CN111153506A - Anaerobic electrochemical membrane bioreactor and water treatment method thereof - Google Patents

Anaerobic electrochemical membrane bioreactor and water treatment method thereof Download PDF

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CN111153506A
CN111153506A CN201910899342.4A CN201910899342A CN111153506A CN 111153506 A CN111153506 A CN 111153506A CN 201910899342 A CN201910899342 A CN 201910899342A CN 111153506 A CN111153506 A CN 111153506A
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membrane
anaerobic
cathode
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张岩
陈锋华
曹孟京
柴毓蔓
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Beijing University of Technology
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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
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/14—Maintenance of water treatment installations
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Abstract

The invention provides an anaerobic electrochemical membrane bioreactor and a water treatment method thereof, belonging to the technical field of sewage treatment. The invention realizes the high-efficiency treatment of the wastewater, recovers energy in the form of collecting methane, and also solves the problems of high membrane pollution speed, high operation cost and the like in the anaerobic membrane biological treatment technology. The anaerobic electrochemical membrane bioreactor comprises a biological anode reaction zone and a cathode membrane filtering zone; the anaerobic microorganisms in the anode region oxidize organic matters in the wastewater, and the cathode membrane filtering region utilizes the dual functions of the functional conductive carbon nanotube hollow fiber membrane: the ultrafiltration membrane is used for filtering pollutants to efficiently treat wastewater and is used as a cathode electrode to generate gas (methane or hydrogen) to wash the surface of the membrane so as to achieve the effect of effectively relieving membrane pollution. The method and the device enable the low-concentration waste water to stably run at low temperature, can generate methane rich in methane for recycling, and are simple in structure and convenient for actual operation.

Description

Anaerobic electrochemical membrane bioreactor and water treatment method thereof
Technical Field
The invention relates to an anaerobic electrochemical membrane bioreactor, in particular to a water treatment method of an anaerobic electrochemical membrane bioreactor for sewage treatment, belonging to the technical field of sewage treatment.
Background
The continuous demand for fresh water worldwide places a tremendous pressure on the available water resources. The recovery and reuse of wastewater and desalination are the only opportunities to increase the available water supply and are therefore critical to meeting the demand for fresh water resources. Especially domestic sewage, is an available water resource for many cities, and desalination of sea water is limited to cities near the coast. Traditional domestic sewage treatment processes based on activated sludge are energy intensive (0.6kWh/m) and occupy a large area. Considering that domestic wastewater is estimated to contain about 2kWh/m, there is an opportunity to offset the energy consumption of wastewater treatment by recovering the inherent energy.
Compared with the aerobic technology, the anaerobic membrane biological treatment technology has the greatest characteristic of converting organic matters in sewage into methane which is recyclable energy gas, and has the ecological, economic and technical advantages of less sludge production, relatively stable process, lower capital construction cost, low operation cost, less secondary pollution and the like. The problem of membrane fouling has been an important factor hindering the rapid development of anaerobic membrane biotechnology.
The microbial electrolytic cell can promote electron transfer through an external electric field, so that the number of electrons acceptable by a cathode in unit time is increased, the microbial metabolism rate is effectively improved, and the removal efficiency of organic matters is improved. In addition, because the oxidation-reduction potential of the anode substrate is higher than that of the cathode hydrogen evolution reaction, the addition of the microbial electrolysis cell can lead protons to obtain electrons from the cathode through an external circuit, thereby generating hydrogen. Therefore, when the microbial electrolytic cell is applied to an anaerobic membrane bioreactor, the recovery of energy substances is more facilitated, and meanwhile, the membrane pollution can be slowed down by generating methane on the surface of the cathode.
With the development of nanotechnology in a new era, carbon nanotube materials have been the focus of research due to their advantages of excellent conductivity, good network structure, high mechanical strength, and large specific surface area. By using the carbon nanotube modified membrane material as the bifunctional cathode electrode, the problems of low electric energy utilization rate and low membrane flux of a membrane modified by a conductive material are solved, and the problem that metal ions of the membrane modified by a metal material are discharged into a system, which can cause potential environmental risks and increase the cost, is avoided.
Disclosure of Invention
The anaerobic membrane biological technology and the microbial electrolysis cell are integrated to form the anaerobic electrochemical membrane bioreactor, so that the wastewater is efficiently treated, the energy is recovered in a methane collection mode, and the problems of high membrane pollution speed, high running cost and the like in the anaerobic membrane biological technology are solved.
The technical scheme of the invention is as follows:
an anaerobic electrochemical membrane bioreactor is obtained by combining anaerobic membrane biotechnology and microbial electrolysis batteries and is divided into a biological anode reaction area and a cathode membrane filtering area; the membrane module adopted by the membrane filtering area comprises a conductive carbon hollow fiber membrane, a conductive sealing glue and a water outlet, wherein the water outlet is connected with a water outlet pipe and is connected with a vacuum pump to pump out water; the conductive carbon hollow fiber membrane is connected with the water outlet through a conductive sealant; the upper end of the reactor is provided with a gas collecting pipe.
The membrane assembly is used as a cathode electrode, the whole body is vertically arranged in the middle of the reactor, and an anode electrode suitable for the existence of electrochemically active microorganisms (EAB) is arranged at the bottom of the reactor. The marsh gas generated on the surface of the cathode is collected by a gas collecting bag at the outlet at the upper end of the reactor
The anaerobic electrochemical membrane bioreactor housing is made of any suitable plastic or polycarbonate material to provide sufficient strength. The reactor has additional outlets at the upper end for insertion of reference electrodes, ORP electrodes, DO electrodes, etc.
The conductive hollow fiber membrane is a functional conductive hollow fiber membrane, and the pore diameter of the conductive hollow fiber membrane is 0.12-0.15 micrometer. The conductive hollow fiber membrane is a carbon material, a conductive polymer or a metal conductive composite material; the anode electrode is made of graphite carbon felt, carbon fiber brushes or metal conductive composite materials.
The water treatment method by using the anaerobic electrochemical membrane bioreactor comprises the following operation processes: the conductive hollow fiber cathode membrane is connected with a power supply cathode, the anode is connected with a power supply anode electrode, and the applied voltage is 0.4-1.0V; so that the conductive hollow fiber membrane plays a dual role: firstly, the electric repulsion between the membrane surface and the charged pollutants in water is enhanced, and the pollution of the membrane can be effectively relieved; and secondly, the membrane is used as a catalytic electrode to degrade water pollutants, so that the effluent quality is obviously improved.
The operation mode is as follows: and sewage is introduced into a biological reaction zone inoculated with anaerobic sludge at the bottom of the reactor from the water inlet pipe, then passes through a membrane filtering zone of a membrane component in the middle of the reactor, effluent obtained after filtering by the membrane component flows out of the water outlet pipe, and generated biogas is collected by the gas collecting bag, wherein the retention time is 8-72 hours.
The invention has the beneficial effects that:
the invention develops an anaerobic electrochemical membrane bioreactor system which has low energy consumption at low temperature, is environment-friendly and can produce energy. The reactor has simple and compact design, the process has quick start time, and the stable state can be quickly realized. Compared with the traditional anaerobic water treatment technology, the anaerobic membrane bioreactor can more effectively treat low-strength wastewater, and can slow down membrane pollution and recover energy in a methane form more quickly compared with an anaerobic membrane bioreactor.
(1) The conductive carbon nanotube hollow fiber membrane plays a dual role: firstly, the ultrafiltration membrane is used for filtering pollutants to obviously improve the quality of effluent water, and secondly, the membrane surface is flushed by methane or hydrogen generated by the cathode membrane electrode to effectively relieve the membrane pollution;
(2) the microbial electrolytic cell promotes electron transfer through an external electric field, so that the number of electrons acceptable by a cathode in unit time is increased, the microbial metabolism rate is effectively improved, and the removal efficiency of organic matters is improved; bubbles on the surface of a cathode membrane electrode of the anaerobic electrochemical membrane bioreactor can be used as a natural scouring mechanism to slow down membrane pollution;
(3) the anaerobic electrochemical membrane bioreactor which is composed of the conductive carbon nanotube hollow fiber membrane as the difunctional cathode electrode can stably run at low temperature, the conductive material of the anaerobic electrochemical membrane bioreactor does not pollute the environment, and simultaneously methane rich methane can be generated for recycling, so that low energy consumption is realized.
Drawings
FIG. 1 is a schematic diagram of a novel anaerobic electrochemical membrane bioreactor.
FIG. 2 is a scanning electron microscope image of the surface of the conductive carbon nanotube hollow fiber membrane.
FIG. 3 shows COD removal in the stable operation of the novel anaerobic electrochemical membrane bioreactor under the applied voltage of 0.4V and 0.7V.
FIG. 4 shows the membrane fouling with time when the novel anaerobic electrochemical membrane bioreactor is operated stably at applied voltages of 0.4V, 0.7V and 1.0V (wherein the voltage of 1.0V is the voltage during the start-up period of the reactor).
FIG. 5 is a graph of current density and coulombic efficiency of the novel anaerobic electrochemical membrane bioreactor as a function of time under applied voltages of 0.4V and 0.7V.
In fig. 1: 1. a water inlet peristaltic pump 2, a graphite carbon felt 3, a reaction column 4, a carbon nano tube modified PVDF hollow fiber membrane 5, an electrochemical workstation 6, a pressure sensor 7, a water outlet peristaltic pump 8, a PH electrode 9, an ORP electrode 10, a DO electrode 11 and a gas collection port 12
Detailed Description
The following further describes the specific embodiments of the present invention with reference to the technical solutions and the accompanying drawings.
Example (b): urban sewage treatment by utilizing conductive carbon nanotube hollow fiber membrane anaerobic electrochemical membrane bioreactor
The reactor consisted of 1 main reaction column (effective volume 3L) and 1 electrochemical station. The reactor main body is organic glass with the inner diameter of 47mm and the height of 50cm, the anaerobic activated sludge is positioned at the bottom of the reactor, the cathode is composed of an anti-pollution conductive hollow fiber membrane, the conductive hollow fiber membrane is 1 group of conductive carbon nano tube polyvinylidene fluoride hollow fiber membranes (CNT-PVDF-HFM) which contain 4 conductive carbon nano tube polyvinylidene fluoride hollow fiber membranes (CNT-PVDF-HFM) with the length of 30cm and the average pore diameter of 0.14 micron; the anode is composed of graphite carbon felt and is positioned at the bottom of the reactor. The top end of the reaction column is provided with 3 probe holes and 1 water outlet hole. The external part of the reactor is connected with an electrochemical workstation, an ORP on-line monitoring detector, a DO on-line detector and a pH on-line detector. The uppermost sampling port is connected to the lowermost sampling port and a peristaltic pump is added to promote internal circulation of the flow and enhance mass transfer between the water and the microorganisms. In this example, the additional voltage applied during the start-up period is 1.0V, and when the COD removal rate is stabilized, the additional voltage is adjusted to 0.7V and 0.4V, respectively.
In the operation process of the embodiment, the operation temperature is room temperature, and the sludge concentration of the main reaction zone is 3.442 g/L. The concentration of the domestic sewage entering the reactor is 400 +/-20 mg/L, the average COD concentration of the membrane effluent is 40 +/-8 mg/L, the COD removal rate is 90 +/-0.67 percent, and the organic matter removal effect is obvious.
The contents of gaseous methane and hydrogen were determined by gas chromatography, and the contents of soluble methane and soluble hydrogen were calculated by henry's law (formula 1).
PB＝Kx,B×XB(1)
In the formula: pBIs the equilibrium partial pressure of the gas in the gas phase, kpa; kx,BIs a henry constant whose value is related to the nature of temperature, solute and solvent, the henry coefficient being substantially unaffected by pressure; xBIs the mole fraction of gas dissolved in water. The mass fraction of methane and hydrogen in the mixed gas is multiplied by 1atm ((atm is a standard atmospheric pressure, 101.325 kpa)) by gas chromatography, the dissolved methane and dissolved hydrogen amount per liter of effluent are calculated by using Henry's law, and the total methane and hydrogen amount per day is further calculated.
The volume of the dissolved gas was calculated by the formula (2)
V＝nTR/P (2)
In the formula, n is the molar mass of the gas, and the T temperature is 298K because the experimental environment is normal temperature and normal pressure; the pressure is 1atm, R is a universal gas constant value of 0.08206L atm & mol-1·K-1。
The gas conversion for the AnEMBR system at different voltages is shown in table 1.
TABLE 1 gas conversion for different external voltage AnEMBR systems
Table.1Gas conversion for AnEMBR system under different voltage
Coulombic efficiency(Coulomb impact, CE) in the system is the actual electric quantity (Q) converted into the circuit by the anode microorganism through the degradation of the organic matters and the theoretical electric quantity (Q) provided by the oxidized organic mattersT) The ratio of (a) to (b) is used to measure the charge-discharge efficiency of the whole system. The calculation formula is as follows:
Figure RE-GDA0002441775790000051
Figure RE-GDA0002441775790000052
the system adopts a continuous flow water inlet and uninterrupted electrical stimulation mode, and can calculate the actual electric quantity converted into a circuit through the degradation of organic matters in the system through the following calculation formula:
Figure RE-GDA0002441775790000053
in the formula, i is the real-time current in the system loop, and t is the action time of the corresponding current.
All substrates of the system are acetic acid, and if the microorganisms of the system completely convert the acetic acid metabolism into coulombs of electrons, the theoretical electric quantity QTComprises the following steps:
QT＝F*b*m/M (5)
in the formula, F is a Faraday constant and takes the value of 96485 C.mol < -1 >; b is the number of moles of electrons lost per mole of substrate to complete oxidation, with 8 moles of electrons required for complete oxidation of 1 mole of acetic acid, and thus b is 8 in this system; m is the molar mass of the substrate and takes the value of 60.05 g/mol.
In the practical application of treating the organic wastewater, the difference value of the Chemical Oxygen Demand (COD) of inlet and outlet water to Q can be adoptedTAnd (6) performing calculation. The calculation formula is as follows:
Figure RE-GDA0002441775790000061
wherein b is oxygen as a standard,the number of electrons transferred by 1mol of organic matter is 4. CODinChemical oxygen demand for influent water; CODoutChemical oxygen demand for effluent; v is the volume of substrate solution treated;
Figure RE-GDA0002441775790000062
the molar mass of oxygen gas is 32 g.mol-1。
The coulomb efficiency of the system can be calculated by the above formula, and the time variation of the coulomb efficiency under different voltages after the system operates stably is shown in fig. 5.
It was calculated that the average coulombic efficiency of the AnEMBR system was 46.35% up to 53.69% when the external voltage was 0.7V and 34.84% up to 41.87% when the external voltage was 0.4V.
The electron reduction efficiency is the ratio of the total electron quantity for generating hydrogen and methane on the cathode surface to the total electron quantity in the whole loop, so as to measure the capability of the cathode surface to catalyze the electron reduction reaction in the AnEMBR system, and the calculation formula is as follows:
rcathode＝rcathode(H2)+rcathode(CH4) (7)
in the formula rcathode(H2) And rcathode(CH4) The calculation formula is that for the electron reduction efficiency of hydrogen production and methane production respectively:
Figure RE-GDA0002441775790000063
Figure RE-GDA0002441775790000064
in the formula (I), the compound is shown in the specification,
Figure RE-GDA0002441775790000065
and
Figure RE-GDA0002441775790000066
hydrogen and methane produced by the AnEMBR system, respectivelyThe total molar mass of (A) can be calculated by equation 1,
Figure RE-GDA0002441775790000067
in that
Figure RE-GDA0002441775790000068
Respectively, the molar mass of all electrons in a system loop which are all used for producing hydrogen or all used for producing methane theoretically is calculated by the following formula:
Figure RE-GDA0002441775790000069
Figure RE-GDA00024417757900000610
in the formula, "2" is the electron molar mass number required per 1mol of hydrogen reduced, and "8" is the electron molar mass number required per 1mol of methane reduced.
The electron reduction efficiency of the AnEMBR system at different voltages is shown in table 2:
TABLE 2 Electron reduction efficiency of the AnEMBR System
Table 2 Electronic reduction efficiency of AnEMBR system
Figure RE-GDA0002441775790000071
Energy gas conversion efficiency (E)Gas) The ratio of the total electric quantity required by the hydrogen and the methane actually generated by the AnEMBR system to the theoretical total electric quantity obtained by the organic substrate consumed by the anode microorganism is used for measuring the capacity of the AnEMBR system for processing the organic substrate into the energy gas. EGasThe calculation formula of (2) is as follows:
Figure RE-GDA0002441775790000072
in the formula (I), the compound is shown in the specification,
Figure RE-GDA0002441775790000073
and
Figure RE-GDA0002441775790000074
respectively the conversion efficiency of the system substrate to hydrogen and methane,
Figure RE-GDA0002441775790000075
and
Figure RE-GDA0002441775790000076
the total electron quantities required for the hydrogen and methane produced by the system, respectively. QTCan be calculated by the equations 5-4. Wherein
Figure RE-GDA0002441775790000077
And
Figure RE-GDA0002441775790000078
the calculation formula of (2) is as follows:
Figure RE-GDA0002441775790000079
Figure RE-GDA00024417757900000710
in the formula (I), the compound is shown in the specification,
Figure RE-GDA00024417757900000711
and
Figure RE-GDA00024417757900000712
the calculation can be made by equation 2.
The energy gas conversion efficiency of the AnEMBR system at different voltages is shown in Table 3
TABLE 3 energy gas conversion efficiency of the AnEMBR System
Table 3Energy gas conversion efficiency of AnEMBR system
Figure RE-GDA00024417757900000713
Energy recovery is a computational analysis of efficiency from both the total energy provided by the substrate and the total energy consumed by the system. Firstly, the system productivity is mainly reflected in the output of energy gas hydrogen and methane, so the total system energy WGasThe calculation formula is as follows:
Figure RE-GDA00024417757900000714
in the formula (I), the compound is shown in the specification,
Figure RE-GDA0002441775790000081
the heat of complete combustion, which is the amount of hydrogen unit substance, was 285.8kJ/mol,
Figure RE-GDA0002441775790000082
the heat of complete combustion per amount of methane substance had a value of 891.0 kJ/mol.
Total energy W provided by the substrateSThe calculation formula is as follows:
WS＝nS·ΔHS(16)
in the formula,. DELTA.HSThe heat of complete combustion of the amount of substrate unit mass, the system already acetic acid is an organic substrate with a value of 870.3 kJ/mol. n isSThe molar mass of substrate consumed by the system can be calculated by using the removal amount of COD
nS＝(CODin-CODout)*vS/64 (17)
In the formula, vSFor water yield, "64" is the mass of oxygen consumed per unit mass of acetic acid.
Energy conversion efficiency of substrate ηSThe calculation formula is as follows:
ηS＝WGas/WS(18)
the system power consumption is mainly embodied in the energy consumption of the water inlet and outlet pump and the energy consumption of the electric circuit of the MEC system. Wherein the pump WBThe theoretical energy consumption calculation formula is as follows:
WB＝PB·t＝(Q1γE1+Q2γE2)·t (19)
in the formula, PBFor the total power of the inlet and outlet pumps, Q1And Q2The water flow rate of the reactor is shown. Since the system employs a continuous flow, Q1＝Q2A value of 5.8X 10-9m 3/s; gamma is 9800N/m 3; e1For the water inlet head loss, the water level height of the reactor is taken as the standard, and the value is 0.4 m; e2For the loss of the water head, the average TMP was about 2.34 m.
Theoretical electric energy W consumed by system MECEThe calculation formula is as follows:
WE＝IEt (20)
where I is the loop current and E is the external voltage, the electrical energy conversion efficiency of the system is ηEThe calculation formula is as follows:
ηE＝WGas/(WB+WE) (21)
the energy conversion efficiency of the AnEMBR system at different voltages is shown in Table 4
TABLE 4 energy conversion efficiency of the AnEMBR System
Table 4 Energy conversion efficiency of AnEMBR system
Figure RE-GDA0002441775790000083
Figure 1
The working flow of the anaerobic membrane bioreactor is as follows:
(1) the anaerobic activated sludge is added into the tank body, the sludge amount is about 20 percent of the volume of the tank body, and then water is gradually injected until the tank body is full of water.
(2) Domestic sewage enters the activated sludge reaction zone from the bottom of the reactor through the water inlet pump.
(3) In the anaerobic reactor, under the higher mass transfer effect, methane (mainly methane and carbon dioxide) or hydrogen generated by decomposing organic matters in the wastewater by using the metabolic function of anaerobic microorganisms can wash the surface of the membrane, thereby slowing down the membrane pollution.
(4) Some gas formed in the sludge layer by the methane generated in the anaerobic state is attached to sludge particles, and the attached and unattached methane is collected by a gas collecting bag at the top.
(5) The sewage after the anaerobic reaction is filtered by the conductive hollow fiber membrane and then is discharged out of the reactor through the water outlet pump, and anaerobic sludge particles in the sewage are intercepted in an activated sludge area of the anaerobic reactor to the maximum extent.

Claims (4)

1. An anaerobic electrochemical membrane bioreactor is characterized in that the anaerobic electrochemical membrane bioreactor is divided into a biological anode reaction zone and a cathode membrane filtration zone; the membrane module adopted by the membrane filtering area comprises a conductive hollow fiber membrane, a conductive sealing adhesive and a water outlet, wherein the water outlet is connected with a water outlet pipe and is connected with a vacuum pump for pumping water; the conductive hollow fiber membrane is connected with the water outlet through the conductive sealant; the upper end of the reactor is provided with a gas collecting pipe which is connected with a gas collecting bag; the membrane assembly is used as a cathode electrode, the whole is vertically arranged in the reactor, and an anode electrode is arranged at the bottom of the reactor; the reference electrode, ORP electrode and DO electrode are inserted into the upper end of the reactor.
2. The anaerobic electrochemical membrane bioreactor as claimed in claim 1, wherein the conductive hollow fiber membrane is a functional conductive carbon nanotube hollow fiber membrane, and the average pore size of the membrane is 0.12-15 μm.
3. The anaerobic electrochemical membrane bioreactor of claim 1, wherein the anode electrode is a graphite carbon felt, a carbon fiber brush or a metal conductive composite.
4. The method for water treatment by using the anaerobic electrochemical membrane bioreactor as claimed in claim 1, which is characterized in that the operation process comprises the following steps: the conductive hollow fiber cathode membrane is connected with a power supply cathode, the anode is connected with a power supply anode electrode, and the applied voltage is 0.4-1.0V; the operation mode is as follows: and sewage is introduced into a biological reaction zone inoculated with anaerobic sludge at the bottom of the reactor from the water inlet pipe, then passes through a membrane filtering zone of a membrane component in the middle of the reactor, effluent obtained after filtering by the membrane component flows out of the water outlet pipe, and generated biogas is collected by the gas collecting bag, wherein the retention time is 8-72 hours.
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