet end; 14-hydrogen; 15-oxygen; 16-water inlet end; 17-3# magnetic pump; 18-a cathode chamber; 19-cathode chamber self-circulation; 20-hydrogen; 21-a cathode plate; 22-ion exchange membrane; 23-an anode plate; 24-a filler; 25-water outlet end; 26-oxygen; 27-anode chamber self-circulation; 28-4# magnetic pump; 29-anode chamber; 30-water inlet end; 31-a filler; 32-a cathode plate; 33-ion exchange membranes; 34-an anode plate; 35-water outlet end; 36-anode chamber self-circulation; 37-5# magnetic pump; 38-anode chamber; 39-a metering pump; 40-6# circulating pump; 41-cathode chamber; 42-cathode chamber self-circulation; 43-hydrogen; 44-oxygen.
Detailed Description
The invention is further illustrated by way of example in the following figures:
FIG. 1 is a schematic diagram of a conductive media assisted twin chamber electrochemical membrane bioreactor.
The reactor set-up is shown in FIG. 1, and the reactor operating scheme is described as follows:
starting a direct current power supply and setting a proper current intensity to start an electrolytic reaction, wherein a hydrogen evolution reaction occurs near the cathode plate 10 to generate hydrogen 14, and an oxygen evolution reaction occurs near the anode plate 12 to generate oxygen 15; sewage enters the cathode chamber 3 from the water inlet end 1, heterotrophic reduction reaction can occur in the cathode chamber 3, and hydrogen autotrophic reduction reaction can also occur by utilizing the generated hydrogen 14; sewage flows into the anode chamber 6 after reacting in the cathode chamber 3, and oxidation reaction is carried out by using oxygen 15 generated by the anode chamber 6; after the reaction is finished, discharging the reaction product out of the reactor through a water outlet end 13; the effluent of the anode chamber 6 partially flows back to the cathode chamber 3 through a metering pump 5, so that the complete degradation of pollutants is ensured; conductive media 9 are filled in the cathode chamber 3 and the anode chamber 6, so that the electrochemical electron transfer process is accelerated, carriers are provided for microorganisms, and the DIET process is strengthened; in addition, self-circulation is arranged, the flow of the cathode chamber self-circulation 2 is controlled by the 1# magnetic pump 4, and the flow of the anode chamber self-circulation 8 is controlled by the 2# magnetic pump 7, so that uniform mixing and reasonable flow state are ensured.
Example 1
The reactor of the invention is used for treating pyridine simulation wastewater. Pyridine is a typical pollutant of wastewater in chemical industry, pharmaceutical industry and other industries, is a heterocyclic organic matter which is difficult to biodegrade, has certain toxicity and has a molecular formula of C5H5And N is added. Establishing a reactor with a total effective volume of 1.6L, wherein the cathode chamber and the anode chamber are respectively 0.8L, and the two chambers are separated by an anion exchange membrane; 0.5L of granular zero-valent iron (the grain diameter is 3-5mm) is filled in the cathode chamber and the anode chamber respectively and is used as a conductive medium and a carrier of microorganism; the concentration of the inlet water pyridine is 50mg/L, the concentration of the electrolyte sodium sulfate is 2mM, the concentration of the carbonate buffer system is 20mM, and the pH value is about 7.5; setting the system current intensity to be 25mA and the current density to be 2.5A/square meter; according to the simulation result of Fluent hydraulic simulation software, the self-circulation of the two chambers is set to be 2.0L/min, so that the uniform mass transfer is ensured. The inflow rate is about 4.4ml/min, and the hydraulic retention time of raw water in the cathode chamber and the anode chamber is 3h respectively; the internal circulation flow rate is about 22.2ml/min, and the circulation ratio is about 5. After long-time running detection, the effluent quality is stable, and the monitoring data are shown in table 2.
Table 1 monitoring data for example 1
| Pyridine (mg/L) | TOC(mg/L) | TN(mg/L) | |
| Inflow water | 50 | 40 | 8.9 |
| Discharging water | 0 | 2.2 | 1.4 |
| Removal rate% | 100 | 94.5 | 84.3 |
Example 2
The reactor of the invention is used for treating the aniline simulation wastewater. Aniline is a typical pollutant of wastewater in pharmaceutical, printing and dyeing industries and the like, has certain toxicity and is difficult to biodegrade; it is composed of amino substituted for one hydrogen on benzene ring, and its molecular formula is C6H7And N is added. Establishing a reactor with the total effective volume of 1.6L, wherein the cathode chamber and the anode chamber are respectively 0.8L, and the two chambers are separated by a proton exchange membrane; the cathode chamber and the anode chamber are respectively filled with 0.4L of activated carbon (the particle size is about 5mm) which is used as a conductive medium and a carrier of microorganism; the concentration of the aniline in the inlet water is 100mg/L, the concentration of the electrolyte sodium sulfate is 0.5mM, the concentration of the carbonate buffer system is 10mM, and the pH value is about 7.5; the system current intensity is set to be 15mA, and the current density is set to be 1.5A per square meter; according to the simulation result of Fluent hydraulic simulation software, the self-circulation of the two chambers is set to be 1.5L/min, so as to ensure the uniform mass transfer. The water inflow rate is about 3.3ml/min, and the hydraulic retention time of raw water in the cathode chamber and the anode chamber is 4 hours respectively; the internal circulation flow rate is about 13.3ml/min, and the circulation ratio is about 4. After long-time running detection, the effluent quality is stable, and the monitoring data are shown in table 2.
Table 2 monitoring data for example 2
| Aniline (mg/L) | COD(mg/L) | TN(mg/L) | |
| Inflow water | 100 | 245 | 15 |
| Discharging water | 0 | 12.4 | 2.8 |
| Removal rate% | 100 | 94.9 | 81.3 |
Comparative example 1
The pyridine simulation wastewater is treated by adopting an electrochemical membrane bioreactor of a traditional double-chamber (single-biological-chamber) electrochemical membrane bioreactor, and the schematic diagram of the reactor is shown as the attached figure 2; the reactor is mainly different from the reactor shown in the attached figure 1 in that only a filler is added into an anode chamber to serve as a microbial reaction chamber, namely a single biological chamber; adding an alkali solution into the cathode chamber, and realizing the control of the pH value of the anode chamber through the ion exchange effect; the anode chamber and the cathode chamber are not communicated, and pollutants are degraded only in the anode chamber. The treatment process comprises the following steps: starting a direct current power supply and setting a proper current intensity to start an electrolytic reaction, wherein a hydrogen evolution reaction is carried out near a cathode plate 21 to generate hydrogen 20, and an oxygen evolution reaction is carried out near an anode plate 23 to generate oxygen 26; sewage enters the anode chamber 29 from the water inlet end 16 and is discharged out of the reactor through the water outlet end 25 after the reaction is finished; the anode chamber 29 is filled with a filler 24 to provide a carrier for microorganisms; sodium hydroxide with a certain concentration is added into the cathode chamber 18 to control the pH value of the anode chamber 29; in addition, self-circulation is arranged, the flow of the cathode chamber self-circulation 19 is controlled by a 3# magnetic pump 17, and the flow of the anode chamber self-circulation 27 is controlled by a 4# magnetic pump 28, so that uniform mixing and reasonable flow state are ensured.
Establishing a reactor with a total effective volume of 1.6L, wherein the cathode chamber and the anode chamber are respectively 0.8L, and the two chambers are separated by an anion exchange membrane; the anode chamber was filled with 0.5L of a commercially available K1 filler as a carrier for the microorganisms; the concentration of the inlet water pyridine is 50mg/L, the concentration of the electrolyte sodium sulfate is 2mM, the concentration of the carbonate buffer system is 20mM, and the pH value is about 7.5; setting the system current intensity to be 25mA and the current density to be 2.5A/square meter; according to the simulation result of Fluent hydraulic simulation software, the self-circulation of the two chambers is set to be 2.0L/min, so that the uniform mass transfer is ensured. The inflow rate is about 4.4ml/min, and the hydraulic retention time of raw water in the cathode chamber and the anode chamber is 3h respectively; the internal circulation flow rate is about 22.2ml/min, and the circulation ratio is about 5. After long-time running detection, the effluent quality is stable, and the monitoring data are shown in Table 3.
Table 3 monitoring data for comparative example 1
| Pyridine (mg/L) | TOC(mg/L) | TN(mg/L) | |
| Inflow water | 50 | 40 | 8.9 |
| Discharging water | 35.5 | 33.2 | 8.5 |
| Removal rate% | 29 | 17 | 4.5 |
Comparative example 2
Pyridine simulated wastewater is treated by using a double-biological-chamber electrochemical membrane bioreactor without adding a conductive medium, and the schematic diagram of the reactor is shown in figure 3. The treatment process comprises the following steps: starting a direct current power supply and setting a proper current intensity to start an electrolytic reaction, wherein a hydrogen evolution reaction occurs near the cathode plate 32 to generate hydrogen 43, and an oxygen evolution reaction occurs near the anode plate 34 to generate oxygen 44; the cathode chamber 41 and the anode chamber 38 are separated by an ion exchange membrane 33; sewage enters the cathode chamber 41 from the water inlet end 30, heterotrophic reduction reaction can occur in the cathode chamber 41, and hydrogen autotrophic reduction reaction can also occur by utilizing the generated hydrogen 43; the sewage flows into the anode chamber 38 after reacting in the cathode chamber 43, and oxidation reaction occurs by using oxygen 44 generated in the anode chamber 38; after the reaction is finished, discharging the reaction product out of the reactor through a water outlet end 35; part of the effluent from the anode chamber 38 flows back to the cathode chamber 41 through a metering pump 39, so as to ensure complete degradation of pollutants; the cathode chamber 41 and the anode chamber 38 are both filled with the filler 31 to provide a carrier for the microorganisms; in addition, self-circulation is arranged, the flow of the cathode chamber self-circulation 42 is controlled by a 6# magnetic pump 40, and the flow of the anode chamber self-circulation 36 is controlled by a 5# magnetic pump 37, so that uniform mixing and reasonable flow state are ensured.
Establishing a reactor with a total effective volume of 1.6L, wherein the cathode chamber and the anode chamber are respectively 0.8L, and the two chambers are separated by an anion exchange membrane; 0.5L of polyethylene filler is filled in the cathode chamber and the anode chamber respectively and is used as a carrier of the microorganism; the concentration of the inlet water pyridine is 50mg/L, the concentration of the electrolyte sodium sulfate is 3mM, the concentration of the carbonate buffer system is 20mM, and the pH value is about 7.5; setting the system current intensity to be 25mA and the current density to be 2.5A/square meter; according to the simulation result of Fluent hydraulic simulation software, the self-circulation of the two chambers is set to be 1.2L/min, so that the uniform mass transfer is ensured. The inflow rate is about 2.2ml/min, and the hydraulic retention time of raw water in the cathode chamber and the anode chamber is 6 hours respectively; the internal circulation flow rate is about 6.6ml/min, and the circulation ratio is about 3. After the operation is stable, the inflow rate is increased to 4.4ml/min, and the hydraulic retention time of raw water in the cathode chamber and the anode chamber is 3 hours respectively; the internal circulation flow rate is about 22.2ml/min, and the circulation ratio is about 5. After long-time running detection, the effluent quality is stable, and the monitoring data are shown in table 4.
Table 4 monitoring data for comparative example 2
| Pyridine (mg/L) | TOC(mg/L) | TN(mg/L) | |
| Inflow water | 50 | 40 | 8.9 |
| Discharging water (two chambers each stay for 6h) | 0.5 | 2.8 | 1.9 |
| Removal rate% | 99 | 93 | 78.7 |
| Discharging water (two chambers each stay for 3h) | 23.1 | 19.8 | 6.5 |
| Removal rate% | 53.8 | 50.5 | 27.0 |
Examples 1 and 2 both adopt the reactor of the present invention, and have good removal effect on pollutants, which proves that the present invention has practicality and universality, and can be widely used for the treatment of refractory wastewater and toxic wastewater.
The same contaminant pyridine was removed in example 1, comparative example 1 and comparative example 2, and the contaminant concentration and the current intensity were also consistent. But the treatment effect and the reaction rate are obviously different: in example 1, the removal rate of pyridine was 100%, the removal rate of TOC was 94.5%, and the removal rate of total nitrogen was 84.3%; in comparative example 1, the pyridine removal rate was only 29%, the TOC removal rate was 17%, and the total nitrogen removal rate was 4.5%; in comparative example 2, under the conditions of 6h each of the hydraulic retention times of the two chambers, the pyridine removal rate was 99%, the TOC removal rate was 93%, and the total nitrogen removal rate was 78.7%, but after adjusting the hydraulic retention time to 3h (consistent with example 1), the contaminant removal rate was significantly reduced, the pyridine removal rate was 53.8%, the TOC removal rate was 50.5%, and the total nitrogen removal rate was 27%; therefore, the reactor has obvious advantages that the construction of the double biological chambers can improve the reaction efficiency and the total nitrogen removal rate, and the addition of the conductive medium can greatly improve the reaction rate and accelerate the reaction process, and is superior to the prior art.
Claims (7)
1. A method for treating sewage by using a conductive medium assisted double-biological-chamber electrochemical membrane bioreactor is characterized by comprising the following steps: the reactor comprises a direct current power supply, a power line, an electrode plate, a cathode chamber (3) and an anode chamber (6), wherein the cathode chamber (3) and the anode chamber (6) are separated by an ion exchange membrane (11); conductive media (9) are filled in the cathode chamber (3) and the anode chamber (6); the sewage treatment process comprises the following steps: the sewage firstly enters the cathode chamber (3) to generate a reduction reaction, then flows into the anode chamber (6) to generate an oxidation reaction, and is discharged from the anode chamber (6) after the pollutants are completely degraded.
2. The method of claim 1, wherein: the sewage in the anode chamber (6) flows back to the cathode chamber (3) at a reflux ratio of 100-600%.
3. The method of claim 1, wherein: the cathode chamber (3) and the anode chamber (6) are both provided with hydraulic self-circulation.
4. The method of claim 1, wherein: the conductive medium (9) is selected from one or more of granular activated carbon, graphite particles, metal particles and particles loaded with conductive materials on the surface, and the filling rate of the conductive medium is 10-70%.
5. The method of claim 1, wherein: the ion exchange membrane (11) is an anion exchange membrane, a cation exchange membrane or a proton exchange membrane.
6. The method of claim 1, wherein: the current intensity of the system is set to be 5-50mA, and the current density is set to be 0.5-5A/square meter.
7. The method of claim 1, wherein: electrolyte and a buffer system are added in the cathode chamber (3) and the anode chamber (6), wherein the electrolyte is sodium sulfate, and the concentration of the electrolyte is 0.1-15 mM; the buffer system is a carbonate buffer system, and the pH value of the cathode chamber (3) and the anode chamber (6) is ensured to be between 6 and 9.
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