Asymmetric continuous flow h-type dual-chamber microbial fuel cell and method of operating the same

Abstract

The application relates to the technical field of biological batteries, in particular to an asymmetric continuous-flow H-shaped double-chamber microbial fuel cell and an operation method thereof. Through the differential configuration of the anode side and the cathode side in the fluid mechanics condition, the construction of the conductive network in the anode chamber and the artificial regulation of the external circuit electronic output condition, the electrogenic bacteria, the fermenting bacteria and the mutual bacteria in the anode microbial community can form a high-efficiency and stable interspecies electron mutual operation relationship under the dual actions of the spatial proximity and the electronic transmission thermodynamic driving force. The application aims to solve the problem of how to improve the electricity generation performance of the double-chamber microbial fuel cell.

Description

Technical Field

[0001] This application relates to the field of bio-battery technology, and in particular to an asymmetric continuous flow H-type dual-chamber microbial fuel cell and its operation method. Background Technology

[0002] Microbial fuel cells (MFCs) are a type of bioelectrochemical device that utilizes microorganisms to catalyze the oxidation of organic substrates and convert chemical energy into electrical energy. A typical MFC includes an anode chamber, a cathode chamber, an ion migration device, and an external circuit. Microorganisms in the anode chamber oxidize the organic substrate under anaerobic conditions, releasing electrons and protons. Electrons are transferred to the cathode via the external circuit, and protons reach the cathode through the ion migration device to participate in the reduction reaction, thus forming a current loop. H-type dual-chamber MFCs are widely used for MFC mechanism research and laboratory validation due to their simple structure, clear separation between the anode and cathode chambers, and ease of independent control of the reaction conditions in both chambers. In existing technologies, H-type dual-chamber MFCs typically employ a symmetrical or near-symmetrical cavity design, with the anode and cathode chambers having essentially the same volume, flow channel configuration, and electrode arrangement.

[0003] While this symmetrical structure can separate the anode and cathode reactions, it has significant limitations under continuous flow operation: First, the stable enrichment of biofilm on the anode side and the full degradation of substrate require a long hydraulic residence time, while the rapid replenishment of electron acceptors on the cathode side requires a short hydraulic residence time to reduce mass transfer resistance. The symmetrical cavity cannot simultaneously meet the differentiated mass transfer needs of both sides. Second, electron exchange between microorganisms in the anode microbial community largely depends on diffuse intermediates or local physical contacts. In the absence of a conductive network structure, it is difficult to form a stable and efficient interspecies electron transfer pathway, limiting the anode electron recovery efficiency. Furthermore, traditional devices mostly operate with a fixed external resistance, making it impossible to apply selective pressure to the electroactive microbial community through dynamic changes in the load, and making it difficult to actively regulate the population structure of the microbial community.

[0004] In view of this, this application proposes an asymmetric continuous flow H-type dual-chamber microbial fuel cell structure, aiming to construct a physical environment conducive to interspecies electron exchange among microorganisms at the structural level, realize differentiated mass transfer conditions between the anode and cathode sides, and construct an anode microbial electron exchange environment that can improve the anode electron recovery efficiency. Summary of the Invention

[0005] The main objective of this application is to provide an asymmetric continuous flow H-type dual-chamber microbial fuel cell, aiming to solve the problem of how to improve the power generation performance of dual-chamber microbial fuel cells.

[0006] To achieve the above objectives, this application provides an asymmetric continuous flow H-type dual-chamber microbial fuel cell, comprising an anode electrode disposed in the anode chamber and a cathode electrode disposed in the cathode chamber, and further comprising: The anode chamber includes an anaerobic continuous flow reaction chamber, which contains influent containing organic substrate; The cathode chamber includes an electron acceptor reduction reaction chamber, which contains a cathode liquid containing electron acceptors; An H-shaped connection channel is disposed between the anode chamber and the cathode chamber, and an ion migration component is disposed in the H-shaped connection channel to maintain ion conduction between the anode chamber and the cathode chamber; A conductive packing biofilm region is disposed in the anode chamber, the conductive packing biofilm region is filled with conductive packing, and the conductive packing is in conductive contact with the anode electrode to form a continuous conductive network. The effective volume of the anode chamber is greater than the effective volume of the cathode chamber, so that the hydraulic residence time of the anode is greater than the hydraulic residence time of the cathode.

[0007] Optionally, the ion migration component includes at least one of a proton exchange membrane, a cation exchange membrane, or a salt bridge; The proton exchange membrane or the cation exchange membrane is fixed in the H-shaped connection channel by sealing gaskets and clamping fasteners disposed on both sides of the membrane; the salt bridge includes a porous tube, a gel electrolyte filled in the porous tube, and porous separators disposed at both ends of the porous tube.

[0008] Optionally, the organic substrate includes at least one of anaerobic sludge, electroactive microorganisms, and mixed microbial communities.

[0009] Optionally, the cathode liquid containing the electron acceptor includes at least one of dissolved oxygen, aerated air, and ferricyanide.

[0010] Optionally, it also includes: An external circuit is used to connect the anode electrode and the cathode electrode, and is equipped with an adjustable load module.

[0011] Optionally, the adjustable load module is configured to switch between different resistance values ​​at preset time intervals.

[0012] Optionally, the effective volume ratio of the anode chamber to the cathode chamber is 1.2 to 3.0.

[0013] Optionally, the conductive filler is one or a mixture of granular activated carbon, biochar, graphite particles, carbon felt fragments, and magnetite.

[0014] Optionally, the ratio of the liquid inlet flow rate of the anode chamber to the liquid inlet flow rate of the cathode chamber is 0.3 to 1.0.

[0015] Furthermore, to achieve the above objectives, this application also provides an operating method for an asymmetric continuous flow H-type dual-chamber microbial fuel cell as described above, the operating method comprising the following steps: S10 controls the adjustable load module to operate with a preset initial external resistance value and a preset initial substrate load, so that anodic microorganisms attach to the conductive filler and the surface of the anode electrode. S20, when the load voltage is stable within a preset time period, the external resistance value of the adjustable load module is reduced at preset intervals to determine the target external resistance value corresponding to the maximum power transmission point in the current operating state. S30, according to a preset time interval, control the adjustable load module to cycle between multiple different external resistance values ​​so that the anode microbial community evolves under changing electron output conditions, wherein the external resistance value includes at least the target external resistance value.

[0016] This application has at least the following beneficial effects: 1. Setting the effective volume of the anode chamber to be larger than that of the cathode chamber creates an asymmetric structure, which prolongs the hydraulic residence time on the anode side. This facilitates full contact between the influent containing organic substrates and the electroactive microbial biofilm attached to the conductive packing and the surface of the anode electrode, thereby improving the mass transfer efficiency and biodegradation degree of the substrate to the microorganisms. At the same time, due to the smaller volume on the cathode side, the hydraulic residence time is correspondingly shortened, which is conducive to the rapid renewal and replenishment of electron acceptors and reduces the mass transfer polarization overpotential on the cathode side. 2. The conductive packing biofilm region provides a physical channel for electron transfer to microorganisms, enabling the microbial community enriched in the asymmetric flow field to achieve interspecific electron exchange through the conductive network; 3. An adjustable load module is configured in the external circuit to provide an adjustable thermodynamic driving force for the transfer of electrons along the conductive network to the external circuit, thereby actively regulating the electron output behavior of the microbial community. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the architecture of the asymmetric continuous flow H-type dual-chamber microbial fuel cell involved in the embodiments of this application; Figure 2 This is a cross-sectional schematic diagram of the conductive filler biofilm region involved in an embodiment of this application; Figure 3 This is a trend graph showing the effect of the effective anode / cathode volume ratio on output power in the embodiments of this application; Figure 4This is a flowchart of the operation method of the asymmetric continuous flow H-type dual-chamber microbial fuel cell involved in the embodiments of this application.

[0018] The realization of the purpose, functional features and advantages of this application will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0019] To better understand the above technical solutions, exemplary embodiments of this disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of this disclosure are shown in the drawings, it should be understood that this disclosure can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of this disclosure to those skilled in the art.

[0020] First Embodiment Reference Figure 1 and Figure 2 This embodiment provides an asymmetric continuous flow H-type dual-chamber microbial fuel cell, including an anode electrode 5 disposed in the anode chamber 1 and a cathode electrode 6 disposed in the cathode chamber 2, characterized in that it further includes: The anode chamber 1 includes an anaerobic continuous flow reaction chamber, which contains influent containing organic substrate; Specifically, the anode chamber 1 is configured to accommodate influent containing organic substrates and provide an anaerobic reaction space for the attachment and metabolism of electroactive microbial communities. The bottom of the anode chamber 1 is provided with an anode inlet 8 and a bottom support anti-clogging mesh 19, and the top or side wall is provided with an anode outlet 9, so that the influent can flow through the packing bed area in the anode chamber from bottom to top, forming a stable concentration gradient and hydraulic conditions.

[0021] In some alternative embodiments, the anode electrode may be one or more of a combination of carbon felt, carbon brush, graphite felt, carbon cloth or stainless steel skeleton composite carbon material, with its main body disposed in the lower middle region of the anode chamber to form sufficient conductive contact with the conductive filler filling the anode chamber.

[0022] The cathode chamber 2 includes an electron acceptor reduction reaction chamber, which contains a cathode liquid containing electron acceptors; Specifically, the cathode chamber 2 is provided with a cathode inlet 10, a cathode outlet 11, and an electron acceptor supply port 12. The electron acceptor supply port 12 is used to supply dissolved oxygen, aerated air, or ferricyanide solution, etc., to the cathode chamber.

[0023] In some alternative embodiments, the cathode electrode 6 may be made of carbon cloth, carbon felt, air cathode, or other electrode materials suitable for oxygen reduction or electron acceptor reduction.

[0024] An H-shaped connection channel 3 is provided between the anode chamber 1 and the cathode chamber 2. An ion migration component 4 is provided in the H-shaped connection channel. The ion migration component 4 is used to maintain ion conduction between the anode chamber 1 and the cathode chamber 2. Specifically, the H-type connecting channel 3 is a tubular or rectangular cross-section flow channel, with its two ends sealed to the side walls of the anode chamber 1 and the cathode chamber 2, respectively. An ion migration component 4 is installed inside the H-type connecting channel. This component 4 maintains ion conduction between the anode and cathode chambers while suppressing direct mixing and cross-contamination of the liquids in the two chambers.

[0025] In some alternative embodiments, the ion migration component may include one of a proton exchange membrane, a cation exchange membrane, or a salt bridge. Specifically, when a proton exchange membrane or a cation exchange membrane is used, the membrane is laterally positioned in the middle of the H-shaped connection channel and is pressed and fixed by corrosion-resistant sealing gaskets and clamping fasteners located on both sides of the membrane, so that the effective conduction area of ​​the membrane is connected to the H-shaped connection channel, while preventing direct convection mixing of the anolyte and catholyte. When a salt bridge is used, the salt bridge includes an insulating porous tube, a gel electrolyte filled in the porous tube, and porous separators sealed at both ends of the tube; the gel electrolyte may be prepared by agar or agarose with at least one inert electrolyte selected from potassium chloride and sodium chloride, and the porous separators are used to limit gel loss and allow ion migration. A sealing structure is provided between the outer periphery of the ion migration component and the H-shaped connection channel to prevent short-circuiting and leakage.

[0026] The conductive packing biofilm region 7 is set in the anode chamber 1. The conductive packing biofilm region 7 is filled with conductive packing. The conductive packing is in conductive contact with the anode electrode 5 to form a continuous conductive network. Specifically, the conductive filler and the anode electrode 5 form a conductive connection through physical contact, thereby constructing a continuous three-dimensional conductive network throughout the entire cavity of the anode chamber.

[0027] Further and optionally, the conductive filler material can be one or a mixture of granular activated carbon, biochar, graphite particles, carbon felt fragments, and magnetite. In some optional embodiments, the particle size is selected in the range of 0.5~10mm to provide a large specific surface area while maintaining sufficient porosity between the filler bed layers, avoiding clogging and pressure drop problems caused by excessively fine particles.

[0028] It should be noted that the conductive packing biofilm region in this embodiment plays at least the following roles: on the one hand, the conductive packing provides a large attachment interface for electrogenic bacteria, fermenting bacteria, and syntrophic bacteria, enabling microorganisms with different functions to form spatial proximity relationships; on the other hand, the conductive contacts between the conductive packings and with the anode electrode constitute a continuous electron transfer path, allowing microorganisms attached to the surface of the packing to directly transfer electrons generated by metabolism to the anode electrode through this conductive network, without relying on traditional diffused electron intermediates such as hydrogen and formic acid, thereby enhancing the direct interspecies electron transfer process.

[0029] The effective volume of the anode chamber 1 is greater than the effective volume of the cathode chamber 2, so that the hydraulic residence time of the anode is greater than that of the cathode.

[0030] Specifically, the volume of the cathode chamber 2 is smaller than the effective volume of the anode chamber, meaning the effective volume of the anode chamber 1 is larger than the effective volume of the cathode chamber. This results in a longer hydraulic residence time and a larger contact area with the conductive biofilm on the anode side, facilitating sufficient contact between the substrate and the biofilm and the complete degradation of organic matter. On the cathode side, the smaller volume of the chamber results in a higher mass transfer rate per unit volume, which is beneficial for the rapid replenishment of electron acceptors and the continuous progress of reduction reactions.

[0031] Further, and optionally, in this embodiment, the asymmetric continuous flow H-type dual-chamber microbial fuel cell is also equipped with a voltage and current acquisition module 14 and a sampling sensor interface 15. The voltage and current acquisition module 14 is connected across the adjustable load module of the external circuit to monitor the output voltage and current of the fuel cell in real time, and then calculate the output power and system internal resistance. The sampling sensor interface is used to insert monitoring devices such as pH electrodes, oxidation-reduction potential (ORP) probes, dissolved oxygen sensors, and temperature probes to obtain the water quality state parameters of the liquids in the anode and cathode chambers.

[0032] Furthermore, and optionally, all of the above components are fixed and sealed by the support frame 16 to form a complete independent operating unit.

[0033] In the technical solution provided in this embodiment, by differentiating the hydrodynamic conditions of the anode side and the cathode side, constructing the conductive network in the anode chamber, and artificially controlling the electronic output conditions of the external circuit, the electrogenic bacteria, fermenting bacteria, and symbiotic bacteria in the anode microbial community can form an efficient and stable interspecies electronic symbiotic relationship under the dual effects of spatial proximity and the thermodynamic driving force of electron transfer.

[0034] Second Embodiment Based on any embodiment, in this embodiment, the asymmetric continuous flow H-type dual-chamber microbial fuel cell further includes: The external circuit 20 is used to connect the anode electrode 5 and the cathode electrode 6, and is equipped with an adjustable load module 13.

[0035] Further and optionally, the adjustable load module 13 is configured to switch between different resistance values ​​at preset time intervals.

[0036] Specifically, the adjustable load module 13 changes the speed at which electrons flow from the anode electrode through the external circuit to the cathode electrode at different operating stages, thereby applying variable electron output selection pressure to the anode microbial community.

[0037] Optionally, the adjustable load module 13 may be implemented as a manually adjustable resistor box, a program-controlled digital potentiometer, or a periodic load switching module that switches between different resistance values ​​according to preset logic.

[0038] It should be noted that when the resistance of the adjustable load module is high, electron outflow is hindered, and the anode potential increases, which is beneficial for electrogenic bacteria to maintain their advantage in electron competition with symbiotic bacteria. When the resistance is low, electron outflow is smooth, the anode potential decreases, and this is beneficial for increasing the system output power. By selectively changing the load state at different operating stages, the ecological structure of the anode microbial community can be actively altered, allowing microorganisms that can more efficiently output electrons to the anode electrode through the conductive network to gain a competitive advantage. This process is known as "forced electron symbiosis."

[0039] Third Embodiment Based on any embodiment, in this embodiment, the organic substrate of the anaerobic continuous flow reaction chamber in the anode chamber includes at least one of anaerobic sludge, electroactive microorganisms, and mixed microbial communities.

[0040] Specifically, electroactive microbial communities include electrogenic bacteria, fermentative bacteria, and symbiotic bacteria. Electrogenic bacteria are responsible for transferring electrons generated from the metabolism of organic matter to the extracellular space; fermentative bacteria are responsible for hydrolyzing and fermenting complex organic matter into small-molecule organic acids and alcohols, providing substrates that electrogenic bacteria can directly utilize; and symbiotic bacteria achieve co-metabolism with electrogenic bacteria through interspecies electron transfer.

[0041] For example, the electrogenic bacteria can be Geobacter sulfurreducens; the fermenting bacteria can be Clostridium butyricum; and the syntrophomonas can be Syntrophomonas wolfei.

[0042] The sources of active microbial communities can be anaerobic digested sludge from urban wastewater treatment plants, electrogenic mixed microbial communities that have been domesticated in the laboratory for a long time, or artificially prepared synthetic microbial communities.

[0043] In some alternative implementations, before inoculation, the anaerobic sludge can be filtered through a 100-mesh sieve to remove large particulate impurities, and then concentrated to a suspended solids concentration of approximately 10-20 g / L by static sedimentation. During inoculation, the concentrated sludge suspension is pumped into the anode chamber through the anode inlet and circulated for a period of time to allow microorganisms to fully adhere to the conductive packing surface and the anode electrode surface and form an initial biofilm.

[0044] Further and optionally, in this embodiment, the catholyte containing the electron acceptor includes at least one of dissolved oxygen, aerated air, and ferricyanide.

[0045] Specifically, when dissolved oxygen is used as an electron acceptor, water bath aeration or microporous aeration is used to bring the dissolved oxygen concentration in deionized water or buffer solution to near saturation, and then the solution is pumped into the cathode chamber in a continuous flow manner.

[0046] When aerated air is used as the electron acceptor, the cathode chamber can adopt an air cathode structure, that is, one side of the cathode electrode is exposed to the air, and the oxygen in the air directly participates in the reduction reaction as the electron acceptor, without the need for an additional catholyte circulation system.

[0047] When using ferricyanide as an electron acceptor, potassium ferricyanide is dissolved in phosphate buffer or bicarbonate buffer. Ferricyanide as an electron acceptor has the advantages of fast reduction kinetics and low cathode overpotential, making it suitable for research scenarios that require the elimination of cathode mass transfer limitations.

[0048] Fourth embodiment Based on any embodiment, in this embodiment, the effective volume ratio of the anode chamber 1 to the cathode chamber 2 is 1.2 to 3.0.

[0049] Specifically, refer to Figure 3 The trend diagram showing the effect of the effective volume ratio of anode / cathode on output power is presented. In this embodiment, experiments have shown that when the effective volume ratio is less than 1.2, the volume advantage of the anode chamber compared to the cathode chamber is not obvious. It is difficult to form a sufficiently long hydraulic residence time and a sufficiently large space for conductive packing on the anode side, and the mass transfer advantage of the asymmetric design cannot be fully reflected. When the effective volume ratio is greater than 3.0, the cathode chamber volume is too small. Although the mass transfer rate on the cathode side is high, it is easy to lead to insufficient utilization of electron acceptors, and the limited cathode electrode area can easily become a bottleneck in system performance.

[0050] Fifth embodiment Based on any embodiment, in this embodiment, the ratio of the liquid inlet flow rate of the anode chamber 1 to the liquid inlet flow rate of the cathode chamber 2 is 0.3~1.0.

[0051] Specifically, the anode chamber needs to maintain a relatively long hydraulic residence time to ensure sufficient degradation of organic substrates and sufficient contact between electrogenic microorganisms and substrates, so the anode inlet flow rate should not be too high; while the cathode chamber needs a higher liquid exchange frequency to maintain a high electron acceptor concentration and reduce cathode mass transfer polarization, so the cathode inlet flow rate is relatively high.

[0052] Experiments showed that when the ratio of the influent flow rate Qa of anode chamber 1 to the influent flow rate Qc of cathode chamber 2, Qa / Qc, is close to 0.3, the influent flow rate of cathode is about 3 times that of anode. At this time, the mass transfer enhancement effect on the cathode side is the most obvious, which is suitable for operation under conditions with high treatment load or rapid consumption of cathode electron acceptors. When Qa / Qc is close to 1.0, the flow rates on both sides tend to be similar. At this time, the hydraulic conditions of the system are more balanced, which is suitable for use in the start-up period or the early stage of microbial activity establishment.

[0053] Sixth Embodiment Based on the first to fifth embodiments, refer to Figure 4 This embodiment provides an operating method for an asymmetric continuous flow H-type dual-chamber microbial fuel cell as described above, the operating method comprising the following steps: S10 controls the adjustable load module to operate with a preset initial external resistance value and a preset initial substrate load, so that anodic microorganisms attach to the conductive filler and the surface of the anode electrode. In this embodiment, during the startup phase, a relatively high preset initial external resistance value and a relatively low preset initial substrate load are used. During this phase, the higher external resistance value results in a relatively weak thermodynamic driving force for electron flow from the anode to the cathode, maintaining the anode potential at a higher level than the standard hydrogen electrode. This potential condition is conducive to the initial attachment of electroactive microorganisms and their adaptation to the electrode surface, preventing the growth of electrogenic bacteria from being inhibited by an excessively low anode potential due to rapid electron outflow. Simultaneously, the lower substrate load avoids the problem of anolyte acidification caused by the accumulation of organic acids, providing a stable chemical environment for the synergistic colonization of electrogenic and symbiotic bacteria.

[0054] S20, when the load voltage is stable within a preset time period, the external resistance value of the adjustable load module is reduced at preset intervals to determine the target external resistance value corresponding to the maximum power transmission point in the current operating state. In this embodiment, when the load voltage rises steadily to a stable range and shows no significant fluctuations within a preset duration, the startup phase ends and the system transitions to a stable phase. During the stable phase, the external resistor value is adjusted every preset period. After each adjustment, the output voltage is continuously monitored. Once the voltage stabilizes again under the new load conditions, the output voltage and output current under the current load conditions are recorded, and the corresponding output power is calculated accordingly.

[0055] By decreasing the resistance and recording the electrical parameters, the voltage-current-power response curves of the system under different external resistance conditions can be obtained. This allows us to determine the target external resistance value corresponding to the maximum power transfer point under the current operating condition, denoted as R. opt .

[0056] S30, according to a preset time interval, control the adjustable load module to cycle between multiple different external resistance values ​​so that the anode microbial community evolves under changing electron output conditions, wherein the external resistance value includes at least the target external resistance value.

[0057] The target external resistance value R corresponding to the point of maximum power transfer is obtained. opt Then, the system cycles through multiple different external resistance values ​​at preset time intervals, wherein the external resistance values ​​include at least the target external resistance value R corresponding to the maximum power transmission point. opt .

[0058] With two external resistance values: namely, the target external resistance value R opt and a higher than R opt The second external resistance value R high For example, in one complete cycle, the system first uses the target external resistance value R. opt Run for a preset time, then switch to the second external resistance value R. high Run for a preset duration, and repeat in this loop.

[0059] It should be noted that during the high resistance period (i.e., at the second external resistance value R), high During this period, electron outflow is hindered, and the anode potential increases, which is beneficial for symbiotic bacteria that conduct interspecies electron transfer through the conductive packing network to gain a competitive advantage; during the low-resistance period (i.e., at the target external resistance value R), opt During this period, the smooth outflow of electrons is conducive to the enrichment of electrogenic bacteria with high electrochemical activity. Through the alternating application of this dynamic selection pressure, the anodic microbial community cannot adapt to a fixed electron output condition for a long time, thus forcing the community as a whole to evolve in a direction that can flexibly adapt to changing conditions and maintain efficient electron transfer, thereby achieving "forced electron exchange".

[0060] Although preferred embodiments of this application have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments as well as all changes and modifications falling within the scope of this application.

[0061] Obviously, those skilled in the art can make various modifications and variations to this application without departing from the spirit and scope of this application. Therefore, if such modifications and variations fall within the scope of the claims of this application and their equivalents, this application also intends to include such modifications and variations.

Claims

1. An asymmetric continuous flow H-type dual-chamber microbial fuel cell, comprising an anode electrode disposed in the anode chamber and a cathode electrode disposed in the cathode chamber, characterized in that, Also includes: The anode chamber includes an anaerobic continuous flow reaction chamber, which contains influent containing organic substrate; The cathode chamber includes an electron acceptor reduction reaction chamber, which contains a cathode liquid containing electron acceptors; An H-shaped connection channel is disposed between the anode chamber and the cathode chamber, and an ion migration component is disposed in the H-shaped connection channel to maintain ion conduction between the anode chamber and the cathode chamber; A conductive packing biofilm region is disposed in the anode chamber, the conductive packing biofilm region is filled with conductive packing, and the conductive packing is in conductive contact with the anode electrode to form a continuous conductive network. The effective volume of the anode chamber is greater than the effective volume of the cathode chamber, so that the hydraulic residence time of the anode is greater than the hydraulic residence time of the cathode.

2. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The ion migration component includes at least one of a proton exchange membrane, a cation exchange membrane, or a salt bridge. The proton exchange membrane or the cation exchange membrane is fixed in the H-shaped connection channel by sealing gaskets and clamping fasteners disposed on both sides of the membrane; the salt bridge includes a porous tube, a gel electrolyte filled in the porous tube, and porous separators disposed at both ends of the porous tube.

3. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The organic substrate includes at least one of anaerobic sludge, electroactive microorganisms, and mixed microbial communities.

4. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The cathode liquid containing the electron acceptor includes at least one of dissolved oxygen, aerated air, and ferricyanide.

5. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, Also includes: An external circuit is used to connect the anode electrode and the cathode electrode, and is equipped with an adjustable load module.

6. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 5, characterized in that, The adjustable load module is configured to switch between different resistance values ​​at preset time intervals.

7. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The effective volume ratio of the anode chamber to the cathode chamber is 1.2 to 3.

0.

8. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The conductive filler is one or a mixture of granular activated carbon, biochar, graphite particles, carbon felt fragments, and magnetite.

9. The asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in claim 1, characterized in that, The ratio of the liquid inlet flow rate of the anode chamber to the liquid inlet flow rate of the cathode chamber is 0.3 to 1.

0.

10. A method for operating an asymmetric continuous flow H-type dual-chamber microbial fuel cell as described in any one of claims 1 to 9, characterized in that, The operating method includes the following steps: S10 controls the adjustable load module to operate with a preset initial external resistance value and a preset initial substrate load, so that anodic microorganisms attach to the conductive filler and the surface of the anode electrode. S20, when the load voltage is stable within a preset time period, the external resistance value of the adjustable load module is reduced at preset intervals to determine the target external resistance value corresponding to the maximum power transmission point in the current operating state. S30, according to a preset time interval, control the adjustable load module to cycle between multiple different external resistance values ​​so that the anode microbial community evolves under changing electron output conditions, wherein the external resistance value includes at least the target external resistance value.

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