An upflow anaerobic reactor-bioelectrochemical coupling process device

Abstract

This invention provides an upflow anaerobic reactor-bioelectrochemical coupling process device, comprising: a hollow main structure, a porous water distribution plate and an anaerobic sludge zone, an inlet, reserved holes, a first electrode module, a second electrode module, an external effluent resistor, an external power supply, a data collector, a three-phase separator, and an effluent outlet. The hollow main structure includes a cone substructure with its tip pointing downwards, a cylindrical substructure closed to the base of the cone substructure, and an effluent structure connected to the bottom of the cylindrical substructure. The cylindrical substructure is divided into multiple working zones from bottom to top by the porous water distribution plate. This invention can enrich electroactive microorganisms through electrochemical acclimation, accelerate electron transfer, speed up the conversion of intermediate metabolites, reduce the biotoxicity of wastewater removal processes and effluent, and achieve safe and efficient removal of PPCPs (polyphenolic compounds).

Description

Technical Field

[0001] This invention relates to the field of bioelectrochemical technology, and in particular to an upflow anaerobic reactor-bioelectrochemical coupled process device. Background Technology

[0002] Pharmaceuticals and personal care products (PPCPs) are emerging pollutants, mainly falling into two categories: one includes prescription and over-the-counter drugs such as antibiotics, corticosteroids, and anti-inflammatory drugs; the other includes personal care products containing ultraviolet absorbers and preservatives. Most of these drugs and personal care products cannot be absorbed or utilized by the human body and enter municipal sewage networks through urine and feces. PPCPs are recalcitrant substances with low biodegradability and high toxicity. Antibiotics, in particular, are lethal to microorganisms, and traditional biological methods are often ineffective in their removal. Therefore, these substances have been frequently detected in sludge and effluent from wastewater treatment plants in recent years. Although the overall concentration of PPCPs discharged into the natural environment is low, their stability, difficulty in decomposition, and tendency to accumulate pose significant risks to human health and the ecological environment if exposed to low doses over a long period.

[0003] Various methods are currently used to remove PPCPs from the environment, such as adsorption, advanced oxidation processes, membrane filtration, and many other technologies. However, the drawbacks of these technologies are obvious. For example, adsorption cannot ultimately remove PPCPs, requiring further treatment of the adsorbent to eliminate secondary pollution. Advanced oxidation processes can completely mineralize or decompose most organic matter, but their process costs are too high when used to treat PPCPs. Traditional biological methods have low operating costs and minimal environmental impact, but they are time-consuming.

[0004] Bioelectrochemical systems (BESs) exhibit excellent performance in degrading stubborn compounds and can effectively remove PPCPs. Microorganisms attached to the anode can reduce the overpotential of PPCP parent compounds and metabolites, while simultaneously using PPCPs as electron donors and carbon sources for metabolic removal. Microorganisms attached to the cathode can remove some PPCPs (chloramphenicol, aromatic hydrocarbons, etc.) through reduction processes. However, the construction cost of BESs is high, and their shock resistance is poor, making them unsuitable as a standalone unit for wastewater treatment. Therefore, combining BESs with other processes is considered. Anaerobic processes can treat various types of wastewater, offering advantages such as biogas recovery, low sludge production, low operating and construction costs, low carbon emissions, and low nutrient requirements. Upflow anaerobic reactors are one of the most commonly used anaerobic biotechnologies, offering advantages over other anaerobic technologies such as no need for stirring devices, small footprint, and strong adaptability, effectively compensating for the shortcomings of BESs. Therefore, a coupled upflow anaerobic reactor-bioelectrochemical process is considered. The key to the application and promotion of the upflow anaerobic reactor-bioelectrochemical coupling process lies in how to modify the existing configuration of the upflow anaerobic reactor and construct a low-cost, high-performance electrode module that can be scaled up or down according to the reactor size. Summary of the Invention

[0005] In order to overcome the shortcomings of the prior art, the purpose of this invention is to provide an upflow anaerobic reactor-bioelectrochemical coupling process device.

[0006] To achieve the above objectives, the present invention provides the following solution:

[0007] An upflow anaerobic reactor-bioelectrochemical coupling process device includes: a hollow main structure, a porous water distribution plate and an anaerobic sludge zone, an inlet, reserved holes, a first electrode module, a second electrode module, an effluent external resistor, an external power supply, a data collector, a three-phase separator, and an effluent outlet; the hollow main structure includes a cone substructure with its apex pointing downwards, a cylindrical substructure closed to the bottom edge of the cone substructure, and an effluent structure connected to the bottom of the cylindrical substructure; the cylindrical substructure is divided into multiple working zones from bottom to top by the porous water distribution plate; each working zone is provided with the reserved holes;

[0008] The anaerobic sludge zone is located within the conical substructure and the first working zone; the inlet is located in the first working zone; the reserved holes are located in the second to fifth working zones; both the first and second electrode modules include at least one anode and one cathode; the anodes of the first and second electrode modules are located in the third working zone; the cathodes of the first and second electrode modules are located in the fourth working zone; the anodes are connected to one end of the effluent external resistor and the data collector via the reserved holes; the cathodes are connected to one end of the external power supply and the data collector via the reserved holes; the other end of the external power supply is connected to the other end of the effluent external resistor; the three-phase separator penetrates the sixth working zone and the effluent structure and is connected to the outside; the effluent outlet is located on the effluent structure.

[0009] Preferably, both the first electrode module and the second electrode module are disposed on the porous water distribution plate; both the first electrode module and the second electrode module have a porous configuration.

[0010] Preferably, the first electrode module consists of two cylinders made of stainless steel mesh and graphite particles; the graphite particles and the circular stainless steel mesh are alternately filled inside the stainless steel mesh cage, and three titanium wires are inserted through the entire stainless steel mesh cage.

[0011] Preferably, the second electrode module comprises two cylinders made of stainless steel mesh and carbon cloth; the second electrode module is formed by sewing and rolling together rectangular carbon cloth and rectangular stainless steel mesh using titanium wire.

[0012] Preferably, the titanium wire is connected to an external circuit through the reserved hole.

[0013] According to specific embodiments provided by the present invention, the present invention discloses the following technical effects:

[0014] This invention provides an upflow anaerobic reactor-bioelectrochemical coupling process device, comprising: a hollow main structure, a porous water distribution plate and an anaerobic sludge zone, an inlet, reserved holes, a first electrode module, a second electrode module, an effluent external resistor, an external power supply, a data collector, a three-phase separator, and an effluent outlet; the hollow main structure includes a cone substructure with its apex pointing downwards, a cylindrical substructure closed to the base of the cone substructure, and an effluent structure connected to the bottom of the cylindrical substructure; the cylindrical substructure is divided into multiple working zones from bottom to top by the porous water distribution plate; each working zone is provided with the reserved holes; the anaerobic sludge zone is located within the cone substructure and the first working zone; the inlet is provided in the first working zone. The second to fifth working areas are provided with the reserved holes; the first electrode module and the second electrode module each include at least one anode and a cathode; the anodes of the first electrode module and the second electrode module are located in the third working area; the cathodes of the first electrode module and the second electrode module are located in the fourth working area; the anodes are connected to one end of the effluent external resistor and the data collector through the reserved holes; the cathodes are connected to one end of the external power supply and the data collector through the reserved holes; the other end of the external power supply is connected to the other end of the effluent external resistor; the three-phase separator penetrates the sixth working area and the effluent structure and is connected to the outside; the effluent outlet is located on the effluent structure. This invention can enrich electroactive microorganisms through electrochemical directional acclimatization, accelerate electron transfer, speed up the conversion of intermediate metabolites, reduce the biotoxicity of the wastewater removal process and the effluent, and achieve safe and efficient removal of PPCPs-like substances. Attached Figure Description

[0015] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0016] Figure 1 A schematic diagram of an upflow anaerobic reactor-bioelectrochemical coupling process device provided in an embodiment of the present invention;

[0017] Figure 2 This is a schematic diagram of a porous water distribution plate structure provided in an embodiment of the present invention; wherein... Figure 2 (a) is a schematic diagram of the water distribution plate in the clear water zone according to an embodiment of the present invention; Figure 2 (b) is a schematic diagram of the sludge zone water distribution plate according to an embodiment of the present invention;

[0018] Figure 3 This is a schematic diagram of the stainless steel mesh-graphite particle electrode module structure provided in an embodiment of the present invention; wherein... Figure 3 (a) is a rectangular stainless steel mesh sheet; Figure 3 (b) is a circular stainless steel mesh sheet; Figure 3 (c) represents graphite particles; Figure 3 (d) is a stainless steel mesh-graphite particle electrode module;

[0019] Figure 4 This is a schematic diagram of the stainless steel mesh-carbon cloth electrode module structure provided in an embodiment of the present invention; wherein... Figure 4 (a) is a rectangular carbon cloth sheet; Figure 4 (b) is a rectangular stainless steel mesh sheet; Figure 4 (c) is a stainless steel mesh-carbon cloth electrode module;

[0020] Figure 5 This is a graph showing the change of output voltage over time for different electrode modules provided in an embodiment of the present invention.

[0021] Figure 6 This is a schematic diagram of the results provided in an embodiment of the present invention; wherein Figure 6 (a) COD removal rate of the comparative examples and embodiments of the present invention; Figure 6 (b) The removal rate of SMX in the comparative examples and embodiments of the present invention;

[0022] Explanation of reference numerals in the attached figures:

[0023] 1-Anaerobic sludge zone, 2-Inlet, 3-Reserved hole, 4-Anode, 5-Cathode, 6-Exit water external resistance, 7-External power supply, 8-Data collector, 9-Three-phase separator, 10-Outlet. Detailed Implementation

[0024] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0025] The purpose of this invention is to provide an upflow anaerobic reactor-bioelectrochemical coupling process device, which can enrich electroactive microorganisms through electrochemical acclimatization, accelerate electron transfer, speed up the conversion of intermediate metabolites, reduce the biotoxicity of wastewater removal process and effluent, and achieve safe and efficient removal of PPCPs.

[0026] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0027] Figure 1 A schematic diagram of an upflow anaerobic reactor-bioelectrochemical coupling process device provided in an embodiment of the present invention is shown below. Figure 1 As shown, the device includes a hollow main structure, an anaerobic sludge zone 1, an inlet 2, a reserved hole 3, an anode 4, a cathode 5, an external resistor for effluent 6, an external power supply 7, a data collector 8, a three-phase separator 9, and an outlet 10.

[0028] Preferably, its hollow main structure consists of six cylindrical sections with an inner diameter of 120 mm, a wall thickness of 10 m, and a height of 200 m, and a conical section with a height of 150 mm, with an overall height of 1350 mm.

[0029] Preferably, the four cylindrical sections are provided with reserved holes for external circuits;

[0030] Preferably, each section is fitted with a perforated water distribution plate (e.g., Figure 2 As shown), the cathode and anode are placed on the third and fourth water distribution plates from the top, respectively;

[0031] In another aspect of the present invention, two sets of electrode modules, both of which are porous and placed on a water distribution plate, are provided. Each set of electrode modules includes at least one cathode module and an anode module.

[0032] Preferably, both the anode module and the cathode module are cylindrical porous structures;

[0033] Preferably, the anode and cathode of the first set of electrode modules are two cylinders made of stainless steel mesh and graphite particles (e.g., Figure 3 (d) is shown);

[0034] Preferably, the electrode module consists of cylindrical graphite particles and circular stainless steel mesh alternately filled in a stainless steel mesh cage, with three titanium wires inserted through the entire electrode module.

[0035] Preferably, the anode and cathode of the second set of electrode modules are two cylinders made of stainless steel mesh and carbon cloth (e.g., Figure 4 (as shown in (c));

[0036] Preferably, the electrode module is formed by sewing and rolling together rectangular carbon cloth and rectangular stainless steel mesh with titanium wire;

[0037] Preferably, the anode and cathode are connected to an external circuit via a pre-installed titanium wire to form an enhanced wastewater treatment device;

[0038] Preferably, the external circuitry includes a controllable DC power supply, an external resistor, and a data acquisition device;

[0039] Preferably, the DC power supply can apply an external voltage to enhance processing efficiency, and the data collector is used to collect and transmit current and voltage data;

[0040] Preferably, the enhanced wastewater treatment device is placed into the modified upflow anaerobic reactor to form an upflow anaerobic-bioelectrochemical coupled process device.

[0041] As an optional implementation, the hollow main structure consists of six cylindrical sections with an inner diameter of 120mm, a wall thickness of 10mm, and a height of 200mm, and one conical section with a height of 150mm. Specifically, from the second to the fifth section from the top, a 5mm diameter pre-reserved hole is provided, which can be adjusted according to actual conditions, ranging from 3mm to 8mm; the water distribution plate in the clear water zone has an opening rate of 20% and an opening diameter of 8mm, which can be adjusted according to actual conditions, ranging from an opening rate of 15% to 25% and an opening diameter of 5mm to 100mm; the water distribution plate in the sludge zone has an opening rate of 7% and an opening diameter of 3mm, which can be adjusted according to actual conditions, ranging from an opening rate of 5% to 10% and an opening diameter of 2mm to 5mm; the distance from the inlet to the bottom is 6cm, which can be adjusted according to actual conditions, ranging from 3cm to 9cm.

[0042] Figure 3 This is a schematic diagram of the stainless steel mesh-graphite particle electrode module structure according to an embodiment of the present invention. Figure 3 As shown, a standard stainless steel mesh-graphite particle electrode module is 100mm high and 120mm in diameter, filled with five layers of graphite particles, each 10mm high and 10mm in diameter. A single module is cut from 304 stainless steel mesh with a 24-mesh aperture and a 0.21mm wire diameter. Figure 3 (a) shows a rectangle with a length of 380 mm and a width of 100 mm. Figure 3 (b) shows six 120mm diameter circles as the skeleton of the electrode module, with a certain amount of Figure 3(c) The graphite particles with a height of 10 mm and a diameter of 10 mm are soaked in 1 mol / L hydrochloric acid for 24 h, then taken out and rinsed three times with deionized water and dried for later use; a rectangular stainless steel mesh is rolled into a cylinder and fixed with titanium wire. A circular stainless steel mesh is used as one bottom surface of the cylinder and fixed with titanium wire. Then, two layers of graphite particles are filled inside, and a circular stainless steel mesh is placed. This process is repeated five times. Finally, a circular stainless steel mesh is used as one top surface of the cylinder and fixed with titanium wire. Finally, three titanium wires are inserted for external circuitry. In the specific implementation process, the above parameters can be adjusted according to the actual size of the reactor. The adjustment range is as follows: the wire diameter of the stainless steel mesh is 0.05mm-0.6mm, preferably 0.2mm-0.3mm; the mesh size is 5-50 mesh, preferably 20-30 mesh; the height of the graphite particles is 5mm-20mm, preferably 8mm-15mm; the diameter of the graphite particles is 5mm-20mm, preferably 8mm-15mm; the diameter of the titanium wire is 0.5mm-3mm, preferably 1mm-2.5mm; the overall height of the module is 50mm-200mm, preferably 80mm-150mm; the overall diameter of the module is 50mm-200mm, preferably 80mm-150mm.

[0043] Figure 4 This is a schematic diagram of the stainless steel mesh-graphite particle electrode module structure according to an embodiment of the present invention. As shown in the figure, a standard stainless steel mesh-carbon cloth electrode module is 100mm high and 120mm in diameter. A module is cut from 304 stainless steel mesh with a 24-mesh aperture and a wire diameter of 0.21mm. Figure 4 (b) A rectangle measuring 1000mm in length and 100mm in width, as shown, serves as the skeleton of the electrode module. A piece of carbon cloth is cut from this skeleton. Figure 4 (a) shows a rectangle 1000mm long and 100mm wide as the main body of the electrode module. After sewing the two together with titanium wire, it is rolled into a cylinder, and finally, three titanium wires are inserted for external circuitry. In the specific implementation, the above parameters can be adjusted according to the actual size of the reactor. The adjustment range is as follows: the wire diameter of the stainless steel mesh is 0.05mm-0.6mm, preferably 0.2mm-0.3mm; the mesh count is 5-50 mesh, preferably 20-30 mesh; the length of the stainless steel mesh rectangle is 100mm-2000mm, preferably 500mm-1500mm; the width is 50mm-200mm, preferably 80mm-150mm; the length of the carbon cloth rectangle is 100mm-2000mm, preferably 500mm-1500mm; the width is 50mm-200mm, preferably 80mm-150mm; the diameter of the titanium wire is 0.5mm-3mm, preferably 1mm-2.5mm.

[0044] A reference electrode is placed between the cathode module and the anode module to record the potential changes of the cathode module and the anode module. In this embodiment, an Ag / AgCl reference electrode (+0.197V vs. standard hydrogen electrode) is used. An external data acquisition instrument is connected to record one layer of data every 3min-20min, preferably 5min-15min. In this embodiment, a Keithley 2700 data logger is used, recording sequential data every 10min.

[0045] An external DC power supply is applied, with a voltage of 0-2V, preferably 0.3V-0.7V. In this embodiment, the MAISHENG MS-305DS DC power supply is used.

[0046] The external resistance value is 10Ω-5000Ω, preferably 100Ω-2000Ω, and in this embodiment it is 1000Ω.

[0047] During implementation, after the electrode module was installed in the reactor, sludge was inoculated at a sludge-to-water ratio of 1:3, and MLSS was controlled at 5000 mg / L. Startup was considered successful when the COD removal rate and potential reached stable values. Meanwhile, to better highlight the effect of this embodiment, a set of upflow anaerobic reactors without internal electrode modules was set up as a blank control. Except for the absence of internal electrode modules, all other design parameters were the same.

[0048] Figure 5 The diagram shows the output voltage over time of the reactors with built-in stainless steel mesh-graphite particle electrode modules and built-in stainless steel mesh-carbon cloth electrode modules in the embodiments. After reaching a stable state, the power density of the reactor with the built-in stainless steel mesh-graphite particle electrode module can reach 30.7 ± 1.2 mW / m². 2 The reactor with a built-in stainless steel mesh-carbon cloth electrode module can achieve a power density of 33.1 ± 0.8 mW / m². 2 .

[0049] Figure 6The chart shows a comparison of the COD removal rates of the examples and comparative examples for treating wastewater containing sulfamethoxazole (SMX). When the influent organic loads are 500 mg / L, 650 mg / L, and 800 mg / L, the COD removal rates of the comparative example are 73.5 ± 2.7%, 71.7 ± 0.8%, and 68.2 ± 0.5%, respectively; the COD removal rates of the stainless steel mesh-graphite particle electrode module example are 86.3 ± 1.2%, 85.3 ± 0.8%, and 86.1 ± 0.5%, respectively; and the COD removal rates of the stainless steel mesh-carbon cloth electrode module example are 88.2 ± 1.6%, 87.2 ± 0.9%, and 87.4 ± 0.5%, respectively. The comparative examples showed SMX removal rates of 63.9±2.5%, 71.4±3.1%, and 70.9±1.7%, respectively; the stainless steel mesh-graphite particle electrode module examples showed SMX removal rates of 76.5±1.2%, 83.3±3.1%, and 80.1±4.8%, respectively; and the stainless steel mesh-carbon cloth electrode module examples showed SMX removal rates of 79.1±3.8%, 85.1±3%, and 82.1±1.6%, respectively. These results indicate that the examples maintained stable COD and SMX removal rates even under high organic loads.

[0050] The beneficial effects of this invention are as follows:

[0051] (1) The modified upflow reactor in this invention has a more uniform water distribution inside and provides external conditions for the addition of the electrode module.

[0052] (2) The electrode module in this invention is made of stainless steel mesh, graphite particles and carbon cloth. Each material has good plasticity, is easy to process and form, has good conductivity and is inexpensive. Moreover, it is constructed by combining metal materials as the skeleton and carbon-based materials as fillers, which takes into account both biocompatibility and electron transfer efficiency.

[0053] (3) The electrode module in this invention has a simple overall design, flexible installation and convenient maintenance; it can be scaled up or down according to the process and reactor configuration, and can be used as a single module or multiple modules in series or parallel; it can also apply external voltage and potential according to changes in water quality and effluent requirements.

[0054] (4) The electrode module in this invention can enrich electroactive microorganisms through electrochemical directional domestication, accelerate electron transfer, speed up the conversion of intermediate metabolites, reduce the biological toxicity of wastewater removal process and effluent, and achieve safe and efficient removal of PPCPs.

[0055] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other.

[0056] This document uses specific examples to illustrate the principles and implementation methods of the present invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of the present invention. Furthermore, those skilled in the art will recognize that, based on the ideas of the present invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of the present invention.

Claims

1. An Upflow Anaerobic Reactor-bioelectrochemical coupling process device, characterized by, include: The system comprises a hollow main structure, a porous water distribution plate and an anaerobic sludge zone, an inlet, reserved holes, a first electrode module, a second electrode module, an external effluent resistor, an external power supply, a data collector, a three-phase separator, and an outlet. The hollow main structure includes a cone-shaped substructure with its apex pointing downwards, a cylindrical substructure connected to the bottom edge of the cone-shaped substructure, and an outlet structure connected to the bottom of the cylindrical substructure. The cylindrical substructure is divided into multiple working zones from bottom to top by the porous water distribution plate. Each working zone is provided with the reserved holes. The anaerobic sludge zone is located within the conical substructure and the first working zone; the inlet is located in the first working zone; the reserved holes are located in the second to fifth working zones; both the first and second electrode modules include at least one anode and one cathode; the anodes of the first and second electrode modules are located in the third working zone; the cathodes of the first and second electrode modules are located in the fourth working zone; the anodes are connected to one end of the effluent external resistor and the data collector via the reserved holes; the cathodes are connected to one end of the external power supply and the data collector via the reserved holes; the other end of the external power supply is connected to the other end of the effluent external resistor; the three-phase separator penetrates the sixth working zone and the effluent structure and is connected to the outside; the effluent outlet is located on the effluent structure. The first electrode module consists of two cylinders made of stainless steel mesh and graphite particles; the graphite particles and the circular stainless steel mesh are alternately filled inside the stainless steel mesh cage, with three titanium wires inserted through the entire stainless steel mesh cage. The specific arrangement is as follows: The standard stainless steel mesh-graphite particle electrode module is 100mm high and 120mm in diameter. It is filled with five layers of graphite particles, each 10mm high and 10mm in diameter. A 304 stainless steel mesh with a 24-mesh aperture and 0.21mm wire diameter is used as the raw material. A rectangle 380mm long and 100mm wide and six circles 120mm in diameter are cut to form the electrode module's skeleton. A certain amount of graphite particles, each 10mm high and 10mm in diameter, are soaked in 1mol / L hydrochloric acid for 24 hours. The particles are then removed, rinsed three times with deionized water, and dried. The rectangular stainless steel mesh is rolled into a cylinder and fixed with titanium wire. A circular stainless steel mesh is used as one base of the cylinder and fixed with titanium wire. Two layers of graphite particles are then filled inside, and another circular stainless steel mesh is placed next. This process is repeated five times. Finally, a circular stainless steel mesh is used as one top surface of the cylinder and fixed with titanium wire. Three titanium wires are then inserted for external circuitry. The second electrode module comprises two cylinders made of stainless steel mesh and carbon cloth; the second electrode module is formed by sewing and rolling together rectangular carbon cloth and rectangular stainless steel mesh using titanium wire, specifically arranged as follows: The standard stainless steel mesh-carbon cloth electrode module is 100mm high and 120mm in diameter. A rectangle 1000mm long and 100mm wide is cut from 304 stainless steel mesh with a 24-mesh aperture and a wire diameter of 0.21mm to serve as the skeleton of the electrode module. A rectangle 1000mm long and 100mm wide is cut from carbon cloth to serve as the main body of the electrode module. The two are sewn together with titanium wire and rolled into a cylinder. Finally, three titanium wires are inserted for external circuitry. A reference electrode is placed between the cathode and anode to record the potential changes at the cathode and anode. The Ag / AgCl reference electrode used is a +0.197V vs SHE standard hydrogen electrode. An external data acquisition instrument is connected to record one layer of data every 3-20 minutes. An external DC power supply is connected, applying a voltage of 0-2V, and the external resistance value is 10Ω-5000Ω. During the implementation, after the electrode module is installed in the reactor, sludge is inoculated at a sludge-to-water ratio of 1:3, and MLSS is controlled at 5000mg / L. When the COD removal rate and potential reach stable values, the start-up is considered successful. When the influent organic load was 500 mg / L, 650 mg / L, and 800 mg / L, the COD removal rates of the stainless steel mesh-graphite particle electrode module were 86.3±1.2%, 85.3±0.8%, and 86.1±0.5%, respectively; the COD removal rates of the stainless steel mesh-carbon cloth electrode module were 88.2±1.6%, 87.2±0.9%, and 87.4±0.5%, respectively; the SMX removal rates of the stainless steel mesh-graphite particle electrode module were 76.5±1.2%, 83.3±3.1%, and 80.1±4.8%, respectively; and the SMX removal rates of the stainless steel mesh-carbon cloth electrode module were 79.1±3.8%, 85.1±3%, and 82.1±1.6%, respectively.

2. The Upflow Anaerobic Reactor-bioelectrochemical coupling process apparatus according to claim 1, characterized in that, Both the first electrode module and the second electrode module are disposed on the porous water distribution plate; both the first electrode module and the second electrode module are porous.

3. The Upflow Anaerobic Reactor-bioelectrochemical coupling process apparatus according to claim 1, characterized in that, The titanium wire is connected to the external circuit through the reserved hole.

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