Overflow type electrochemical reactor

Abstract

Belonging to the technical field of electrochemical oxidation, the invention relates to an overflow electrochemical reactor, which comprises a reaction cavity provided with a medium inlet and a medium outlet; the outer cover plate is connected to the opening of the reaction cavity in a sealing manner; the at least one group of electrode reaction units are arranged in the reaction cavity; the electrode reaction unit comprises an anode grating plate and a cathode grating plate which are parallel and opposite to each other, and an anode plate array and a cathode plate array which are arranged between the anode grating plate and the cathode grating plate; and the anode plates and the cathode plates in the anode plate array and the cathode plate array are staggered and arranged in parallel at equal intervals. The reactor has the characteristics of simple and compact structure, light weight and large contact area between the anode and the conductive part, and can solve the problems of complex structure, high processing cost of non-standard parts and poor contact between the anode and the conductive part of the existing reactor.

Description

Technical Field

[0001] This invention belongs to the field of electrochemical oxidation technology, and particularly relates to a flow-through electrochemical reactor. Background Technology

[0002] Electrochemical advanced oxidation technology is an environmentally friendly water treatment technology. Its basic principle is that under the action of an external electric field, strong oxidizing substances hydroxyl radicals (·OH) are generated on the anode surface, which mineralize recalcitrant organic pollutants into substances such as carbon dioxide and water on the anode surface, thereby purifying wastewater.

[0003] Among numerous anode materials, boron-doped diamond (BDD) electrodes are considered the most promising high-performance anode material due to their extremely high oxygen evolution overpotential, wide electrochemical window, extremely low background current, and excellent physicochemical stability and antifouling ability. They are capable of efficiently degrading various persistent organic pollutants. However, existing electrochemical reactors using BDD electrodes still have the following shortcomings in structural design and practical applications:

[0004] First, existing reactors typically have complex structures and are costly to manufacture. To achieve reliable sealing, insulation, and electrical connections, traditional designs often employ complex mechanical clamping and fastening structures, resulting in a large number of installation components and non-standard custom parts. This not only makes the reactor bulky but also significantly increases material processing and manufacturing costs.

[0005] Secondly, BDD electrodes often use brittle materials such as silicon as the substrate, making them highly sensitive to mechanical stress. Existing designs typically use conductive metal sheets to clamp the electrodes. If the clamping force is uneven or excessive, it can easily lead to stress concentration and breakage of the electrodes, affecting the stable operation of the reactor. Furthermore, the clamping connection has a small effective contact area and high contact resistance. Under high current density operating conditions, localized overheating can easily occur at the connection point, causing not only energy loss but also potential safety hazards, hindering the continuous and efficient conduct of the electrochemical reaction.

[0006] Furthermore, the existing reactors have complex sealing structures, require a large amount of fluororubber seals, and are inconvenient to install and disassemble, making electrode replacement difficult and causing inconvenience for on-site maintenance. At the same time, the reactor structure lacks flexibility, making it difficult to expand or adjust the electrode units according to the actual processing scale, thus limiting its adaptability to different application scenarios.

[0007] In summary, existing electrochemical advanced oxidation reactors still need improvement in terms of structural simplification, cost control, electrode protection, conductivity reliability, and ease of maintenance. There is an urgent need to develop a flow-through electrochemical reactor that is simple in structure, low in cost, easy to maintain, and suitable for high-performance electrode materials. Summary of the Invention

[0008] To address the shortcomings of existing technologies, this invention provides a flow-through electrochemical reactor, which features a simple and compact structure, light weight, and a large contact area between the anode and conductive components, thereby solving the problems of complex structure, high processing cost of non-standard parts, and poor contact between the anode and conductive components in existing reactors.

[0009] A flow-through electrochemical reactor, comprising:

[0010] A reaction chamber, wherein the reaction chamber is provided with a medium inlet and a medium outlet;

[0011] The outer cover plate is sealed to the opening of the reaction chamber;

[0012] At least one set of electrode reaction units is disposed inside the reaction chamber;

[0013] The electrode reaction unit includes an anode grid plate and a cathode grid plate arranged in parallel and opposite directions, as well as an anode plate array and a cathode plate array disposed between the anode grid plate and the cathode grid plate; the anode plates and cathode plates in the anode plate array and the cathode plate array are arranged alternately and parallel at equal intervals.

[0014] The reaction chamber is made of fiber-reinforced polypropylene and is processed from sheet material by ultrasonic welding. The outside of the reaction chamber is equipped with reinforcing ribs, and the inside of the reaction chamber is equipped with a flow guide plate at the medium inlet end.

[0015] The electrode reaction unit further includes:

[0016] An anode conductive strip is disposed on the anode grid plate and electrically connected to each anode plate in the anode plate array;

[0017] A cathode conductive strip is disposed on the cathode grid plate and electrically connected to each cathode plate in the cathode plate array;

[0018] The anode busbar is located on the side of the anode grid plate away from the cathode grid plate and is electrically connected to the surface of the anode conductive strip.

[0019] The cathode busbar is located on the side of the cathode grid plate away from the anode grid plate and is electrically connected to the surface of the cathode conductive strip.

[0020] The anode terminal connects to the anode busbar and extends to the outside of the reaction chamber;

[0021] The cathode terminal connects to the cathode busbar and extends to the outside of the reaction chamber.

[0022] Both the anode grid plate and the cathode grid plate are provided with rectangular grooves for installing conductive strips and slotted grids for installing electrode plate arrays; the anode grid plate and the cathode grid plate are fixedly connected by connectors to form a frame structure.

[0023] The anode and cathode conductive strips are provided with grooves for inserting electrode plates, and the sides of the anode and cathode conductive strips are provided with threaded holes for tightening the electrode plates with set screws.

[0024] The anode busbar and cathode busbar are respectively connected to the corresponding grid plate by fasteners, and the surface of the busbar is in close contact with the surface of the conductive strip to form a surface contact.

[0025] The anode and cathode terminals are flat conductive bolts, and a conical sealing gasket is provided between the flat conductive bolt and the outer cover plate or reaction chamber; one end of the flat conductive bolt is welded to the busbar, and the other end is connected to a copper busbar at the flat position.

[0026] The anode plate is made of boron-doped diamond electrode or shape-stabilized anode electrode, and the cathode plate is made of titanium metal or boron-doped diamond electrode.

[0027] When the cathode plate is made of titanium, the surface roughness Ra of the cathode plate is 0.4μm~0.8μm; when the cathode plate is made of boron-doped diamond electrode, the cathode plate is operated as the anode by switching the current direction, thereby removing the scale layer on the electrode surface.

[0028] The reaction chamber is provided with two or more sets of electrode reaction units along the water flow direction, and the sets of electrode reaction units are connected in parallel or in series by copper busbars.

[0029] By employing the above technical solution, the present invention has at least the following beneficial effects:

[0030] The flow-through electrochemical reactor provided by this invention has fewer installed components, resulting in a significant reduction in reactor weight; fewer customized components lead to lower processing costs, while a large number of standard parts contribute to lower costs.

[0031] The flow-through electrochemical reactor provided by this invention has fewer fastening points, a simple sealing structure, low fluororubber ring usage, reduced mechanical damage to the anode plate, and a compact structure.

[0032] The flow-through electrochemical reactor provided by this invention features a large contact area between the anode plate and the titanium connector, resulting in stable contact, which facilitates electrical conduction and reduces heat generation. The titanium connector utilizes a surface connection, allowing it to withstand higher current densities.

[0033] The flow-through electrochemical reactor provided by this invention is easy to install and disassemble, and the electrodes can be replaced as a whole in one go.

[0034] Based on the actual site conditions, the reaction chamber in the flow-through electrochemical reactor provided by this invention can be increased with several electrode reaction units to expand the anode usable area. Attached Figure Description

[0035] Figure 1 This is a schematic diagram of the overall structure of the flow-through electrochemical reactor provided in Embodiment 1 of the present invention;

[0036] Figure 2 This is a side view of the flow-through electrochemical reactor provided in Embodiment 1 of the present invention;

[0037] Figure 3 An exploded view of the flow-through electrochemical reactor provided in Embodiment 1 of the present invention;

[0038] Figure 4 This is a schematic diagram of the electrode reaction unit in the flow-through electrochemical reactor provided in Embodiment 1 of the present invention;

[0039] Figure 5 This is a schematic diagram of the flow-through electrochemical reactor provided in Embodiment 2 of the present invention;

[0040] Figure 6 This is a schematic diagram of the flow-through electrochemical reactor provided in Embodiment 3 of the present invention;

[0041] In the picture:

[0042] 1. Reaction chamber; 11. Square flange; 12. Rear plate; 13. Side plate; 14. Lower plate; 15. Upper plate; 16. Medium inlet; 17. Medium outlet; 18. Reinforcing rib; 2. Fluoropolymer ring; 3. Outer cover plate; 4. Flow guide plate; 500. Electrode reaction unit; 510. Anode reaction unit; 520. Cathode reaction unit; 511. Anode grid plate; 521. Cathode grid plate; 512. Anode conductive strip; 522. Cathode conductive strip; 513. Anode busbar; 523. Cathode busbar; 514. Anode flat conductive bolt; 524. Cathode flat conductive bolt; 515. Anode plate; 525. Cathode plate; 516. Titanium screw; 5111. Rectangular groove; 5211. Groove grid; 6. Conical sealing fluoropolymer gasket; 7. Copper busbar. Detailed Implementation

[0043] To better explain and facilitate understanding of the present invention, the technical solution and effects of the present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.

[0044] Example 1

[0045] like Figures 1-3As shown, this embodiment provides a flow-through electrochemical reactor, including a reaction chamber 1, an outer cover plate 3 sealing the reaction chamber 1, and a set of electrode reaction units 500 disposed within the reaction chamber 1. Terminals are provided on the reaction chamber 1 and the outer cover plate 3.

[0046] The reaction chamber 1, used to mount the electrode reaction unit 500, is made of fiber-reinforced polypropylene composite board and prepared using a melt extrusion process. Short-cut fiber-reinforced polypropylene granules are used as raw material, plasticized and extruded using a single / twin-screw extruder, and then cut to obtain a continuous sheet. This results in superior corrosion resistance and mechanical properties, improved heat distortion temperature, and enhanced long-term durability. Furthermore, each surface of the reaction chamber 1 is processed using ultrasonic welding. High-frequency mechanical vibration causes frictional heat generation at the contact interface molecules, achieving localized melting of the material under pressure, thus forming a strong joint. Multiple welding is performed at the internal corners of the reaction chamber 1, and secondary welding is performed at the external corners to increase the sealing performance of the reaction chamber 1.

[0047] In other embodiments, the reaction chamber 1 can also be made of PP, PVC, UPVC, fiberglass, PTFE-lined metal, or other acid and alkali resistant insulating materials. The reaction chamber 1 can also be obtained through processes such as mold making, machining, PTFE lining, and spraying.

[0048] The reaction chamber 1 has an opening at the front, and a square flange 11 is provided at the opening to seal with the outer cover plate 3. The square flange 11 has a through hole for connection with the outer cover plate 3. The outer cover plate 3 has a through hole corresponding to the square flange 11 of the reaction chamber 1. The outer cover plate 3 and the square flange 11 are locked and fixed together by bolts, gaskets, spring washers, and nuts. To ensure a good sealing effect and uniform stress on the outer cover plate 3 and the square flange 11, a large-diameter stainless steel gasket is used. A fluororubber ring 2 is provided between the outer cover plate 3 and the square flange 11 to ensure the airtightness of the outer cover plate 3 and the reaction chamber 1.

[0049] Furthermore, the rear plate 12 of the reaction chamber 1, which is opposite to the opening, is provided with a through hole for fixing the electrode reaction unit 500.

[0050] like Figure 2 As shown, two reinforcing ribs 18 are symmetrically distributed on the left and right side plates 13 of the reaction chamber 1. The reinforcing ribs 18 are connected to the square flange 11 and the rear plate 12 of the reaction chamber 1. Furthermore, the two reinforcing ribs 18 are equidistantly distributed on the left and right side plates 13 of the reaction chamber 1. This structural design of the reinforcing ribs 18 effectively increases the strength of the reaction chamber 1 and reduces its thickness, thereby reducing processing costs.

[0051] The reaction chamber 1 has a media inlet 16 on its lower plate 14 and a media outlet 17 on its upper plate 15. Water enters the reaction chamber 1 through the media inlet 16, flows through the electrode reaction unit 500, and exits the reaction chamber 1 through the media outlet 17. A large number of bubbles generated during the electrochemical process are carried out of the reaction chamber 1 by the water flow, ensuring the smooth operation of the electrochemical reaction. Furthermore, the media inlet 16 and media outlet 17 are respectively located at the center of the lower plate 14 and the upper plate 15 of the reaction chamber 1. A guide plate 4 is installed at the media inlet 16 inside the reaction chamber 1. The guide plate 4 is made of porous silicon carbide material, utilizing the porous structure of silicon carbide to distribute and evenly distribute the liquid. Simultaneously, porous silicon carbide material has excellent chemical properties, resisting corrosion from strong acids, strong alkalis, high-salt environments, and other organic substances. The baffle plate 4 plays a role in uniformly guiding the flow, avoiding uneven flow field inside the reaction chamber 1, and ensuring the smooth operation of the electrochemical treatment of organic wastewater.

[0052] Preferably, the connection between the reaction chamber 1 and the medium inlet 16 and the medium outlet 17 can take various forms. Threads can be machined in the center of the lower plate 14 and the upper plate 15 of the reaction chamber 1 to install external threads, flanges, pagodas, copying rings, etc., for the medium inlet 16 and the medium outlet 17. Alternatively, the medium inlet 16 and the medium outlet 17 can be installed by molding injection, hot melt welding, or other processing methods.

[0053] Among them, such as Figure 4 The electrode reaction unit 500 includes an anode grid plate 511 and a cathode grid plate 521 arranged opposite to each other and connected by a titanium screw 516. The anode grid plate 511 is positioned close to and parallel to the outer cover plate 3. An array of anode plates and an array of cathode plates are interleaved between the anode grid plate 511 and the cathode grid plate 521. The anode grid plate 511 has multiple closely arranged anode conductive strips 512, and the cathode grid plate 521 has multiple closely arranged cathode conductive strips 522. Furthermore, an anode busbar 513 is provided on the outer side of the anode grid plate 511, near the outer cover plate 3; correspondingly, a cathode busbar 523 is provided on the outer side of the cathode grid plate 521, near the rear plate 12.

[0054] Furthermore, the anode plate array consists of several anode plates 515, and the cathode plate array consists of several cathode plates 525, with the anode plates 515 and cathode plates 525 placed alternately. The anode plate array is placed on the anode grid plate 511, and the cathode plate array is placed on the cathode grid plate 521. Each anode plate 515 has a cathode plate 525 on both sides, and the anode plates 515 and cathode plates 525 are arranged in parallel and equidistantly to form the anode plate array and cathode plate array. The spacing between adjacent anode plates 515 and cathode plates 525 is controlled at 2mm. If the spacing is too large, energy consumption will increase; if the spacing is too small, short circuits may occur. This structure eliminates the need for complex structural design and significantly reduces machining costs and assembly labor and time costs.

[0055] The anode plate 515 is made of materials such as ruthenium-iridium titanium electrode, lead oxide electrode, tin oxide electrode, sub-titanium oxide electrode, and BDD electrode (boron-doped diamond electrode). Utilizing the principle of electrolysis, strong oxidizing substances, hydroxyl radicals (·OH), are generated on the surface of the anode plate 515. These radicals, through direct or indirect oxidation, mineralize recalcitrant organic pollutants into substances such as carbon dioxide and water on the anode surface, thereby purifying the wastewater. When the anode plate 515 is made of a BDD electrode, the boron doping range of the BDD electrode is 10%. 19 cm -3 ~10 22 cm -3 The microstructure of the BDD material in the anode plate 515 adopts various forms such as planar BDD, vertically oriented BDD, porous BDD, and two-dimensional BDD.

[0056] Meanwhile, the cathode plate 525 is made of pure titanium TA2 and is processed using wire cutting technology. Traditional laser processing can cause thermal stress that leads to deformation of the plate. Wire cutting avoids deformation or stress caused by cutting force and temperature. After wire cutting, the titanium plate is acid-washed to thoroughly remove the oxide layer and oil stains from the surface, and then mechanically polished to reduce the surface roughness to Ra 0.4μm~Ra0.8μm. Because the content of calcium and magnesium ions in actual organic wastewater is generally high, a large amount of OH- accumulates in the vicinity of the cathode surface during the electrochemical degradation of organic wastewater. - A strongly alkaline microenvironment will be generated on the electrode surface. In high OH... - Under certain concentration conditions, calcium and magnesium ions in water will react with OH- -The reaction forms a complex scale deposit on the surface of cathode plate 525. This scale layer is a poor conductor, increasing the interfacial resistance between the anode and cathode, leading to increased cell voltage and affecting the current efficiency and pollutant degradation efficiency of the entire electrochemical oxidation system. Reducing the surface roughness of cathode plate 525 can effectively reduce the adhesion of the scale layer to the cathode surface. During electrochemical operation, the scale layer is detached from the cathode surface by the scouring action of the high-speed water flow and carried away from the reactor. Therefore, reducing the surface roughness of the cathode can effectively reduce the adhesion of the scale layer.

[0057] Similarly, the cathode plate 525 can be made of BDD electrode material. By changing the current direction, when the previously scaled cathode plate 525 is converted into the anode plate 515, a high concentration of H2 is generated on the electrode plate surface. + This creates a localized, weakly acidic environment, which dissolves the scale layer on the electrode surface, loosening and peeling it off. The scale layer is then carried away by the high-speed water flow. When the cathode plate 525 is switched to the anode plate 515, the electrode material must maintain structural stability under strong acidity and high potential. Therefore, when using a BDD electrode as the cathode plate 525, changing the current direction will not reduce the pollutant degradation efficiency of the electrochemical oxidation system. This allows for continuous scale removal without shutting down the system, ensuring continuous operation of the electrochemical oxidation process.

[0058] The anode grid plate 511 and cathode grid plate 521 adopt a symmetrical structural design. Corresponding through holes are formed at the four edges of both the anode grid plate 511 and cathode grid plate 521. Titanium screws 516 pass through these through holes and are secured to the anode grid plate 511 and cathode grid plate 521 with titanium nuts. The anode grid plate 511, cathode grid plate 521, and titanium screws 516 form a frame structure for mounting the anode conductive strip 512, cathode conductive strip 522, cathode plate array, and anode plate array. Both the anode grid plate 511 and cathode grid plate 521 have rectangular grooves 5111 and grooved grids 5211, forming a structure where the grid plates are integrally machined. The rectangular groove 5111 is a rectangular groove adapted to fit the anode conductive strip 512 and the cathode conductive strip 522. It is machined along the corresponding direction of the grid plate and is used for precise placement and fixing of the conductive strip. The grooved grid 5211 is a multi-set, spaced groove-shaped limiting structure, machined according to the arrangement spacing of the anode plates 515 and cathode plates 525 of the cathode plate array and anode plate array, and is used for positioning the electrode plate array. Specifically, the rectangular groove 5111 of the anode grid plate 511 is set near the outer side, that is, near the outer cover plate 3, and the anode conductive strip 512 is installed on the rectangular groove 5111; the grooved grid 5211 of the anode grid plate 511 is set near the cathode grid plate 521, and the anode plate array is installed on the grooved grid 5211. The rectangular groove 5111 of the cathode grid plate 521 is located near the rear plate 12, and cathode conductive strips 522 are installed on the rectangular groove 5111. The grooved grid 5211 of the cathode grid plate 521 is located near the anode grid plate 511, and a cathode plate array is installed on the grooved grid 5211. The grooved grid 5211 can effectively limit the anode plate array and the cathode plate array, preventing the anode plate array and the cathode plate array from deforming or breaking under the scouring action of high-speed water flow, which could lead to short circuits.

[0059] The anode grating plate 511 and cathode grating plate 521 are made of polyvinyl chloride (PVC), which has excellent chemical corrosion resistance, good rigidity and strength, and is suitable for machining. Similarly, the anode grating plate 511 and cathode grating plate 521 can also be made of corrosion-resistant and machinable engineering plastics such as polytetrafluoroethylene (PTFE) and polyetheretherketone (PEEK).

[0060] Furthermore, the anode conductive strip 512 and the cathode conductive strip 522 have the same structure. Strip-shaped grooves are machined on the surfaces of both the anode conductive strip 512 and the cathode conductive strip 522, allowing insertion into the anode plate array and cathode plate array. Threads are machined on the side surfaces of the anode conductive strip 512 and the cathode conductive strip 522, allowing for lateral locking with set screws to secure the anode plate array and cathode plate array. This ensures a tighter fit between the electrode plates and the conductive strips, completely eliminating contact gaps and further reducing contact resistance. Compared to existing reactor conductive sheet designs, the clamping force acts directly on the electrode plate surface, increasing the contact area and structural strength. The electrode plates are tightly fitted to the anode conductive strip 512 and the cathode conductive strip 522, reducing surface contact resistance, reducing heat generation under high current density, and lowering energy consumption during the electrochemical reaction process. The anode conductive strip 512 and the cathode conductive strip 522 are made of titanium, but can also be made of corrosion-resistant conductive materials such as niobium, tantalum, titanium-based platinum coating, or titanium-based ruthenium-iridium titanium coating.

[0061] The anode busbar 513 and cathode busbar 523 are provided with holes for mounting the anode grid plate 511 and cathode grid plate 521, respectively. Titanium bolts are used to pass through the anode busbar 513 and cathode busbar 523 and lock them to the anode grid plate 511 and cathode grid plate 521, ensuring that the surface of the anode busbar 513 is in close contact with the surface of the anode conductive strip 512, and the surface of the cathode busbar 523 is in close contact with the surface of the cathode conductive strip 522. To ensure a tight fit between the busbar and the conductive strip, the contact surface between the busbar and the conductive strip needs to be machined to a low roughness Ra 0.4μm~Ra 0.8μm. This structure achieves surface contact to carry a higher current density and reduce heat generation and power consumption.

[0062] Furthermore, the anode busbar 513 and cathode busbar 523 can be made of conductive materials suitable for machining and oxidation resistance, such as industrial pure titanium, niobium, tantalum, or titanium plating, so that they can carry a large current density.

[0063] The terminals include an anode flat conductive bolt 514 mounted on the outer cover plate 3 and a cathode flat conductive bolt 524 mounted on the rear plate 12 of the reaction chamber 1. The anode flat conductive bolt 514 and the cathode flat conductive bolt 524 have the same structure and are machined into a columnar shape as terminals. One end of the terminal is threaded for connection and fixation to the rear plate 12 or the outer cover plate 3 of the reaction chamber 1; the other end of the terminal is machined into a smooth columnar surface. A conical sealing fluororubber gasket 6 is provided between the anode flat conductive bolt 514 and the outer cover plate 3 to ensure the sealing between the anode flat conductive bolt 514 and the outer cover plate 3; a conical sealing fluororubber gasket 6 is also provided between the cathode flat conductive bolt 524 and the rear plate 12 of the reaction chamber 1 to ensure the sealing between the cathode flat conductive bolt 524 and the reaction chamber 1. The anode flat conductive bolt 514 is connected to the anode busbar 513, and the cathode flat conductive bolt 524 is connected to the cathode busbar 523. The connection between the terminal block and the busbar can be achieved using inert gas shielded welding. Before welding, the contact surfaces of the terminal block and the busbar need to be ground smooth to remove the surface oxide layer. Both the terminal block and the busbar must be made of titanium from the same batch. After welding, vacuum annealing is performed to eliminate residual welding stress, forming a single integrated structure that can withstand higher current densities and greater strength. Alternatively, the connection between the terminal block and the busbar can also be achieved using machining, laser welding, or vacuum brazing.

[0064] Furthermore, the threaded portion of one end of the anode flat conductive bolt 514 is machined into a flat position, and a through hole is provided on the side of the flat position. Two copper busbars 7 are installed on each side of the flat position. Each copper busbar 7 has through holes at both ends; one end is connected to the anode flat conductive bolt 514 by a bolt, and the other end is used to install a copper terminal block. Similarly, the threaded portion of one end of the cathode flat conductive bolt 524 is machined into a flat position, and a through hole is provided on the side of the flat position. Two copper busbars 7 are installed on each side of the flat position. Each copper busbar 7 has through holes at both ends; one end is connected to the cathode flat conductive bolt 524 by a bolt, and the other end is used to install a copper terminal block. The surface of the copper busbar 7 is tin-plated to improve its oxidation resistance.

[0065] Preferably, the end surface of the copper busbar 7 is provided with a through hole. The temperature sensing end of the thermocouple is inserted into the through hole and fixed with high-temperature thermally conductive insulating adhesive to ensure tight contact between the thermocouple and the copper busbar 7. The thermocouple is connected to a PLC system and a temperature alarm is set to measure the heating of the copper busbar 7 during electrochemical operation. When the temperature of the copper busbar 7 is abnormal, the power is cut off in time.

[0066] The anode grid plate 511, anode plate array, anode conductive strip 512, anode busbar 513, and anode flat conductive bolt 514 constitute the anode reaction unit 510, which is an integral structure. The cathode grid plate 521, cathode plate array, cathode conductive strip 522, cathode busbar 523, and cathode flat conductive bolt 524 constitute the cathode reaction unit 520, which is also an integral structure. The anode reaction unit 510 and the cathode reaction unit 520 can be replaced separately as a whole. Only the titanium screws at both ends of the busbar used to fix the busbar to the grid plate need to be removed to remove the anode reaction unit 510 for replacement. This allows for efficient and rapid replacement of the anode and cathode plates on-site, reducing on-site reactor maintenance time.

[0067] In the flow-through electrochemical reactor provided by this invention, the cathode conductive component and the anode conductive component are located on opposite sides of the reaction chamber 1, directly reducing the electric field strength and increasing the resistance between the cathode and anode conductive components. This avoids oxidation and corrosion of the anode-side conductive components and their fasteners at high potentials. The anode conductive material can be titanium, reducing the reactor's manufacturing cost. In some reports, traditional electrochemical reactors operating at high current densities for extended periods have experienced oxidation and corrosion of the anode conductive device and screws, leading to reactor damage. The anode-side conductive components and fasteners are mostly made of titanium because if the anode material uses a BDD electrode, the material connected to the BDD electrode is titanium. Titanium's resistivity is much lower than that of the BDD electrode. If the cathode and anode conductive devices are close together and the current density is high, the current will preferentially choose the lower resistance path. Therefore, after the current enters the anode of the electrochemical reactor, it quickly passes through the titanium conductive device and then is conducted to the higher-resistance BDD coating. When the titanium conductive device operates at a high potential, oxidation and corrosion may occur, causing voltage increases and structural damage to the electrochemical reactor. To address this issue, other cases have proposed using niobium, tantalum, or titanium plated with platinum, but this significantly increases the manufacturing cost of the electrochemical reactor. Other solutions involve sealing the conductive components to prevent organic wastewater from contacting the conductive electrode. However, achieving this water-sealing is complex and undoubtedly increases the design and manufacturing cost of the electrochemical reactor.

[0068] To demonstrate the effectiveness of this embodiment, the following application example 1 is given:

[0069] The flow-through electrochemical reactor provided in this embodiment is applied to the degradation of a certain organic wastewater.

[0070] Compared with the traditional titanium sheet anode conductive scheme, the flow-through electrochemical reactor provided in this embodiment has a 1V lower actual operating voltage. When treating 1 ton of organic wastewater using the same current density, the heat generated by the organic wastewater decreases by 3-6℃ after 3 hours of operation.

[0071] To demonstrate the effectiveness of this embodiment, the following application example 2 is given:

[0072] The above-mentioned flow-through electrochemical reactor was applied to the treatment of leachate from a certain type of kitchen waste.

[0073] The leachate from a municipal food waste treatment plant is characterized by complex composition, high COD concentration, and poor biodegradability. In this example, the anode plate 515 uses a BDD electrode. In this example: COD is 800 mg / L ~ 1500 mg / L, Cl... - With a concentration of 8000 mg / L, 18 flow-through electrochemical reactors were used, with a BDD electrode area of ​​7.6 m², a current density of 75 mA / cm², and 12 hours of operation per day, processing 20 tons of concentrate daily, achieving stable operation for one year. Field results showed that the influent COD was 800 mg / L–1500 mg / L, the effluent COD was below 300 mg / L, the removal rate reached 80%, and the power consumption per ton of water treated was 28.8 kWh. This example demonstrates that the reactor of this invention has comprehensive advantages of low cost, high efficiency, and stability in treating high-concentration, recalcitrant organic wastewater, and possesses significant industrial application value.

[0074] Example 2

[0075] The electrode reaction unit 500 can be expanded according to the actual application scenario, such as... Figure 5 As shown, the reaction chamber 1 extends along the water flow direction. Two electrode reaction units 500 are installed as a group within the reaction chamber 1. The anode flat conductive bolt 514 in each electrode reaction unit 500 is fixed to the corresponding fixing hole in the reaction chamber 1, and the cathode flat conductive bolt 524 is fixed to the corresponding fixing hole in the outer cover plate 3. Each electrode reaction unit 500 does not require mechanical connection or sealing with each other. The two electrode reaction units 500 can be electrically connected in parallel or series via copper busbars 7. The reaction chamber 1 of the electrochemical reactor is customized and expanded according to the number of electrode reaction units 500.

[0076] The difference between this embodiment and embodiment 1 is that there are two electrode reaction units 500 in this embodiment, while the rest of the structural settings and application principles are the same as in embodiment 1.

[0077] Example 3

[0078] like Figure 6As shown, the difference between this embodiment and embodiment 2 is that in this embodiment, the four electrode reaction units 500 are installed as a group in the reaction chamber 1, while the rest of the structural settings, connections and application principles are the same as in embodiment 2.

Claims

1. A flow-through electrochemical reactor, characterized in that, include: A reaction chamber, wherein the reaction chamber is provided with a medium inlet and a medium outlet; The outer cover plate is sealed to the opening of the reaction chamber; At least one set of electrode reaction units is disposed inside the reaction chamber; The electrode reaction unit includes an anode grid plate and a cathode grid plate arranged in parallel and opposite directions, as well as an anode plate array and a cathode plate array disposed between the anode grid plate and the cathode grid plate; the anode plates and cathode plates in the anode plate array and the cathode plate array are arranged alternately and parallel at equal intervals.

2. The flow-through electrochemical reactor according to claim 1, characterized in that: The reaction chamber is made of fiber-reinforced polypropylene and is processed from sheet material by ultrasonic welding. The outside of the reaction chamber is equipped with reinforcing ribs, and the inside of the reaction chamber is equipped with a flow guide plate at the medium inlet end.

3. The flow-through electrochemical reactor according to claim 1, characterized in that: The electrode reaction unit further includes: An anode conductive strip is disposed on the anode grid plate and electrically connected to each anode plate in the anode plate array; A cathode conductive strip is disposed on the cathode grid plate and electrically connected to each cathode plate in the cathode plate array; The anode busbar is located on the side of the anode grid plate away from the cathode grid plate and is electrically connected to the surface of the anode conductive strip. The cathode busbar is located on the side of the cathode grid plate away from the anode grid plate and is electrically connected to the surface of the cathode conductive strip. The anode terminal connects to the anode busbar and extends to the outside of the reaction chamber; The cathode terminal connects to the cathode busbar and extends to the outside of the reaction chamber.

4. A flow-through electrochemical reactor according to claim 3, characterized in that: Both the anode grid plate and the cathode grid plate are provided with rectangular grooves for installing conductive strips and grooved grids for installing electrode plate arrays; the anode grid plate and the cathode grid plate are fixedly connected by connectors to form a frame structure.

5. A flow-through electrochemical reactor according to claim 3, characterized in that: The anode and cathode conductive strips are provided with grooves for inserting electrode plates, and the sides of the anode and cathode conductive strips are provided with threaded holes for tightening the electrode plates with set screws.

6. A flow-through electrochemical reactor according to claim 3, characterized in that: The anode busbar and cathode busbar are respectively connected to the corresponding grid plate by fasteners, and the surface of the busbar is in close contact with the surface of the conductive strip to form a surface contact.

7. A flow-through electrochemical reactor according to claim 3, characterized in that: The anode and cathode terminals are flat conductive bolts, and a conical sealing gasket is provided between the flat conductive bolt and the outer cover plate or reaction chamber; one end of the flat conductive bolt is welded to the busbar, and the other end is connected to a copper busbar at the flat position.

8. A flow-through electrochemical reactor according to claim 1, characterized in that: The anode plate is made of boron-doped diamond electrode or shape-stabilized anode electrode, and the cathode plate is made of titanium metal or boron-doped diamond electrode.

9. A flow-through electrochemical reactor according to claim 8, characterized in that: When the cathode plate is made of titanium, the surface roughness Ra of the cathode plate is 0.4μm~0.8μm; when the cathode plate is made of boron-doped diamond electrode, the cathode plate is operated as the anode by switching the current direction, so as to remove the scale layer on the electrode surface.

10. A flow-through electrochemical reactor according to claim 1, characterized in that: The reaction chamber is provided with two or more sets of electrode reaction units along the water flow direction, and the sets of electrode reaction units are connected in parallel or in series by copper busbars.

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