An anaerobic ammonia oxidation reaction device for full-scale treatment of landfill leachate

Abstract

The application provides an anaerobic ammonia oxidation reaction device for full-quantity treatment of landfill leachate, and relates to the technical field of wastewater treatment. The application comprises a reaction tank, a mud bed reaction zone is arranged in the reaction tank, a plurality of heat insulation plates are arranged at intervals from the water inlet end to the water outlet end of the mud bed reaction zone, and the mud bed reaction zone is divided into a plurality of filler layers by the heat insulation plates, a plurality of liquid inlet holes are formed in the heat insulation plates; the upper end of a heat conduction shaft at least partially extends into liquid outside the water outlet end of the mud bed reaction zone, and the lower end of the heat conduction shaft is located in the filler layer close to the water inlet end of the mud bed reaction zone; a plurality of heat conduction plates fixed on the heat conduction shaft are arranged in each filler layer, the heat conduction plates are arranged at intervals along the circumference of the heat conduction shaft and extend outward along the radial direction; and the heat conduction coefficients of the corresponding heat conduction shaft sections and heat conduction plates of each filler layer decrease layer by layer. Compared with the prior art, the application has the advantages of fully utilizing the heat generated by the anaerobic ammonia oxidation reaction, improving the temperature distribution of the reaction zone and reducing the overall temperature regulation energy consumption.

Description

Technical Field

[0001] This application relates to the field of wastewater treatment technology, and in particular to an anaerobic ammonia oxidation reactor for the full-volume treatment of landfill leachate. Background Technology

[0002] The full-scale treatment of landfill leachate involves anaerobic ammonia oxidation (AMO). AMO is a novel biological nitrogen removal technology with advantages such as low oxygen demand, no need for external organic carbon sources, and low sludge production, making it highly valuable for landfill leachate nitrogen removal. However, anaerobic ammonia oxidizing bacteria are sensitive to environmental temperature; their biological activity and nitrogen removal performance are significantly affected by temperature. When the temperature deviates from the optimal range, the anaerobic ammonia oxidation reaction rate tends to decrease, thus affecting the treatment effect. Therefore, related technologies typically require maintaining the temperature of the liquid throughout the reaction tank at the optimal reaction temperature.

[0003] However, long-term research on the operation of the reaction tanks revealed that maintaining the liquid in the large-volume tanks at a suitable reaction temperature requires continuous temperature regulation, resulting in significant energy consumption. Furthermore, temperature differences exist along the liquid flow direction within the anaerobic ammonia oxidation reaction zone. Because heat is released during the anaerobic ammonia oxidation reaction, the liquid temperature at the front end of the reaction zone is higher than at the rear end, leading to uneven temperature distribution within the reaction zone and consequently affecting the stable progress of the anaerobic ammonia oxidation reaction.

[0004] Therefore, how to reduce the energy consumption for temperature regulation during the reaction process and improve the temperature distribution within the reaction zone are problems that need to be solved in anaerobic ammonia oxidation reactors at this stage. Summary of the Invention

[0005] The purpose of this application is to provide an anaerobic ammonia oxidation reactor for the full-scale treatment of landfill leachate, so as to solve the above-mentioned technical problems existing in the prior art.

[0006] This application provides an anaerobic ammonia oxidation reactor for the full-volume treatment of landfill leachate, including a reaction tank, wherein the reaction tank is provided with a sludge bed reaction zone, and further comprising: The heat insulation plate is provided with multiple heat insulation plates at intervals from the water inlet end to the water outlet end of the mud bed reaction zone, and the mud bed reaction zone is divided into multiple packing layers. The heat insulation plate is provided with a number of liquid inlet holes. A heat-conducting shaft is inserted through each of the packing layers. The upper end of the heat-conducting shaft extends at least partially into the liquid outside the water outlet of the mud bed reaction zone, and the lower end of the heat-conducting shaft is located in the packing layer near the water inlet of the mud bed reaction zone. Each of the filler layers is provided with a plurality of heat-conducting plates fixed on the heat-conducting shaft, and each of the heat-conducting plates is arranged circumferentially along the heat-conducting shaft and extends radially outward; The thermal conductivity of the shaft segment located within each of the packing layers is the same as that of the corresponding thermal conductive plate. Furthermore, along the direction from the inlet to the outlet of the mud bed reaction zone, the thermal conductivity of the corresponding thermal conductive shaft segment and thermal conductive plate of each packing layer decreases layer by layer.

[0007] Preferably, the heat-conducting shaft is rotatably disposed inside the reaction vessel; And / or, the heat-conducting shaft is located in the middle of the mud bed reaction zone.

[0008] Preferably, along the direction from the water inlet to the water outlet of the mud bed reaction zone, the distribution density of the heat-conducting plates in each of the packing layers decreases layer by layer in the circumferential direction of the heat-conducting axis; And / or, the surface of the heat-conducting plate is provided with a bio-compatible coating; And / or, each of the heat-conducting plates is arranged at an angle; And / or, the heat-conducting plate is a thin plate structure.

[0009] Preferably, the heat-conducting plate in each of the filler layers is divided into an upper plate and a lower plate, and the inclination direction of the upper plate is opposite to that of the lower plate.

[0010] Preferably, a heat-conducting ring is provided between the upper plate and the lower plate, and the heat-conducting ring is connected between the upper plate and the lower plate; And / or, the end of the upper plate is slidably engaged with the corresponding upper heat insulation plate; And / or, the end of the lower plate is slidably engaged with the corresponding lower heat insulation plate.

[0011] Preferably, in the thermally conductive shaft segments corresponding to two adjacent filler layers, the shaft segment with higher thermal conductivity is provided with an extension segment, and the shaft segment with lower thermal conductivity is provided with an insertion groove, wherein the extension segment is inserted into the insertion groove.

[0012] Preferably, a mounting base is provided below the heat insulation plate located at the water inlet end of the mud bed reaction zone, and the lower end of the heat-conducting shaft is rotatably mounted on the mounting base. The mounting base is provided with a heat exhaust port, which can communicate with the liquid outside the water inlet end of the mud bed reaction zone. A sealing member is provided at the heat exhaust port. The sealing member opens the heat exhaust port when the temperature of the heat-conducting shaft exceeds a threshold value, and closes the heat exhaust port when the temperature is below the threshold value.

[0013] Preferably, the sealing element includes a heat-deformable metal sheet connected to the heat-conducting shaft. The heat-deformable metal sheet deforms to open the heat exhaust port when the temperature of the heat-conducting shaft exceeds a threshold, and restores its deformation to close the heat exhaust port when the temperature of the heat-conducting shaft is below the threshold.

[0014] Preferably, the reaction vessel is provided with a driving component, which is used to drive the heat-conducting shaft to rotate.

[0015] Preferably, the driving component includes a drive motor, which is disposed above the reaction vessel. The output shaft of the drive motor passes through the reaction vessel and is connected to the upper end of the heat-conducting shaft via a flange. The flange is made of heat-insulating material.

[0016] This application has the following advantages and beneficial effects: This application embodiment divides the mud bed reaction zone into multiple packing layers by setting multiple heat insulation plates within the zone. Each packing layer contains a heat-conducting plate, and a heat-conducting shaft is used to transfer the heat generated by the anaerobic ammonia oxidation reaction within each packing layer, allowing for a redistribution of the heat generated during the reaction process within the mud bed reaction zone. Since the degree of reaction is not entirely uniform across different areas of the mud bed reaction zone along the liquid flow direction, the anaerobic ammonia oxidation reaction is more intense in the packing layer near the inlet, generating relatively more heat. As the liquid flow gradually extends towards the outlet, the reactant concentration gradually decreases, the reaction intensity weakens accordingly, and the heat generated also decreases. Therefore, this application does not use the same thermal conductivity for uniform heat dissipation across all packing layers. Instead, the thermal conductivity of the corresponding heat-conducting shaft section and heat-conducting plate decreases layer by layer along the direction from the inlet to the outlet of the mud bed reaction zone.

[0017] The packing layer near the water inlet generates more heat. By using heat-conducting shaft sections and plates with high thermal conductivity, the heat generated in this area can be quickly transferred to adjacent packing layers, preventing a large amount of heat from concentrating at the bottom of the reaction zone. As the liquid flows to subsequent packing layers upstream, the heat release from the reaction gradually decreases. By progressively reducing the thermal conductivity of the heat-conducting shaft sections and plates, the rate of further heat transfer can be slowed down, allowing some of the heat already transferred to subsequent packing layers to be retained, thus matching the heat release intensity at different locations. Therefore, a relatively reasonable temperature distribution can be formed by utilizing the heat generated at different locations in the reaction zone, avoiding heat concentration at the bottom and insufficient heat at the top, improving temperature differences along the liquid flow direction, and helping to maintain a relatively stable reaction environment for anaerobic ammonia-oxidizing bacteria in each packing layer.

[0018] Furthermore, the upper end of the heat-conducting shaft extends at least partially into the liquid outside the outlet of the mud bed reaction zone, allowing excess heat generated during the reaction to be transferred to the liquid outside the reaction zone via the heat-conducting shaft, thus providing a necessary heat release path for the reaction zone. Simultaneously, the lower end of the heat-conducting shaft is located within the packing layer near the inlet of the mud bed reaction zone. Combined with the heat insulation plates installed between the packing layers, this reduces the direct and widespread diffusion of reaction heat into the liquid throughout the entire reaction tank. Therefore, it is no longer necessary to heat and maintain a large volume of liquid within the reaction tank at the optimal reaction temperature for anaerobic ammonia oxidation bacteria. Instead, the heat generated by the anaerobic ammonia oxidation reaction itself is used to maintain the temperature of the mud bed reaction zone, allowing the liquid temperature in the non-reaction areas of the reaction tank to be relatively lower. This reduces the volume of liquid requiring temperature regulation and the corresponding energy demand, thereby lowering the operating energy consumption of the reaction apparatus.

[0019] Through the above structure, on the one hand, the heat generated by the anaerobic ammonia oxidation reaction itself is utilized, reducing the need to heat the entire liquid in the reaction tank; on the other hand, by progressively reducing the thermal conductivity along the liquid flow direction, the heat transfer capacity is matched with the heat release intensity of each packing layer, ensuring sufficient heat in the reaction zone while reducing excessive heat loss. Therefore, this application can maintain a suitable reaction environment for anaerobic ammonia oxidizing bacteria while eliminating the need to maintain an excessively high temperature in the entire liquid inside the reaction tank, thus balancing reaction stability and energy-saving operation. Attached Figure Description

[0020] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 This is a schematic diagram of the overall structure of the reaction vessel provided in the embodiments of this application.

[0022] Figure 2 yes Figure 1 Enlarged view of section A.

[0023] Figure 3 This is a schematic diagram of the structure of the heat insulation plate, heat-conducting shaft, and heat-conducting plate provided in the embodiments of this application.

[0024] Figure 4 This is a schematic diagram of the structure of the heat-conducting shaft and heat-conducting plate provided in the embodiments of this application.

[0025] Figure 5 This is a schematic diagram of the structure of the shaft segment, heat-conducting plate, and heat-conducting ring provided in the embodiments of this application.

[0026] Figure 6 This is a cross-sectional view of the heat-conducting shaft provided in an embodiment of this application.

[0027] Figure 7 This is a schematic diagram of the sealing component provided in the embodiment of this application in the state of sealing the heat dissipation port.

[0028] Figure 8 This is a schematic diagram of the closure component provided in the embodiment of this application in the state of having its heat dissipation port open.

[0029] The diagram is marked as follows: 100. Reaction vessel; 200. Mud bed reaction zone; 201. Water inlet; 202. Water outlet; 203. Packing layer; 210. Heat insulation plate; 211. Liquid inlet hole; 300. Heat-conducting shaft; 310. Shaft section; 311. Extension section; 312. Insertion groove; 400. Heat-conducting plate; 410. Upper plate; 420. Lower plate; 430. Heat-conducting ring; 500. Mounting base; 510. Heat outlet; 600. Enclosure; 610. Heat-deformed metal sheet; 611. Deformation groove; 612. Rubber pad; 613. Contact head; 614. Insulation layer; 700. Drive component; 710. Drive motor; 710. Flange; D. Direction of heat conduction; E. Direction of deformation; F. Direction of heat dissipation; G. Direction of liquid inlet. Detailed Implementation

[0030] To make the objectives, technical solutions, and advantages of this application clearer, the technical solutions of this application will be described in detail below. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. Based on the embodiments in this application, all other implementation methods obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0031] During long-term operational studies of the anaerobic ammonia oxidation reactor, it was found that the temperature of the liquid inside the reactor does not entirely depend on external temperature regulation; the heat generated during the anaerobic ammonia oxidation reaction itself also affects the temperature distribution in the reaction zone.

[0032] Further temperature monitoring at different locations in the reaction zone revealed that the degree of reaction varied along the direction of liquid flow, resulting in different amounts of heat generated and uneven temperature distribution within the reaction zone.

[0033] Based on the above findings, it is necessary to rationally regulate the heat transfer within the reaction zone to fully utilize the heat generated by the anaerobic ammonia oxidation reaction, thereby improving the temperature distribution within the reaction zone and reducing the need for temperature regulation of the liquid throughout the entire reaction vessel.

[0034] In view of this, the following will be combined with Figures 1 to 8 The anaerobic ammonia oxidation reactor for full-scale treatment of landfill leachate provided in this application will be described in detail through specific embodiments and application scenarios.

[0035] First, it should be noted that the reaction tank 100 of the anaerobic ammonia oxidation reactor typically includes an inlet, an outlet, and a gas outlet at the top. A three-phase separator for gas-liquid-solid three-phase separation can be installed at the top of the reaction tank 100 to separate the gas generated during the reaction, the treated liquid, and the sludge flowing with the liquid. Specifically, after the landfill leachate enters the reaction tank 100 through the inlet, it flows into the sludge bed reaction zone 200 inside the reaction tank 100 and comes into contact with the anaerobic ammonia oxidizing bacteria in the sludge bed reaction zone 200 to carry out a biological denitrification reaction. The gas generated by the reaction, as well as the sludge and liquid moving upward with the liquid, continue to flow to the top of the reaction tank 100 and are separated by the three-phase separator.

[0036] The separated gas can be discharged through the gas outlet, the treated liquid can be discharged through the effluent outlet, and some of the sludge can fall back into the sludge bed reaction zone 200 under gravity, thereby reducing the large-scale loss of anaerobic ammonia oxidizing bacteria with the effluent. The specific structure of the three-phase separator can adopt the structural form commonly used in existing anaerobic ammonia oxidation reactors, such as using separation components with gas-liquid separation space and solid-liquid separation space. This application does not limit its specific structure.

[0037] Before entering the reaction tank 100, the landfill leachate undergoes pretreatment, which may include bar filtration, sedimentation, solid-liquid separation, and water quality conditioning. This pretreatment reduces the amount of large particulate impurities and suspended solids entering the reaction tank 100, lowering the risk of blockage in the subsequent sludge bed reaction zone 200. Furthermore, the water quality parameters of the influent are adjusted according to the requirements of the anaerobic ammonia oxidation reaction. For example, the ammonia nitrogen, nitrite nitrogen, and other substances affecting the anaerobic ammonia oxidation reaction can be adjusted based on the actual water quality conditions to ensure that the landfill leachate entering the reaction tank 100 meets the corresponding reaction conditions.

[0038] The above-mentioned pretreatment process is a routine treatment measure before landfill leachate enters the bioreactor. The focus of this application is on the heat transfer and temperature control structure inside the reaction tank 100. Therefore, no further limitations are made on the specific pretreatment process.

[0039] The reaction apparatus can also be equipped with pH detection components, temperature detection components, and a pump for conveying influent. Pressure valves, check valves, and other pipeline control components can also be installed on the influent pipeline as needed. Specifically, the pH detection component can be used to detect the pH value of the liquid inside the reaction tank 100 or in the influent pipeline; the temperature detection component can be used to detect the temperature of the liquid inside the reaction tank 100 or in the sludge bed reaction zone 200; and the pump is used to continuously convey pretreated landfill leachate into the reaction tank 100. The pressure valve can be used to regulate pipeline pressure, and the check valve can prevent backflow of liquid from the reaction tank 100 into the influent pipeline. The above structure is mainly used for the routine conveying, detection, and operational control of landfill leachate, and is a relatively conventional auxiliary structure in anaerobic ammonia oxidation reactors. It can be selected and installed according to actual operational needs, and this application does not impose specific limitations on it.

[0040] In this embodiment, the reaction tank 100 adopts a vertical arrangement, with the inlet located at the bottom and the outlet at the top. The landfill leachate flows upwards and passes through the sludge bed reaction zone 200 before being discharged. This arrangement allows the leachate to flow upwards using the inlet pressure provided by the pump and the liquid level difference within the reaction tank 100, allowing it to pass through different reaction zones within the sludge bed reaction zone 200 and fully contact the anaerobic ammonia-oxidizing bacteria during its flow. Accordingly, the end of the sludge bed reaction zone 200 closest to the inlet is defined as the inlet end 201, and the end closest to the outlet is defined as the outlet end 202. Subsequent structures such as the heat insulation plate 210, the packing layer 203, and the heat-conducting shaft 300 are arranged and described with reference to this liquid flow direction.

[0041] It should be understood that the term "inlet end 201" in this embodiment is not limited to the mud bed reaction zone 200 being directly connected to the inlet of the reaction tank 100, but rather refers to the side where the liquid enters the mud bed reaction zone 200 and begins to react with the anaerobic ammonia oxidizing bacteria; similarly, "outlet end 202" refers to the side where the liquid flows out to subsequent areas after completing the main reaction process within the mud bed reaction zone 200. Therefore, even if a water distribution space, buffer space, or other conventional water flow distribution structure is provided between the inlet and the mud bed reaction zone 200, the side closer to where the liquid first enters the mud bed reaction zone 200 can still serve as the inlet end 201 of the mud bed reaction zone 200.

[0042] Furthermore, the sludge bed reaction zone 200 can be positioned in the lower middle part of the reaction tank 100 according to the actual processing capacity, ensuring sufficient residence time for the influent after entering the sludge bed reaction zone 200, and allowing it to continue flowing towards the three-phase separation zone at the top of the reaction tank 100 after passing through the sludge bed reaction zone 200. The height, cross-sectional area, and effective volume of the sludge bed reaction zone 200 can be adjusted according to the processing capacity of the landfill leachate, the influent flow rate, and the preset hydraulic residence time. For example, for treatment units of different scales, the effective reaction volume can be increased by increasing the height or cross-sectional area of ​​the sludge bed reaction zone 200 without changing the basic working principle of the subsequent heat transfer structure of this application.

[0043] It should be understood that the specific shape and arrangement of the reaction tank 100 are not limited to a vertical structure. In some embodiments, the reaction tank 100 can also be arranged horizontally or inclined, as long as the mud bed reaction zone 200 has a clearly defined water inlet 201 and water outlet 202, and the liquid can pass through different packing layers 203 sequentially according to a preset flow path.

[0044] For example, when the reaction vessel 100 is arranged laterally, the side near the inlet can be defined as the inlet end 201 of the mud bed reaction zone 200, and the side near the outlet can be defined as the outlet end 202. The heat insulation plates 210 are still spaced along the liquid flow direction, and the heat-conducting shaft 300 still extends from the inlet end 201 to the outlet end 202. Therefore, changes in the specific installation direction of the reaction vessel 100 will not change the basic principle of this application of gradient transfer and utilization of reaction heat from different reaction zones.

[0045] In addition, the reaction vessel 100 may be provided with an insulation layer 614, which can cover the outer wall of the reaction vessel 100 to reduce heat exchange between the liquid inside the reaction vessel 100 and the external environment.

[0046] For the mud bed reaction zone 200 within the reaction tank 100, the mud bed reaction zone 200 serves as the primary site for the anaerobic ammonia oxidation reaction. In this embodiment, the mud bed reaction zone 200, without the heat insulation plate 210, can be considered as an integral mud bed structure continuously distributed along the liquid flow direction. That is, the anaerobic ammonia oxidizing bacteria are entirely distributed within the mud bed reaction zone 200. After entering the mud bed reaction zone 200, the liquid sequentially passes through different locations within the mud bed and undergoes the anaerobic ammonia oxidation reaction.

[0047] The present application does not pre-set the mud bed reaction zone 200 as multiple independent reaction zones, but instead sets multiple heat insulation plates 210 inside the continuous mud bed reaction zone 200 along the liquid flow direction. The heat insulation plates 210 separate the originally continuous mud bed reaction zone 200, thereby forming multiple interconnected but heat transfer restricted filler layers 203.

[0048] Specifically, multiple heat insulation plates 210 are spaced apart from the inlet end 201 to the outlet end 202 of the sludge bed reaction zone 200, forming a packing layer 203 between adjacent heat insulation plates 210, thereby dividing the sludge bed reaction zone 200 into multiple packing layers 203 along the liquid flow direction. The heat insulation plates 210 are mainly used to limit the direct heat exchange between adjacent packing layers 203, while not completely blocking the flow of landfill leachate along the direction from the inlet end 201 to the outlet end 202. Through this arrangement, while maintaining the original overall reaction path of the sludge bed reaction zone 200, it can be divided into multiple regions with certain independent temperature characteristics, so that the subsequent setting of structures with different thermal conductivity for different packing layers 203 has a clear target.

[0049] The insulation panel 210 can be made of a material with low thermal conductivity that can withstand the environment of landfill leachate for a long time, such as polytetrafluoroethylene, polypropylene, polyurethane insulation material, or other corrosion-resistant insulation materials. The specific material of the insulation panel 210 can be selected according to the temperature inside the reaction tank 100, the corrosiveness of the landfill leachate, and the mechanical strength requirements, and is not limited to the above-mentioned materials.

[0050] As an example, the thickness of the insulation plate 210 can be set to 10-30mm, which reduces direct heat transfer between adjacent packing layers 203 while ensuring the self-supporting strength of the insulation plate 210. For larger reaction vessels 100, the thickness of the insulation plate 210 can be appropriately increased, or an insulation plate 210 with a sandwich structure can be used to further reduce the rate at which heat is transferred through the insulation plate 210 body.

[0051] The packing layer 203 is used to contain anaerobic ammonia oxidizing bacteria. The anaerobic ammonia oxidizing bacteria can be directly placed in the packing layer 203 in the form of granular sludge, or the anaerobic ammonia oxidizing bacteria can be pre-attached to a carrier and then the carrier with attached anaerobic ammonia oxidizing bacteria is filled into the corresponding packing layer 203.

[0052] The carrier can be made of polyurethane sponge, porous polyethylene carrier, polypropylene filler, ceramsite, or other porous materials with a large specific surface area that can be immersed in landfill leachate for a long time. When using a carrier to immobilize anaerobic ammonia-oxidizing bacteria, the internal pores of the carrier can be used to provide attachment space for the bacteria, reducing the direct discharge of bacteria with the liquid flow, and at the same time enabling the bacteria to maintain a relatively stable distribution within the filler layer 203.

[0053] In practical applications, anaerobic ammonia-oxidizing bacteria can first be enriched and cultured in an independent culture system to form granular sludge or attached biofilm. The cultured granular sludge or carrier can then be transferred and filled into the sludge bed reaction zone 200. Alternatively, after the reaction tank 100 is installed, anaerobic ammonia-oxidizing granular sludge can be added to each packing layer 203, and after a period of acclimatization and biofilm formation, a stable bacterial community will form.

[0054] For embodiments using carrier filling, the effective filling volume of the packing layer 203 can be adjusted according to the liquid flow rate, bacterial load, and reaction load. For example, it can be controlled at 40%-70% of the effective volume of the corresponding packing layer 203, with the remaining space used to provide space for landfill leachate flow and bacterial growth. The above filling ratio is only one implementation example, and can be adjusted according to the load of anaerobic ammonia oxidizing bacteria and the type of carrier.

[0055] As the landfill leachate flows continuously from the inlet 201 to the outlet 202 of the mud bed reaction zone 200, the concentration of reactants participating in the anaerobic ammonia oxidation reaction in the liquid entering the inlet 201 is relatively high. Therefore, the packing layer 203 near the inlet 201 usually has a high reaction load, and the reaction degree of anaerobic ammonia oxidizing bacteria is relatively concentrated. As the liquid continues to flow towards the outlet 202, some reactants are consumed in the preceding packing layer 203, and the concentration of reactants in the subsequent packing layer 203 gradually decreases, and the intensity of the anaerobic ammonia oxidation reaction at the corresponding position also decreases.

[0056] Therefore, under actual operating conditions, the effective reaction volume and bacterial activity of anaerobic ammonia oxidizing bacteria in the sludge bed reaction zone 200 vary along the direction from the inlet end 201 to the outlet end 202, and the bacterial quantity and filling method can be adjusted according to the actual operating conditions of each packing layer 203. For example, the packing layer 203 near the inlet end 201 can be configured with a relatively large number of anaerobic ammonia oxidizing bacteria or a higher carrier filling volume, while the packing layer 203 near the outlet end 202 can appropriately reduce the bacterial quantity or carrier filling volume, thereby matching the bacterial quantity distribution with the reaction load at each location.

[0057] The heat insulation plate 210 has several liquid inlet holes 211, which allow leachate to sequentially enter adjacent packing layers 203, thus preventing the heat insulation plate 210 from completely isolating the packing layers 203. In other words, the heat insulation plate 210 primarily restricts direct heat exchange between adjacent packing layers 203, while the leachate can still flow from one packing layer 203 to the next through the inlet holes 211, creating a continuous reaction path in the liquid flow direction among the multiple packing layers 203. This maintains the original continuous processing capacity of the sludge bed reaction zone 200 while reducing disordered heat diffusion between different areas using the heat insulation plate 210.

[0058] Multiple liquid inlet holes 211 can be distributed around the heat insulation plate 210 to allow the liquid to pass through the heat insulation plate 210 more evenly, avoiding the liquid from passing through a single position and forming obvious flow deviation.

[0059] As one implementation method, the inlet hole 211 can be a circular hole with a diameter of 5-20 mm, which can be adjusted according to the suspended solids content of the landfill leachate, the carrier size of the anaerobic ammonia oxidizing bacteria, and the liquid flow rate. When the packing layer 203 uses granular sludge with a larger particle size or blocky, porous carriers, the diameter of the inlet hole 211 can be appropriately increased; when using packing with a smaller particle size, the diameter of the inlet hole 211 can be appropriately decreased to balance the liquid flow capacity and the bacterial cell retention effect.

[0060] The number of liquid inlet holes 211 can also be adjusted according to the area of ​​the heat insulation plate 210. For example, multiple liquid inlet holes 211 can be set in a uniform distribution manner to keep the liquid flow on both sides of the heat insulation plate 210 relatively balanced.

[0061] In this embodiment, a heat-conducting shaft 300 is inserted into each packing layer 203, extending along the direction from the inlet end 201 to the outlet end 202 of the mud bed reaction zone 200. The upper end of the heat-conducting shaft 300 extends at least partially into the liquid outside the outlet end 202 of the mud bed reaction zone 200, while the lower end of the heat-conducting shaft 300 is located within the packing layer 203 near the inlet end 201 of the mud bed reaction zone 200. The length of the heat-conducting shaft 300 extending into the liquid outside the outlet end 202 is not fixed and can be adjusted according to the heat generation of the mud bed reaction zone 200, the volume of the liquid in the reaction tank 100, the allowable temperature range, and actual heat dissipation requirements.

[0062] In other words, it is not necessary to extend most or even all of the heat-conducting shaft 300 into the liquid outside the outlet 202. Instead, it is only necessary to ensure that the heat-conducting shaft 300 has an effective heat dissipation section that can transfer some heat to the liquid outside. When it is necessary to reduce heat loss, the length of the heat dissipation section can be appropriately reduced. When there is a lot of reaction heat and it is necessary to increase the heat release capacity, the length of the section extending into the liquid can be appropriately increased, thereby adjusting the amount of reaction heat transferred to the liquid outside.

[0063] Through the above structure, the heat-conducting shaft 300 can pass through multiple packing layers 203 sequentially, allowing the reaction heat generated in different packing layers 203 to be collected by the heat-conducting plate 400 and transferred along the direction from the inlet end 201 to the outlet end 202 of the mud bed reaction zone 200. Since only a portion of the upper part of the heat-conducting shaft 300 extends into the liquid outside the outlet end 202, the heat-conducting shaft 300 mainly undertakes the heat transfer function inside the mud bed reaction zone 200, while the portion extending into the outer liquid mainly serves as a release path for some excess heat. This not only allows the reaction heat to be transferred and utilized among multiple packing layers 203, but also avoids the heat-conducting shaft 300 forming an excessively large heat dissipation channel, preventing the heat generated by the reaction from dissipating too quickly to the outside of the reaction zone.

[0064] Specifically, the upper end of the heat-conducting shaft 300 can be selected with an appropriate length to extend into the liquid according to different reaction loads and operating conditions, so that the reaction heat is kept in a reasonable balance between "internal transfer and utilization" and "appropriate external release", rather than all the reaction heat is discharged, which is more in line with the design purpose of this application to utilize the heat generated by the reaction itself and reduce the overall temperature regulation energy consumption.

[0065] For example, the heat-conducting shaft 300 can be made of a metallic thermally conductive material, such as copper, aluminum alloy, brass, stainless steel, or other materials with good thermal conductivity and corrosion resistance. Considering that the heat-conducting shaft 300 is exposed to landfill leachate environment for extended periods, its surface can be treated with anti-corrosion measures according to the actual water quality conditions, such as by applying a corrosion-resistant metal layer, a polymer protective layer, or other anti-corrosion coatings. Alternatively, while ensuring thermal conductivity, the heat-conducting shaft 300 can be directly machined from a corrosion-resistant alloy material, thereby reducing the degradation of structural performance due to corrosion during long-term operation.

[0066] Each packing layer 203 is equipped with multiple heat-conducting plates 400 fixed to a heat-conducting shaft 300. The heat-conducting plates 400 are arranged circumferentially along the heat-conducting shaft 300 and extend radially outwards. The heat-conducting plates 400 extend into the packing area where the anaerobic ammonia-oxidizing bacteria reside, allowing the reaction heat generated in the packing layer 203 away from the heat-conducting shaft 300 to be transferred to the heat-conducting shaft 300 through the heat-conducting plates 400, thus expanding the actual heat exchange area covered by the heat-conducting shaft 300. Figure 5 As shown, the heat conduction direction D of the heat conduction plate 400 is illustrated.

[0067] Compared to setting only one heat-conducting shaft 300, multiple radially extending heat-conducting plates 400 can shorten the distance between different positions within the filler layer 203 and the heat-conducting structure, which is beneficial to improving the efficiency of heat transfer from the microbial reaction area to the heat-conducting shaft 300.

[0068] Multiple heat-conducting plates 400 can be arranged in multiple groups along the axial direction of the heat-conducting shaft 300. Each group of heat-conducting plates 400 can include 3-20 heat-conducting plates 400. An interval space is formed between adjacent heat-conducting plates 400 to allow liquid to pass through, thereby avoiding excessive occupation of the effective flow section of the filler layer 203 by the heat-conducting plates 400.

[0069] The number, length, and radial extension dimensions of the heat-conducting plates 400 can be adjusted according to the cross-sectional area of ​​the packing layer 203. For example, in embodiments where the diameter of the reaction vessel 100 is large, the radial length of the heat-conducting plates 400 or the number of heat-conducting plates 400 on the same circumferential cross-section can be appropriately increased to expand the heat collection range; when the size of the reaction vessel 100 is small, the size of the heat-conducting plates 400 can be appropriately reduced to avoid generating excessive resistance to liquid flow.

[0070] To ensure that the heat transfer capacity of different packing layers 203 matches the corresponding exothermic reaction intensity, the shaft segment 310 of the heat-conducting shaft 300 located within each packing layer 203 and the corresponding heat-conducting plate 400 are made of materials with the same thermal conductivity. Furthermore, the thermal conductivity of the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 corresponding to each packing layer 203 decreases layer by layer along the direction from the inlet end 201 to the outlet end 202 of the mud bed reaction zone 200. In other words, the packing layer 203 closer to the inlet end 201 of the mud bed reaction zone 203 uses the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 with higher thermal conductivity, while the closer to the outlet end 202, the lower the thermal conductivity of the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400.

[0071] The aforementioned gradient of thermal conductivity is not simply based on structural location, but rather corresponds to the degree of reaction in the mud bed reaction zone 200 along the liquid flow direction. The packing layer 203 near the inlet 201 receives a higher concentration of reactants, resulting in a more concentrated anaerobic ammonia oxidation reaction and generating more heat. Therefore, using the shaft section 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 with higher thermal conductivity allows for rapid collection and transfer of the heat generated in this area, enabling the higher heat of reaction to be transferred to the subsequent packing layer 203, thus preventing a large amount of heat from concentrating at the inlet 201 and forming localized high temperatures.

[0072] As the liquid continues to flow toward the outlet 202, the reactants are gradually consumed, the intensity of the anaerobic ammonia oxidation reaction decreases, and the heat of reaction generated is reduced accordingly. Therefore, the subsequent packing layer 203 uses the shaft section 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 with a lower thermal conductivity to gradually reduce the heat transfer rate, thereby reducing the heat of reaction from being carried away too quickly during the transfer to the outlet 202.

[0073] Therefore, the thermal conductivity of each packing layer 203 forms a gradient corresponding to the intensity of the exothermic reaction: the front-end reaction is strong and generates more heat, so heat conduction is rapid; the rear-end reaction is weak and generates less heat, so heat conduction is reduced and heat loss is minimized. Through this design, the significant heat generated by the front-end packing layer 203 can be transferred sequentially to subsequent packing layers 203 and appropriately retained, allowing for more efficient utilization of the heat generated by the anaerobic ammonia oxidation reaction itself, rather than rapid dissipation into the large volume of liquid in the reaction tank 100 after the reaction. This also provides a structural basis for subsequently utilizing the self-generated heat of the reaction to maintain the temperature of the mud bed reaction zone 200 and reducing the temperature regulation required for the entire liquid in the reaction tank 100.

[0074] It should be noted that the interior of the packing layer 203 is not a completely open liquid flow space, but rather a relatively dense reaction zone formed by granular sludge, carrier, and anaerobic ammonia-oxidizing bacteria. Although landfill leachate can flow along the packing layer 203, it mainly passes through the pore channels between the packing materials. The heat exchange capacity between the liquid and various locations within the packing is affected by factors such as flow velocity, packing density, and pore structure.

[0075] Therefore, the heat generated inside the packing layer 203, far from the main flow channels, is not easily carried away quickly by liquid flow alone. Especially in practical applications, to ensure sufficient bacterial count and reaction volume, the packing layer 203 usually has a certain thickness. The heat inside the packing layer 203 needs to travel a relatively long transfer path to reach the flowing liquid, and relying solely on liquid flow for heat exchange can easily lead to insufficient internal heat transfer. Based on this, this application provides a heat-conducting plate 400 inside the packing layer 203 and uses a heat-conducting shaft 300 to directionally transfer heat from different locations, enabling the reaction heat generated inside the packing layer 203 to actively collect and transfer along a predetermined direction, rather than relying primarily on liquid flow to carry away the heat.

[0076] In this embodiment, the sludge bed reaction zone 200 is divided into three packing layers 203 along the liquid flow direction. The three packing layers 203 are located sequentially from the inlet end 201 to the outlet end 202 of the sludge bed reaction zone 200. Adjacent packing layers 203 are separated by heat insulation plates 210, while maintaining liquid communication through liquid inlet holes 211 on the heat insulation plates 210, allowing the landfill leachate to pass through the three packing layers 203 sequentially to complete the anaerobic ammonia oxidation reaction. The three packing layers 203 can have the same or different thicknesses, which can be set according to the size of the reaction tank 100, the inlet flow rate, and the reaction load of each area. For example, if the size of the reaction tank 100 is large or if it is necessary to increase the reaction residence time, the thickness of the packing layer 203 can be appropriately increased; if it is necessary to further reduce heat exchange between different areas, more packing layers 203 can be formed by increasing the number of heat insulation plates 210.

[0077] As a specific example of material combination, when the mud bed reaction zone 200 is divided into three packing layers 203, the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 in the first packing layer 203 near the water inlet 201 can be made of copper with a thermal conductivity of approximately 398 W / (m·K); the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 in the second packing layer 203 can be made of aluminum alloy with a thermal conductivity of approximately 180 W-220 W / (m·K); and the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 in the third packing layer 203 near the water outlet 202 can be made of 304 stainless steel with a thermal conductivity of approximately 16 W / (m·K).

[0078] By combining the above materials, a gradient of thermal conductivity can be formed from the inlet 201 to the outlet 202 of the mud bed reaction zone 200. This results in the first packing layer 203 near the inlet 201 having a strong heat transfer capacity, while the third packing layer 203 near the outlet 202 has a relatively low heat transfer capacity. The specific thermal conductivity of each material is affected by factors such as material grade, composition, processing condition, and operating temperature. The values ​​mentioned above are mainly used to illustrate the relationship of thermal conductivity between the packing layers 203 and are not intended to limit specific material parameters. In practical applications, the materials of the shaft segment 310 of the heat-conducting shaft 300 and the heat-conducting plate 400 corresponding to each packing layer 203 can be appropriately replaced based on the corrosiveness of the landfill leachate, operating temperature, mechanical strength, and processing cost, as long as the relationship of decreasing thermal conductivity from the inlet 201 to the outlet 202 is maintained.

[0079] In different embodiments, copper alloys, titanium alloys, stainless steel, or other corrosion-resistant thermally conductive materials can also be used in combination, as long as the shaft segment 310 of the thermally conductive shaft 300 and the thermally conductive plate 400 corresponding to adjacent packing layers 203 can form a thermal conductivity that decreases layer by layer from the inlet end 201 to the outlet end 202. For highly corrosive landfill leachate, a corrosion-resistant protective layer can also be provided on the surface of the thermally conductive shaft 300 and the thermally conductive plate 400 to reduce the impact of corrosion while maintaining their internal thermally conductive structure.

[0080] This structure does not simply discharge heat from the bottom layer or the inlet 201 directly into the reaction vessel 100. Instead, it directionally and hierarchically transfers the heat generated by the anaerobic ammonia oxidation reaction. The packing layer 203 near the inlet 201 generates more heat, which is rapidly collected by the high thermal conductivity of the heat-conducting shaft 300 (shaft section 310) and the heat-conducting plate 400, and transferred to subsequent packing layers 203. Subsequent packing layers 203 use the lower thermal conductivity of the heat-conducting shaft 300 (shaft section 310) and the heat-conducting plate 400, gradually reducing the rate of further heat transfer. This allows some of the heat generated in the preceding stages to be retained in the subsequent packing layers 203 for a longer period. This reduces the rapid loss of reaction heat during liquid flow, ensuring that multiple packing layers 203 can utilize the heat generated by the anaerobic ammonia oxidation reaction itself.

[0081] It is particularly important to note that the temperature control approach of this application does not involve heating the entire liquid in the reaction vessel 100 to the optimal reaction temperature for anaerobic ammonia oxidizing bacteria. Instead, it utilizes the reaction heat generated by the mud bed reaction zone 200 itself to compensate for the reaction in the reaction area. By reducing the large-scale diffusion of reaction heat to the outside of the mud bed reaction zone 200 through the heat-conducting shaft 300 and the heat-conducting plate 400, the reaction heat is directionally transferred and retained within the mud bed reaction zone 200. This allows the mud bed reaction zone 200 to maintain a relatively stable reaction temperature by relying on its own generated heat.

[0082] Therefore, provided the temperature conditions required for normal anaerobic ammonia oxidation are met, the large volume of liquid outside the reaction zone in reactor 100 does not need to be maintained at the same high temperature as the reaction zone. In fact, the base temperature of the entire liquid in reactor 100 can be set far below the optimal reaction temperature, with local compensation achieved using the heat generated during the anaerobic ammonia oxidation reaction. This reduces the volume of liquid requiring active heating, thereby lowering the energy required for continuous temperature control.

[0083] In this embodiment, the heat-conducting shaft 300 is rotatably disposed within the reaction vessel 100. As a specific implementation, the heat-conducting shaft 300 is located in the center of the mud bed reaction zone 200, allowing multiple heat-conducting plates 400 fixed on the heat-conducting shaft 300 to extend radially into different directions within the packing layer 203. This expands the contact range between the heat-conducting plates 400 and the packing, and shortens the heat transfer distance between different locations within the packing layer 203 and the heat-conducting structure. Especially when the packing layer 203 is thick, placing the heat-conducting shaft 300 in the center of the packing layer 203 prevents the heat-conducting plates 400 from only covering the area near one side of the packing layer 203, allowing the heat inside the packing layer 203 to be more evenly distributed to the heat-conducting shaft 300.

[0084] The heat-conducting shaft 300 can be supported by a sealed bearing mounted on the top of the reaction vessel 100, allowing the heat-conducting shaft 300 to maintain a stable position inside the reaction vessel 100. One or more sealed bearings can be provided depending on the length and weight of the heat-conducting shaft 300. Multiple sealed bearings can be arranged at axial intervals along the heat-conducting shaft 300 to reduce radial sway during the rotation of the heat-conducting shaft 300.

[0085] The reaction vessel 100 is equipped with a drive unit 700, which is used to drive the heat-conducting shaft 300 to rotate. The drive unit 700 includes a drive motor 710, which is located above the reaction vessel 100. The output shaft of the drive motor 710 passes into the reaction vessel 100 and is connected to the upper end of the heat-conducting shaft 300 through a flange 710.

[0086] Flange 710 is made of heat-insulating material, which can reduce heat transfer from the heat-conducting shaft 300 to the drive motor 710 side. The heat-insulating material can be polytetrafluoroethylene, polyetheretherketone, or other temperature-resistant and corrosion-resistant engineering plastics, or a composite heat-insulating gasket combined with a metal flange can be used to form a heat-insulating structure.

[0087] The drive motor 710 can be electrically connected to the controller, which controls the drive motor 710 to drive the heat-conducting shaft 300 to rotate at a low speed according to preset operating parameters. Since the packing layer 203 containing anaerobic ammonia-oxidizing bacteria needs to maintain a relatively stable biological reaction environment, the heat-conducting shaft 300 does not need to rotate at high speed, but can operate at a low speed, such as 0.5-5 r / min. This allows the heat-conducting plate 400 to slowly change its circumferential position, promoting heat transfer while reducing drastic disturbance to the bacterial community and biofilm within the packing layer 203. The specific speed can be adjusted according to the structure of the packing layer 203, the bacterial count, and the liquid flow rate.

[0088] When the heat-conducting shaft 300 rotates, multiple heat-conducting plates 400 fixed on it rotate synchronously, causing the heat-conducting plates 400 to form periodic contact with the liquid and carrier at different positions within the packing layer 203. This not only allows the heat conducted by the heat-conducting plates 400 themselves to diffuse in different directions, but also changes the local flow state of the liquid near the heat-conducting plates 400 to a certain extent, reducing the temperature boundary layer formed around the heat-conducting plates 400, and allowing heat to be transferred more evenly to the packing layer 203.

[0089] The drive motor 710 can also operate intermittently based on temperature detection results. For example, when the temperature difference is large, the operating frequency of the heat-conducting shaft 300 can be increased, and the operating frequency can be reduced after the temperature of each packing layer 203 tends to stabilize, thereby further reducing drive energy consumption.

[0090] In other embodiments, the heat-conducting shaft 300 may not have a separate drive motor 710, but instead utilize the gas generated inside the reaction vessel 100 as a power source. Specifically, a connecting shaft may be provided at the upper end of the heat-conducting shaft 300, and a turbofan blade may be provided on the connecting shaft. When the gas generated inside the reaction vessel 100 flows upward, it drives the turbofan blade to rotate, thereby driving the connecting shaft and the heat-conducting shaft 300 to rotate.

[0091] This method utilizes the flow energy of the gas generated during the anaerobic ammonia oxidation reaction to drive the heat-conducting shaft 300, reducing the need for a separate drive motor 710. The number of turbofan blades can be set to 3-8, with the specific number determined based on the gas flow rate and the required rotational speed.

[0092] In this embodiment, along the direction from the inlet end 201 to the outlet end 202 of the mud bed reaction zone 200, the distribution density of the heat-conducting plates 400 in each packing layer 203 decreases layer by layer in the circumferential direction of the heat-conducting shaft 300. The packing layer 203 near the inlet end 201 has a larger number of heat-conducting plates 400 due to the more vigorous reaction, which can further increase the heat exchange area in this region, allowing the generated reaction heat to be quickly transferred to the heat-conducting shaft 300. The packing layer 203 near the outlet end 202 releases relatively less heat from the reaction; therefore, reducing the number of heat-conducting plates 400 can slow down the rate of heat transfer to the heat-conducting shaft 300, reducing subsequent heat loss.

[0093] As an example, the first filler layer 203 can be provided with 6-8 heat-conducting plates 400 in each circumferential section, the second filler layer 203 can be provided with 5-6 heat-conducting plates 400, the third filler layer 203 can be provided with 4-5 heat-conducting plates 400, and the fourth filler layer 203 can be provided with 2-4 heat-conducting plates 400, so that the distribution density and thermal conductivity of the heat-conducting plates 400 change step by step.

[0094] As one implementation, the surface of the heat-conducting plate 400 is provided with a bio-affinity coating. The bio-affinity coating may be a polydopamine coating, a hydrophilic polymer coating, or other coatings that can promote the adhesion of microorganisms, enabling some anaerobic ammonia-oxidizing bacteria to form a biofilm on the surface of the heat-conducting plate 400.

[0095] In this way, the heat-conducting plate 400 can not only transfer heat to the filler layer 203, but also serve as part of the microbial attachment area, thereby increasing the contact area between the anaerobic ammonia-oxidizing bacteria and the heat-conducting plate 400, which is beneficial for the timely transfer of reaction heat to the heat-conducting plate 400. The coating thickness can be controlled according to the adhesion performance and thermal conductivity requirements, for example, within the range of 0.05mm-0.5mm, to avoid the coating being too thick and significantly increasing the heat transfer resistance.

[0096] In one implementation, the heat-conducting plates 400 are arranged at an angle, forming a certain angle with respect to the radial direction of the heat-conducting shaft 300. When the heat-conducting shaft 300 rotates, the inclined heat-conducting plates 400 can exert a certain axial pushing effect on the surrounding liquid, causing the liquid in the packing layer 203 to form a slow circulating flow, thereby improving the uniform transfer of heat within the packing layer 203. The inclination angle of the heat-conducting plates 400 can be set to 10°-45°, and the specific angle can be determined according to the thickness of the packing layer 203 and the allowable liquid flow velocity to avoid excessive shearing action.

[0097] In one implementation, the heat-conducting plate 400 adopts a thin-plate structure to reduce the space occupied by the heat-conducting plate 400 in the filler layer 203 and allow liquid to pass through both sides of the heat-conducting plate 400. The thickness of the heat-conducting plate 400 can be set to 1mm-5mm. While meeting the strength and connection reliability requirements of the heat-conducting plate 400 itself, a thinner plate can reduce the amount of effective volume occupied by the filler layer 203. The heat-conducting plate 400 can also adopt an arc-shaped cross-section, so that the heat-conducting plate 400 forms a smoother guiding effect on the liquid when the heat-conducting shaft 300 rotates.

[0098] In some embodiments, the heat-conducting plates 400 within each packing layer 203 are divided into an upper plate 410 and a lower plate 420, with the upper plate 410 tilted in the opposite direction to the lower plate 420. This prevents the liquid from flowing in only one direction, increasing the reaction contact time. This oppositely tilted arrangement also reduces the tendency for the liquid to move rapidly along the heat-conducting axis 300, allowing more heat to be exchanged within the current packing layer 203.

[0099] A heat-conducting ring 430 is provided between the upper plate 410 and the lower plate 420, connecting the upper plate 410 and the lower plate 420. The heat-conducting ring 430 can be made of the same material as the heat-conducting plate 400 in the same layer, so that the upper plate 410, the lower plate 420, and the heat-conducting ring 430 form a continuous heat transfer path. The number of heat-conducting rings 430 can be set according to the length and structural strength of the heat-conducting plate 400, for example, 1-3 heat-conducting rings 430 can be set for each group of heat-conducting plates 400. The heat-conducting ring 430 does not have to be a complete circular structure; it can also be an arc segment, a semi-circular structure, or a connecting segment spaced circumferentially, as long as it can achieve the thermal connection between the upper plate 410 and the lower plate 420.

[0100] In one implementation, the end of the upper plate 410 is slidably engaged with the corresponding upper heat insulation plate 210, and the end of the lower plate 420 is slidably engaged with the corresponding lower heat insulation plate 210. With this arrangement, when the heat-conducting shaft 300 drives the heat-conducting plate 400 to rotate, the ends of the upper plate 410 and the lower plate 420 can slide relative to each other along the surface of the corresponding heat insulation plate 210, allowing the heat insulation plate 210 to form a certain circumferential constraint on the heat-conducting plate 400, while not hindering the normal rotation of the heat-conducting plate 400 with the heat-conducting shaft 300. This reduces the radial oscillation of the heat-conducting plate 400 during the rotation of the heat-conducting shaft 300, improving the stability of the operation of the heat-conducting shaft 300 and the heat-conducting plate 400.

[0101] Since the heat insulation plate 210 is provided with a liquid inlet hole 211, when the heat conduction plate 400 rotates and passes near the liquid inlet hole 211, the heat conduction plate 400 can also disturb the packing around the liquid inlet hole 211 to a certain extent, which helps to reduce the accumulation of packing near the liquid inlet hole 211, thereby reducing the possibility of the liquid inlet hole 211 becoming blocked.

[0102] In the thermally conductive shaft sections 310 corresponding to two adjacent filler layers 203, the shaft section 310 with higher thermal conductivity is provided with an extension section 311, and the shaft section 310 with lower thermal conductivity is provided with an insertion groove 312. The extension section 311 is fixedly inserted into the insertion groove 312. In this embodiment, the extension section 311 is columnar. After the extension section 311 extends into the insertion groove 312, it increases the axial contact or heat transfer area between adjacent thermally conductive shaft sections 310, making it easier for the heat collected in the lower thermally conductive shaft section 310 to be transferred to the adjacent upper thermally conductive shaft section 310.

[0103] In particular, the packing layer 203 near the water inlet 201 of the mud bed reaction zone 200 has a relatively high concentration of reactants, and the anaerobic ammonia oxidation reaction is more concentrated, generating a relatively large amount of reaction heat. Therefore, through the lower shaft section 310 and the extension section 311 with a high thermal conductivity, the heat accumulated in this area can be quickly transferred to the adjacent upper shaft section 310, so that the heat generated at the bottom can be transported upward in a preset direction, rather than concentrated at the bottom to form a large temperature difference.

[0104] Meanwhile, since the insertion groove 312 is located within the shaft section 310 with a relatively low thermal conductivity, the rate at which heat continues to transfer towards the outlet end 202 after entering this shaft section 310 is lower than that of the previous high thermal conductivity shaft section 310. Therefore, adjacent shaft sections 310 do not form a simple high-efficiency heat conduction channel, but rather a progressively changing heat transfer path through shaft sections 310 with different thermal conductivity: the shaft section 310 near the inlet end 201 rapidly collects and transfers the heat of reaction, while the shaft section 310 near the outlet end 202 reduces the rate of continued heat transfer, allowing a certain degree of retention of the heat already transferred to the upper packing layer 203.

[0105] Therefore, the extension section 311 and the insertion groove 312 can not only realize the mechanical connection between adjacent heat-conducting shaft sections 310, but also cooperate with the setting of the thermal conductivity of each shaft section 310 decreasing layer by layer, so that a more effective gradient heat transfer structure is formed between adjacent packing layers 203.

[0106] As an optional embodiment, a mounting base 500 is fixedly provided below the heat insulation plate 210 located at the water inlet 201 of the mud bed reaction zone 200, and the lower end of the heat-conducting shaft 300 is rotatably mounted on the mounting base 500. The mounting base 500 can be made of a corrosion-resistant material with a low thermal conductivity. The mounting base 500 is provided with a heat exhaust port 510, which communicates with the liquid outside the water inlet 201 of the mud bed reaction zone 200, and a sealing member 600 is provided at the heat exhaust port 510.

[0107] Under normal operating conditions, the sealing element 600 keeps the heat exhaust port 510 closed, so that the reaction heat generated by the packing layer 203 at the water inlet 201 and collected by the heat conduction shaft 300 is retained as much as possible inside the mud bed reaction zone 200. When the reaction in the packing layer 203 at the water inlet 201 is relatively intense and the temperature at the lower end of the heat conduction shaft 300 continues to rise and exceeds a preset threshold, the sealing element 600 opens the heat exhaust port 510, so that some of the heat accumulated near the water inlet 201 can be transferred to the liquid outside the water inlet 201 of the mud bed reaction zone 200 through the heat conduction shaft 300, the mounting base 500, and the heat exhaust port 510. Figure 8 As shown, the heat dissipation direction F of the heat-conducting shaft 300 and the liquid inlet direction G are illustrated. Therefore, while primarily retaining and utilizing the heat of reaction, it also provides an appropriate heat release path when excessive heat accumulates, preventing a continuous rise in local temperature, thus balancing the utilization of the heat of reaction with safe temperature control.

[0108] The enclosure 600 includes a heat-deformable metal sheet 610, which is connected to the heat-conducting shaft 300, allowing the temperature in the heat-conducting shaft 300 to be transferred to the heat-deformable metal sheet 610. The heat-deformable metal sheet 610 can adopt a bimetallic sheet structure, that is, combining two metal materials with different coefficients of thermal expansion to form a composite sheet.

[0109] For example, a bimetallic sheet can be formed using a copper alloy and a nickel-iron alloy. The two metals expand at different rates under the same temperature change. Because the two materials are interconnected, the difference in thermal expansion causes the overall sheet to bend and deform. By adjusting the combination of the two metals, their thickness ratio, and the effective deformation length, the temperature response characteristics of the heat-deformable metal sheet 610 can be altered, allowing it to generate sufficient deformation to drive the closure 600 after reaching a preset temperature. In practical applications, a bimetallic sheet of appropriate specifications can be selected based on the temperature range that the heat-conducting shaft 300 needs to control, rather than being limited to the above material combinations. Figure 8As shown, the deformation direction E of the heat-deformable metal sheet 610 is illustrated.

[0110] When the temperature of the heat-conducting shaft 300 rises and reaches the operating temperature of the heat-deformed metal sheet 610, heat is transferred to the heat-deformed metal sheet 610 via the heat-conducting shaft 300, causing the heat-deformed metal sheet 610 to bend and deform. This deformation displacement then moves the sealing member 600 away from the heat outlet 510, thus opening the heat outlet 510. At this time, some of the heat accumulated near the water inlet 201 can be transferred to the outer liquid through the heat outlet 510, achieving appropriate release of excessively high temperatures.

[0111] When the temperature of the heat-conducting shaft 300 drops to the recovery temperature of the heat-deformed metal sheet 610, the degree of deformation of the heat-deformed metal sheet 610 decreases, and it drives the sealing member 600 to move back towards the heat exhaust port 510, so that the heat exhaust port 510 returns to the closed state. Through the deformation of the heat-deformed metal sheet 610 itself with temperature changes, the temperature-responsive opening and closing of the heat exhaust port 510 can be achieved without setting up an additional complex temperature control mechanism.

[0112] The specific operating temperature can be set according to the actual suitable reaction temperature of the anaerobic ammonia oxidizing bacteria, the operating temperature of the reaction vessel 100, and the allowable temperature fluctuation range. For example, in one embodiment, the opening temperature of the heat exhaust port 510 can be set in the range of 35℃-40℃. That is, when the temperature of the heat conduction shaft 300 is higher than the normal reaction temperature and reaches the preset opening temperature, the heat exhaust port 510 is opened to release an appropriate amount of heat. The closing temperature of the heat exhaust port 510 is set in the range of 33℃-35℃, so that the temperature of the heat conduction shaft 300 drops to close to the temperature range required for the normal reaction of the anaerobic ammonia oxidizing bacteria, and then the heat exhaust port 510 is closed. This results in the opening temperature being higher than the closing temperature, forming a certain temperature hysteresis between the two, and avoiding frequent opening and closing of the heat exhaust port 510 near the critical temperature. The above temperature range is only one implementation example, and can be adjusted according to the characteristics of the anaerobic ammonia oxidizing bacteria, the reaction load, and the operating conditions of the reaction vessel 100.

[0113] In some embodiments, to reduce the interference of the liquid temperature outside the water inlet 201 of the mud bed reaction zone 200 on the operating characteristics of the heat-deformed metal sheet 610, a thermal insulation layer 614 can be provided on the outside of the heat-deformed metal sheet 610. The thermal insulation layer 614 can be made of polyurethane foam, aerogel felt, or other thermal insulation materials suitable for this environment. By providing the thermal insulation layer 614, the direct heat exchange between the external liquid and the heat-deformed metal sheet 610 can be reduced, allowing the heat-deformed metal sheet 610 to primarily respond to temperature changes transmitted by the heat-conducting shaft 300, thereby improving the stability of its operating temperature.

[0114] In some embodiments, a contact head 613 may be provided between the heat-deformable metal sheet 610 and the lower end of the heat-conducting shaft 300 to increase the contact area between the two, so that the heat at the lower end of the heat-conducting shaft 300 can be transferred to the heat-deformable metal sheet 610 more quickly and stably. The contact head 613 may be independently provided and fixed to the lower end of the heat-conducting shaft 300, or it may be formed by bending a part of the heat-deformable metal sheet 610 to reduce the number of parts.

[0115] In some embodiments, a deformation groove 611 may also be provided on the heat-deformable metal sheet 610. The deformation groove 611 can extend along a preset deformation direction. By changing the stiffness of a local area of ​​the heat-deformable metal sheet 610, the main deformation position of the heat-deformable metal sheet 610 can be guided so that it bends in a preset direction after being heated.

[0116] As an optional embodiment, the bottom end of the heat dissipation port 510 can be configured as a large, bowl-shaped arc-shaped groove, with the wider end facing downwards. This allows a larger contact area to be formed along the periphery of the bowl-shaped arc-shaped groove when the heat-deformable metal sheet 610 deforms and abuts against the heat dissipation port 510. Compared to a simple planar contact structure, this arc-shaped fit improves the adhesion between the heat-deformable metal sheet 610 and the heat dissipation port 510, and provides a certain guiding space for the heat-deformable metal sheet 610 to deform under heat.

[0117] In some embodiments, a rubber gasket 612 may be provided between the heat-deformable metal sheet 610 and the heat outlet 510. The rubber gasket 612 may be made of corrosion-resistant fluororubber or silicone rubber, so that when the heat-deformable metal sheet 610 closes the heat outlet 510, the rubber gasket 612 can generate an elastic compression and sealing effect, reducing the risk of landfill leachate leakage from the heat outlet 510. The rubber gasket 612 can also form a buffer between the heat-deformable metal sheet 610 and the heat outlet 510.

[0118] In other embodiments, the sealing member 600 may also be a sealing plate structure, with the sealing plate connected to a motor drive and driven by the motor to move relative to the heat exhaust port 510, thereby realizing the active opening and closing of the heat exhaust port 510. A temperature detection probe may be installed inside the reaction device to detect the temperature of the heat-conducting shaft 300 or the temperature near the water inlet 201 of the mud bed reaction zone 200, and transmit the detection results to the controller.

[0119] The controller can control the motor action based on the relationship between the detected temperature and the preset temperature threshold: when the detected temperature exceeds the preset opening threshold, the controller controls the motor to drive the sealing plate to open the heat exhaust port 510, so that some of the reaction heat accumulated near the water inlet 201 is released to the outside liquid; when the detected temperature drops to the preset closing temperature, the controller controls the motor to drive the sealing plate to close the heat exhaust port 510, so that the reaction heat is maintained inside the mud bed reaction zone 200 again.

[0120] In addition, the reaction device itself is usually equipped with a temperature detection probe in the mud bed reaction zone 200 to monitor the temperature status of the mud bed reaction zone 200 in real time. Therefore, in the embodiment using a motor-driven enclosed plate, the temperature data of the mud bed reaction zone 200 can be directly obtained using the existing temperature detection probe, and the controller can control the motor rotation based on the temperature data, without the need for an additional independent temperature detection system.

[0121] This allows the opening and closing of the heat dissipation port 510 to correspond to the actual temperature state of the mud bed reaction zone 200: when the temperature is within the normal range, the heat dissipation port 510 should be kept closed as much as possible to reduce the loss of reaction heat; when the temperature is too high, the heat dissipation port 510 should be opened to release an appropriate amount of heat, so that the heat utilization structure of this application can not only "lock in" the reaction heat, but also make adaptive adjustments when the heat accumulates excessively.

[0122] As a specific operational embodiment, when using the anaerobic ammonia oxidation reactor of this application for landfill leachate treatment, the base liquid temperature of the reaction tank 100 can be set according to the actual reaction temperature requirements of the anaerobic ammonia oxidizing bacteria. Taking the requirement to heat and maintain the liquid in the reaction tank 100 at approximately 35°C during normal operation as an example, after adopting the structure of this application, the base temperature of the liquid in the reaction tank 100 can be set to approximately 30°C, which is about 5°C lower than the operation method of directly maintaining the liquid in the entire reaction tank 100 at 35°C.

[0123] At this time, the anaerobic ammonia oxidation reaction takes place in the mud bed reaction zone 200 and continuously generates heat. The reaction heat generated by the packing layer 203 near the water inlet 201 is transferred to the subsequent packing layer 203 through the heat-conducting plate 400 and the shaft section 310 of the heat-conducting shaft 300 with a high thermal conductivity. The lower thermal conductivity of the shaft section 310 of the subsequent packing layer 203 is used to reduce the rate of heat loss, so that the reaction heat is transferred and retained step by step in the mud bed reaction zone 200, thereby compensating for the temperature of the liquid in the mud bed reaction zone 200.

[0124] Under the above operating conditions, the reaction tank 100 does not rely on an external heating device to continuously heat all the liquid from 30°C to 35°C. Instead, it uses a lower base temperature as the operating condition and utilizes the heat generated by the anaerobic ammonia oxidation reaction itself to compensate for the heat in the reaction zone, thereby reducing energy consumption during the continuous temperature regulation process.

[0125] The above description is merely a specific embodiment of this application, but the scope of protection of this application is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in this application should be included within the scope of protection of this application.

Claims

1. An anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate, comprising a reaction tank (100), wherein a sludge bed reaction zone (200) is provided within the reaction tank (100), characterized in that, Also includes: A heat insulation plate (210) is provided at intervals from the water inlet (201) to the water outlet (202) of the mud bed reaction zone (200), and the mud bed reaction zone (200) is divided into multiple packing layers (203). A number of liquid inlet holes (211) are provided on the heat insulation plate (210). A heat-conducting shaft (300) is inserted through each of the packing layers (203). The upper end of the heat-conducting shaft (300) extends at least partially into the liquid outside the water outlet (202) of the mud bed reaction zone (200), and the lower end of the heat-conducting shaft (300) is located in the packing layer (203) near the water inlet (201) of the mud bed reaction zone (200). Each of the filler layers (203) is provided with a plurality of heat-conducting plates (400) fixed on the heat-conducting shaft (300). Each of the heat-conducting plates (400) is arranged circumferentially along the heat-conducting shaft (300) and extends radially outward. The thermal conductivity of the shaft segment (310) of the heat-conducting shaft (300) located in each of the packing layers (203) is the same as that of the corresponding heat-conducting plate (400). Furthermore, along the direction from the inlet end (201) to the outlet end (202) of the mud bed reaction zone (200), the thermal conductivity of the shaft segment (310) of the heat-conducting shaft (300) and the heat-conducting plate (400) corresponding to each of the packing layers (203) decreases layer by layer.

2. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 1, characterized in that, The heat-conducting shaft (300) is rotatably disposed inside the reaction vessel (100); And / or, the heat-conducting shaft (300) is located in the middle of the mud bed reaction zone (200).

3. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 1, characterized in that, Along the direction from the inlet end (201) to the outlet end (202) of the mud bed reaction zone (200), the distribution density of the heat-conducting plates (400) in each of the packing layers (203) decreases layer by layer in the circumferential direction of the heat-conducting axis (300); And / or, the surface of the heat-conducting plate (400) is provided with a bio-compatible coating; And / or, each of the heat-conducting plates (400) is arranged at an angle; And / or, the heat-conducting plate (400) is a thin plate structure.

4. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 3, characterized in that, The heat-conducting plate (400) in each of the filler layers (203) is divided into an upper plate (410) and a lower plate (420), and the tilting direction of the upper plate (410) is opposite to that of the lower plate (420).

5. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 4, characterized in that, A heat-conducting ring (430) is provided between the upper plate (410) and the lower plate (420), and the heat-conducting ring (430) is connected to the upper plate (410) and the lower plate (420). And / or, the end of the upper plate (410) is slidably engaged with the corresponding upper heat insulation plate (210); And / or, the end of the lower plate (420) is slidably engaged with the corresponding lower heat insulation plate (210).

6. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 1, characterized in that, In the thermally conductive shaft segments (310) corresponding to two adjacent filler layers (203), the shaft segment (310) with high thermal conductivity is provided with an extension segment (311), and the shaft segment (310) with low thermal conductivity is provided with an insertion groove (312). The extension segment (311) is inserted into the insertion groove (312).

7. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 1, characterized in that, A mounting base (500) is provided below the heat insulation plate (210) located at the water inlet (201) of the mud bed reaction zone (200). The lower end of the heat-conducting shaft (300) is rotatably mounted on the mounting base (500). The mounting base (500) is provided with a heat exhaust port (510). The heat exhaust port (510) can communicate with the liquid outside the water inlet (201) of the mud bed reaction zone (200). A sealing member (600) is provided at the heat exhaust port (510). The sealing member (600) opens the heat exhaust port (510) when the temperature of the heat-conducting shaft (300) exceeds a threshold value, and closes the heat exhaust port (510) when the temperature is below the threshold value.

8. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 7, characterized in that, The closure (600) includes a heat-deformable metal sheet (610) connected to the heat-conducting shaft (300). The heat-deformable metal sheet (610) deforms to open the heat exhaust port (510) when the temperature of the heat-conducting shaft (300) exceeds a threshold, and restores its deformation to close the heat exhaust port (510) when the temperature of the heat-conducting shaft (300) is below the threshold.

9. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 2, characterized in that, The reaction vessel (100) is provided with a drive unit (700), which is used to drive the heat-conducting shaft (300) to rotate.

10. The anaerobic ammonia oxidation reactor for full-volume treatment of landfill leachate according to claim 9, characterized in that, The drive unit (700) includes a drive motor (710), which is located above the reaction vessel (100). The output shaft of the drive motor (710) passes into the reaction vessel (100) and is connected to the upper end of the heat-conducting shaft (300) through a flange (710). The flange (710) is made of heat-insulating material.

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