Bipolar membrane, bioelectrochemical device including bipolar membrane, and energy and resource application device including bipolar membrane

Abstract

According to a self-pH-balancing bipolar membrane and a manufacturing method thereof, and a microorganism electrolytic cell, a hydrogen-producing device, a resource recovery device, and an acid-base-producing device that include the bipolar membrane, the bipolar membrane (BPM) can perform self-balancing of pH by OH- and can be implemented in a cylindrical form and formed by dual electrospinning to increase the interfacial area and thereby reduce voltage drop and membrane resistance.

Description

Anode membrane, bioelectrochemical device including anode membrane, and energy and resource application device including anode membrane

[0001] This document relates to a microbial electrolysis cell that produces hydrogen.

[0002] Figure 1a is a diagram illustrating the process of producing hydrogen from organic waste resources based on microbial electro-fermentation, and Figure 1b is a diagram illustrating the bio-electro-fermentation process.

[0003] Referring to Fig. 1a, hydrogen can be produced from organic waste resources based on microbial electrofermentation. Specifically, to overcome the limitations of biological fermentation hydrogen production, electrodes are provided as electron acceptors, allowing for the simultaneous implementation of fermentation and respiration processes. More specifically, energy such as hydrogen can be recovered from organic waste resources using electrochemically active bacteria. That is, microbial electrofermentation fusion energy can be recovered by generating an electric current using organic waste fermentation microorganisms and anode-respiring bacteria. Furthermore, 12 mol of hydrogen is produced per 1 mol of glucose, and since the recovered hydrogen is of high purity and does not require CO2 separation, high-yield / high-purity biohydrogen can be produced. Additionally, referring to Fig. 1b, the process of bio-electrofermentation consisting of dark fermentation and a bio-electrolyte cell is applicable from high to low concentrations, and since fermentation, hydrogen, and purification are possible in a one-step process, a compact system with high flexibility of raw materials can be designed.

[0004] Figure 2 is a diagram illustrating a conventional microbial electrolytic cell.

[0005] Referring to Fig. 2, a conventional microbial electrolysis cell (MEC) can produce hydrogen using electrochemical hydrogen production technology that utilizes the biocatalytic oxidation process of the anode electrode and the reduction process of the cathode electrode. That is, at the anode electrode, "C6H 12 O6 + 6H2O -> 6CO2 + 24e - + 24H + The oxidation process of " takes place, and at the cathode electrode, "2H2O + 2e - -> H2 + 2OH - The reduction process of can be carried out.

[0006] Figure 3 is a diagram illustrating the hydrogen production operation using a conventional fermentation tank and steam reforming, and the hydrogen production operation using conventional microbial electrolysis technology.

[0007] Referring to Figure 3, a hydrogen production operation using conventional microbial electrolysis technology can produce approximately 1.7 times more hydrogen than a hydrogen production operation using conventional microbial fermentation and steam reforming. In addition, a hydrogen production operation using conventional microbial electrolysis technology consumes 9.6 kWh / kg of electrical energy (assuming: 0.9 kg kWh / kg COD, 47 mol H2 / kg COD), whereas a hydrogen production operation using conventional microbial fermentation and steam reforming consumes 11.1 kWh / kg of electrical energy. That is, based on microbial electrolysis technology, it is possible to produce approximately 650,000 tons of hydrogen annually (producing 14% of the 2040 hydrogen supply target) by utilizing solid / liquid organic waste resources, and achieve a reduction effect of 4.6 million tons of CO2-eq / y.

[0008] Figure 4 is a diagram illustrating the operation of P2X (Power to X) using conventional microbial electrochemical technology.

[0009] Referring to Figure 4, microbial electrochemical technology capable of intermittent power application is a future technology that can be applied as P2X (Power to X) technology.

[0010] Figure 5 is a diagram illustrating the technical issues of conventional microbial electrochemical technology.

[0011] Referring to Fig. 5, according to the driving method of conventional microbial electrochemical technology, the anode electrode has a low pH (pH < 6) while the cathode electrode has a high pH (pH > 11), and losses occur due to electrode potential, electrolyte resistance, membrane resistance, and pH imbalance between the two chambers.

[0012] FIG. 6 is a diagram illustrating a conventional anode film, and FIG. 7 is a diagram illustrating a method for manufacturing a conventional anode film.

[0013] Referring to Fig. 6, the bipolar membrane (BPM) is a special type in which a cation exchange layer (CEL) and an anion exchange layer (AEL) are combined. However, the bipolar membrane (BPM) has a higher resistance compared to a single membrane, and current commercial bipolar membranes (BPM) undergo repeated expansion and contraction during repeated charging and discharging, resulting in delamination. Although bipolar membranes (BPM) are recently applied in various fields such as energy storage, acid-base production, and water treatment, there are problems with high resistance and high cost.

[0014] Referring to Fig. 7, a conventional bipolar membrane (BPM) can be manufactured through an immersing step of the HPAN membrane, a heating step, a casting step of Fe(III)@PEI-based HPAN, and a water dissociation step of the Fe(III)@PEI-based BPM. The design of the interlayer region where water is dissociated, which is the interface between the cation exchange layer (CEL) and the anion exchange layer (AEL), is key to the bipolar membrane (BPM). It is necessary to improve the performance of water dissociation through the use of an appropriate catalyst, and to reduce the thickness of the cation exchange layer (CEL) and the anion exchange layer (AEL) to lower membrane resistance, while preventing co-ion leakage.

[0015] According to one embodiment of the present document, a self-pH-balancing bipolar membrane (BPM) that performs pH self-balancing, is implemented in a cylindrical shape, and is formed by double electrospinning, and a method for manufacturing the same may be provided.

[0016] In addition, according to one embodiment of the present document, a microbial electrolytic cell, a hydrogen production device, a resource recovery device, and an acid-base production device comprising a self-pH-balancing bipolar membrane (BPM) may be provided.

[0017] In addition, according to another embodiment of the present document, the purpose is to provide an electrochemical device capable of increasing the capacity of an electrochemical cell stack using a zero-gap structure and an electrochemical module using the same.

[0018] In particular, according to another embodiment of this document, as it can be utilized as a hydrogen production device capable of recovering energy from organic waste resources using electrochemically active bacteria, we intend to provide an electrochemical device and an electrochemical module utilizing the same that can produce hydrogen more effectively using microbial electrochemical technology.

[0019] In addition, according to another embodiment of the present document, there is an intention to provide an electrochemical device and an electrochemical module utilizing the same that can be scaled up in large capacity using a zero-gap structure for at least one of an energy conversion device including a fuel cell and a water electrolysis device, an energy storage device including a battery and a capacitor, an electrochemical reaction device, a wastewater treatment and resource recovery device, an electrochemical bioreactor including a microbial electrochemical device, an electrochemical desalination device including an electrodialysis device, a carbon dioxide conversion device, a metal electrodeposition and resource recovery device, reverse electrodialysis (RED), an electrolysis cell stack, and microbial reverse-electrodialysis electrolysis cells.

[0020] The problems to be solved in this disclosure are not limited to those mentioned above and can be extended in various ways without departing from the spirit and scope of this disclosure.

[0021] A self-pH-balancing bipolar membrane according to one embodiment of the present document is a bipolar membrane (BPM) used in a microbial electrolysis cell (MEC), comprising a cation exchange layer (CEL); and an anion exchange layer (AEL); and the bipolar membrane (BPM) is in the shape of a cylinder.

[0022] The above bipolar membrane (BPM) can have the cation exchange layer (CEL) and the anion exchange layer (AEL) interlocked by double electrospinning.

[0023] The above cation exchange layer (CEL) may form the outer surface of the cylindrical anode membrane (BPM), and the above anion exchange layer (AEL) may form the inner surface of the cylindrical anode membrane (BPM).

[0024] The above-mentioned anode membrane (BPM) may further include a catalyst layer disposed between the cation exchange layer (CEL) and the anion exchange layer (AEL).

[0025] The catalyst layer above may be composed of an organic-inorganic nanocomposite material that aids in water splitting.

[0026]

[0027] A method for manufacturing a self-pH-balancing bipolar membrane according to one embodiment of the present document is a method for manufacturing a bipolar membrane (BPM) used in a microbial electrolysis cell (MEC), comprising: a step of forming an anion exchange layer (AEL) that forms the interior of the cylindrical bipolar membrane (BPM); and a step of forming a cation exchange layer (CEL) that forms the exterior of the cylindrical bipolar membrane (BPM).

[0028] The above cation exchange layer (CEL) and the above anion exchange layer (AEL) can be interlocked with each other by double electrospinning.

[0029] It may further include the step of forming a catalyst layer disposed between the cation exchange layer (CEL) and the anion exchange layer (AEL).

[0030] The catalyst layer above may be composed of an organic-inorganic nanocomposite material that aids in water splitting.

[0031]

[0032] A microbial electrolytic cell according to one embodiment of the present document includes any one of the self-pH-balancing anode membranes described above.

[0033]

[0034] A hydrogen production device according to one embodiment of the present document includes any one of the self-pH-balancing anodic membranes described above.

[0035]

[0036] A resource recovery device according to one embodiment of the present document includes any one of the self-pH-balancing bipolar membranes described above.

[0037]

[0038] An acid-base production device according to one embodiment of the present document includes any one of the self-pH-balancing bipolar membranes described above.

[0039]

[0040] A microbial electrochemical battery according to one embodiment of the present document comprises any one of the self-pH-balancing anode membranes described above.

[0041]

[0042] An e-fuel production device according to one embodiment of the present document includes any one of the self-pH-balancing anodic membranes described above.

[0043] According to one embodiment of the present document, a bipolar membrane (BPM) is OH - Self-balancing of pH can be achieved by this, and by implementing it in a cylindrical shape and forming it by double electrospinning, the interfacial area can be increased, and accordingly, voltage drop and membrane resistance can be reduced.

[0044] In addition, according to one embodiment of the present document, a self pH-balancing bipolar membrane (BPM) can be used in various fields such as microbial electrolytic cells, hydrogen production devices, resource recovery devices, acid-base production devices, etc.

[0045] Furthermore, according to another embodiment of this document, the internal resistance of the stack is reduced by minimizing the distance between the first and second split electrodes (zero-gap structure), allowing hydrogen ions transferred from the ion exchange membrane (anode membrane, etc.) to be utilized directly at the second split electrode. Accordingly, there is an advantage in that energy loss can be minimized due to excellent hydrogen ion concentration and ion transfer properties. Additionally, by installing first and second partition members (cross-shaped partitions) within the intermediate plate (chamber) to fix the ion exchange membrane (separator) in the center, the ion exchange membrane (separator) can be fixed consistently, enabling large capacity and thus allowing for more efficient hydrogen production.

[0046] The effects according to the various embodiments of this document are not limited to those described above, and it is obvious to those skilled in the art that various effects are inherent in this disclosure.

[0047] Figure 1a is a diagram illustrating the process of producing hydrogen from organic waste resources based on microbial electro-fermentation.

[0048] Figure 1b is a diagram illustrating the bioelectric fermentation process.

[0049] Figure 2 is a diagram illustrating a conventional microbial electrolytic cell.

[0050] Figure 3 is a diagram illustrating the hydrogen production operation using a conventional fermentation tank and steam reforming, and the hydrogen production operation using conventional microbial electrolysis technology.

[0051] Figure 4 is a diagram illustrating the operation of P2X (Power to X) using conventional microbial electrochemical technology.

[0052] Figure 5 is a diagram illustrating the technical issues of conventional microbial electrochemical technology.

[0053] Figure 6 is a diagram illustrating a conventional bipolar film.

[0054] Figure 7 is a diagram illustrating a conventional method for manufacturing a bipolar film.

[0055] FIG. 8 is a block diagram illustrating a self-pH-balancing anode membrane according to one embodiment of the present document.

[0056] Figure 9 is a cross-sectional view of the self-pH-balancing bipolar membrane illustrated in Figure 8.

[0057] FIG. 10 is a drawing for explaining the ionomer of a cation exchange layer and the ionomer of an anion exchange layer according to one embodiment of the present document.

[0058] FIG. 11 is a drawing for explaining the material of a catalyst layer according to one embodiment of the present document.

[0059] FIG. 12 is a flowchart illustrating a method for manufacturing a self-pH-balancing anodic membrane according to one embodiment of the present document.

[0060] FIG. 13 is a drawing for explaining an example of a method for manufacturing a self-pH-balancing anodic membrane according to one embodiment of the present document.

[0061] FIG. 14 is a block diagram illustrating a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0062] FIG. 15 is a drawing for illustrating an example of a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0063] FIG. 16 is a drawing for illustrating an example of a positive electrode assembly of a microbial electrolytic cell including a self-pH-balancing positive membrane according to one embodiment of the present document.

[0064] FIG. 17 is a drawing showing an example of implementation of the bipolar membrane electrode assembly illustrated in FIG. 16.

[0065] FIG. 18 shows an example of a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document implemented in the form of a cartridge.

[0066] FIG. 19 is a block diagram illustrating a hydrogen production apparatus including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0067] FIG. 20 is a cross-sectional view of the hydrogen production device illustrated in FIG. 19.

[0068] FIG. 21 is a drawing for illustrating an example of a hydrogen production device including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0069] FIG. 22 is a block diagram illustrating a resource recovery device including a self-pH-balancing bipolar membrane according to one embodiment of the present document.

[0070] FIG. 23 is a cross-sectional view of the resource recovery device illustrated in FIG. 22.

[0071] FIG. 24 is a drawing for illustrating an example of a resource recovery device including a self-pH-balancing bipolar membrane according to one embodiment of the present document.

[0072] FIG. 25 is a block diagram illustrating an acid-base production apparatus including a self-pH-balancing bipolar membrane according to one embodiment of the present document.

[0073] FIG. 26 is a drawing for illustrating an example of an acid-base production device including a self-pH-balancing bipolar membrane according to one embodiment of the present document.

[0074] FIG. 27 is a drawing for illustrating an example of a microbial electrochemical battery including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0075] FIG. 28 is a drawing for illustrating an example of an e-fuel production device including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0076] FIG. 29 is a drawing for illustrating an example of a nitrate production device including a self-pH-balancing anodic membrane according to one embodiment of the present document.

[0077] FIG. 30 is an exploded perspective view of an electrochemical device according to another embodiment of the present document.

[0078] FIG. 31 is a drawing showing the first and second intermediate plates and the first and second partition members of an electrochemical device according to another embodiment of the present document.

[0079] FIG. 32 is a drawing showing a plurality of first and second partition members illustrated in FIG. 31.

[0080] FIG. 33a is a drawing showing first and second intermediate plates equipped with first and second partition members shown in FIG. 31.

[0081] FIG. 33b is a front view of the first and second intermediate plates equipped with the first and second partition members shown in FIG. 31.

[0082] FIG. 34 is a drawing showing first and second divided electrodes according to another embodiment of the present document.

[0083] FIG. 35 is a diagram showing the stacked state of the first and second divided electrodes shown in FIG. 34.

[0084] FIG. 36 is a drawing showing a mesh member according to another embodiment of the present document.

[0085] FIG. 37 is a partial enlarged view showing a divided electrode mounted within a zone according to another embodiment of the present document.

[0086] FIG. 38 is a drawing showing first and second end plates according to another embodiment of the present document.

[0087] FIG. 39 is a drawing showing the state in which the first and second current collectors are mounted on each end plate according to another embodiment of the present document.

[0088] FIG. 40 is a magnified partial view of a part of a mesh member and a current collector according to another embodiment of the present document.

[0089] FIG. 41 is a side view showing the assembled state of an electrochemical device according to another embodiment of the present document.

[0090] FIG. 42 is a schematic diagram illustrating a reaction occurring within an electrochemical apparatus according to another embodiment of the present document.

[0091] FIGS. 43 and 44 are drawings showing the flow path of a fluid flowing inside an intermediate plate in a state where fluid is introduced into an electrochemical device according to another embodiment of the present document.

[0092] FIG. 45 is an exploded perspective view showing an electrochemical device according to another embodiment of the present document.

[0093] FIG. 46 is a schematic diagram showing an electrochemical module using an electrochemical device according to another embodiment of the present document and an electrochemical module using an electrochemical device according to yet another embodiment of the present document.

[0094] Hereinafter, embodiments of this document will be described in detail with reference to the attached drawings. The advantages and features of the embodiments of this document, and the methods for achieving them, will become clear by referring to the details described below in conjunction with the attached drawings. However, the embodiments of this document are not limited to those disclosed below but can be implemented in various different forms, and the embodiments of this document are defined only by the scope of the claims.

[0095] Throughout the specification, the same reference numerals refer to the same components. Unless otherwise defined, all terms used in this specification (including technical and scientific terms) may be used in a meaning commonly understood by those skilled in the art to which the embodiments of this document pertain. Additionally, terms defined in commonly used dictionaries are not to be interpreted ideally or excessively unless explicitly and specifically defined otherwise.

[0096] In this specification, terms such as "first," "second," etc. are used to distinguish one component from another, and the scope of rights shall not be limited by these terms. For example, the first component may be named the second component, and similarly, the second component may be named the first component.

[0097] In this specification, identification symbols (e.g., a, b, c, etc.) for each step are used for convenience of explanation and do not indicate the order of the steps; the steps may occur differently from the specified order unless the context clearly indicates a specific order. That is, the steps may occur in the same order as specified, may be performed substantially simultaneously, or may be performed in the reverse order.

[0098] In this specification, expressions such as “have,” “may have,” “include,” or “may include” refer to the existence of the relevant feature (e.g., a numerical value, function, operation, or component, etc.) and do not exclude the existence of additional features.

[0099]

[0100] With reference to FIGS. 8 to 29, a self-pH-balancing anode membrane and a method for manufacturing the same, a microbial electrolytic cell including the anode membrane, a hydrogen production device, a resource recovery device, and an acid-base production device according to one embodiment of the present document will be described in detail.

[0101]

[0102] A. Self pH-balancing bipolar membrane (BPM)

[0103] First, a self-pH-balancing anodic membrane according to one embodiment of the present document will be described with reference to FIGS. 8 to 11.

[0104] FIG. 8 is a block diagram illustrating a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 9 is a cross-sectional view of the self-pH-balancing anode membrane illustrated in FIG. 8, FIG. 10 is a diagram illustrating an ionomer of a cation exchange layer and an ionomer of an anion exchange layer according to one embodiment of the present document, and FIG. 11 is a diagram illustrating a material of a catalyst layer according to one embodiment of the present document.

[0105] Referring to FIGS. 8 and 9, a self pH-balancing anode membrane (BPM) (10) according to one embodiment of the present document can perform self-balancing of pH.

[0106] To this end, the self-pH-balancing anode membrane (BPM) (10) may include a cation exchange layer (CEL) (11), a catalyst layer (12), and an anion exchange layer (AEL) (13).

[0107] Here, the self-pH-balancing anode membrane (BPM) (10) may be cylindrical. That is, the cation exchange layer (CEL) (11) may form the exterior of the cylindrical self-pH-balancing anode membrane (BPM) (10), and the anion exchange layer (AEL) (13) may form the interior of the cylindrical self-pH-balancing anode membrane (BPM) (10).

[0108] At this time, the self-pH-balancing bipolar membrane (BPM) (10) can have the cation exchange layer (CEL) (11) and the anion exchange layer (AEL) (13) interlocked with each other by double electrospinning.

[0109] And, the cation exchange layer (CEL) (11) can be formed using a CEL ionomer as shown in FIG. 10.

[0110] And, the anion exchange layer (AEL) (13) can be formed using an AEL ionomer as shown in FIG. 10.

[0111] And, the catalyst layer (12) can be placed between the cation exchange layer (CEL) (11) and the anion exchange layer (AEL) (13). Here, the catalyst layer (12) may be made of an organic-inorganic nanocomposite material that aids in water splitting. For example, the catalyst layer (12) may be formed using an organic-inorganic nanocomposite material as shown in FIG. 11. For example, the organic-inorganic nanocomposite material may include CB[6]-Ir composite (CB[6]: (C6H6N4O2)6).

[0112]

[0113] B. Method for manufacturing a self-pH-balancing bipolar membrane (BPM)

[0114] Then, with reference to FIGS. 12 and FIGS. 13, a method for manufacturing a self-pH-balancing anodic membrane according to one embodiment of the present document will be described.

[0115] FIG. 12 is a flowchart for explaining a method for manufacturing a self-pH-balancing anode membrane according to one embodiment of the present document, and FIG. 13 is a diagram for explaining an example of a method for manufacturing a self-pH-balancing anode membrane according to one embodiment of the present document.

[0116] Referring to FIG. 12, an anion exchange layer (AEL) (13) forming the interior of a cylindrical self-pH-balancing anode membrane (BPM) (10) can be formed (S110).

[0117] Then, a catalyst layer (12) can be formed between the cation exchange layer (CEL) (11) and the anion exchange layer (AEL) (13) (S120).

[0118] Here, the catalyst layer (12) may be made of an organic-inorganic nanocomposite material that helps split water.

[0119] Afterwards, a cation exchange layer (CEL) (11) forming the outer surface of a cylindrical self-pH-balancing anode membrane (BPM) (10) can be formed (S130).

[0120] At this time, the cation exchange layer (CEL) (11) and the anion exchange layer (AEL) (13) can be interlocked by double electrospinning. For example, the self-pH-balancing anode membrane (BPM) (10) can be manufactured in a cylindrical shape using double electrospinning for robust interlocking of the ion exchange layers, as shown in FIG. 13. Accordingly, the self-pH-balancing anode membrane (BPM) (10) can increase the interfacial area and thereby reduce the voltage drop and membrane resistance.

[0121]

[0122] C. Microbial electrolysis cell (MEC) containing a self-pH-balancing bipolar membrane (BPM)

[0123] Then, with reference to FIGS. 14 to 18, a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document will be described.

[0124] FIG. 14 is a block diagram for explaining a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 15 is a diagram for explaining an example of a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 16 is a diagram for explaining an example of an anode membrane electrode assembly of a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 17 is a diagram showing an example of implementation of the anode membrane electrode assembly shown in FIG. 16, and FIG. 18 shows an example of a microbial electrolytic cell including a self-pH-balancing anode membrane according to one embodiment of the present document implemented in a cartridge form.

[0125] Referring to FIG. 14, the microbial electrolytic cell (MEC) (20) may include a self-pH-balancing anode membrane (BPM) (10), a reaction chamber (21), an anode electrode (22), and a cathode electrode (23).

[0126] Here, the reaction chamber (21) may be cylindrical.

[0127] And, the anode electrode (22) can be placed in the reaction chamber (21).

[0128] And, the cathode electrode (23) can be positioned opposite the anode electrode (22).

[0129] And, a self-pH-balancing anode membrane (BPM) (10) can be placed between the anode electrode (22) and the cathode electrode (23).

[0130] That is, the microbial electrolytic cell (MEC) (20), as illustrated in FIG. 15, can reduce voltage loss caused by pH imbalance through pH self-balancing and produce high-purity hydrogen separated from the microbial environment. More specifically, a symbiotic relationship between a fermenter and anode-respiring bacteria (ARB) is possible in the oxidation electrode tank into which organic matter is injected. Although the electrolyte becomes acidified due to fermentation and the decomposition of fermentation products, the OH generated through the self-pH-balancing anode membrane (BPM) (10) - Neutralization is possible. This is made possible by continuous current conversion (removal) of organic matter by anode breathing bacteria (ARB), thereby enabling the continuity of the fermentation process. Accordingly, the self-pH-balancing anode membrane (BPM) (10) can increase the current density by 1.7 times, increase the hydrogen production rate by 3.4 times, and increase the COD removal rate by 1.5 times compared to a conventional single-membrane anion exchange membrane (AEM).

[0131] Meanwhile, as shown in FIGS. 16 and 17, the microbial electrolytic cell (MEC) (20) is implemented as a bipolar membrane electrode assembly (BPMEA) consisting of a reduction electrode and a zero gap, thereby minimizing bubble resistance and improving the performance of the microbial electrolytic cell (MEC) (20).

[0132] In addition, the microbial electrolytic cell (MEC) (20) may be implemented in the form of a cartridge, as shown in FIG. 18. That is, by configuring the microbial electrolytic cell (MEC) (20) in the form of a cartridge, replacement can be made easy and the convenience of assembly can be improved.

[0133]

[0134] D. Hydrogen production device including a self-pH-balancing anode membrane (BPM)

[0135] Then, with reference to FIGS. 19 to 21, a hydrogen production apparatus including a self-pH-balancing anodic membrane according to one embodiment of the present document will be described.

[0136] FIG. 19 is a block diagram for explaining a hydrogen production apparatus including a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 20 is a cross-sectional view of the hydrogen production apparatus shown in FIG. 19, and FIG. 21 is a drawing for explaining an example of a hydrogen production apparatus including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0137] Referring to FIGS. 19 and 20, the hydrogen production device (30) may include a self-pH-balancing anode membrane (BPM) (10), a cathode electrode (31), and a bio-anode electrode (32).

[0138] Here, the cathode electrode (31) can be placed inside the self-pH-balancing anode membrane (BPM) (10).

[0139] Additionally, the bio-anode electrode (32) can be placed outside the self-pH-balancing anode membrane (BPM) (10). The bio-anode electrode (32) can be made of electrochemically active bacteria.

[0140] That is, the hydrogen production device (30) can produce high-purity hydrogen and improve the hydrogen production rate through hydrogen ions generated via the self-pH-balancing anode membrane (BPM) (10). Referring to FIG. 21 for a more detailed explanation, the self-pH-balancing anode membrane (BPM) (10) can be configured such that the interior is a cathode electrode and the exterior is a bio-anode electrode composed of electrochemically active bacteria. Hydrogen gas is produced from water splitting on the surface of the cathode electrode, and additionally, high-purity hydrogen can be produced through an increase in hydrogen ions generated after water splitting in the catalyst layer (12) of the self-pH-balancing anode membrane (BPM) (10), thereby improving the hydrogen production rate and efficiency. Furthermore, a low-energy consumption system can be designed by utilizing the bio-anode electrode. In addition, the hydrogen production device (30) may be used in conjunction with renewable energy-linked high-purity, high-efficiency green hydrogen production, decentralized organic waste resource treatment and resource recovery facilities (smart cities, etc.), carbon capture and utilization (CCU) technology, seawater / seawater concentrate treatment technology, seawater desalination, seawater electrolysis, salinity gradient power generation, etc., and seawater-based system utilization technologies. Here, organic waste resources refer to biologically decomposable organic waste such as food waste and agricultural waste, and resources that can be recycled into energy and resources (e.g., three major organic waste resources: food waste, livestock manure, and sewage sludge).

[0141]

[0142] E. Resource recovery device including a self-pH-balancing bipolar membrane (BPM)

[0143] Then, with reference to FIGS. 22 to 24, a resource recovery device including a self-pH-balancing anodic membrane according to one embodiment of the present document will be described.

[0144] FIG. 22 is a block diagram illustrating a resource recovery device including a self-pH-balancing anode membrane according to one embodiment of the present document, FIG. 23 is a cross-sectional view of the resource recovery device illustrated in FIG. 22, and FIG. 24 is a drawing illustrating an example of a resource recovery device including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0145] Referring to FIGS. 22 and 23, the resource recovery device (40) may include a self-pH-balancing anode membrane (BPM) (10), a cation exchange membrane (CEM) (41), a cathode electrode (42), and a bio-anode electrode (43).

[0146] Here, the cation exchange membrane (CEM) (41) can be placed inside the self-pH-balancing anode membrane (BPM) (10).

[0147] And, the cathode electrode (42) can be placed inside the cation exchange membrane (CEM) (41).

[0148] Additionally, the bio-anode electrode (43) can be placed outside the self-pH-balancing anode membrane (BPM) (10). The bio-anode electrode (43) can be made of electrochemically active bacteria.

[0149] That is, the resource recovery device (40) can recover mineral resources such as calcium (Ca) and magnesium (Mg) from seawater or seawater concentrate between the cathode electrode (42) and the cation exchange membrane (CEM) (41). Referring to FIG. 24 for a more detailed explanation, a cation exchange membrane (CEM) (41) can be added inside a self-pH-balancing anode membrane (BPM) (10), so that the innermost chamber is a cathode chamber and the outer chamber is a bio-anode chamber composed of electrochemically active bacteria. In the innermost chamber, a high alkaline environment is created and can be utilized for recovering mineral resources from seawater or seawater concentrate. After resource recovery, the seawater from which polyvalent ions have been removed passes through an intermediate chamber and can be supplied for seawater electrolysis and salinity gradient power generation, etc. Additionally, a low-energy consumption system can be designed through the use of the bio-anode electrode. In addition, the resource recovery device (40) may be used in conjunction with carbon dioxide capture and utilization (CCU) technology, seawater / seawater concentrate CO2 mineralization / resource recovery technology, low energy consumption multivalent ion removal (water softening) technology, pretreatment technology for removing inorganic contamination in seawater-based systems such as seawater desalination, seawater electrolysis, salinity gradient power generation, distributed organic waste resource treatment and resource recovery facilities (smart cities, etc.), renewable energy-linked green hydrogen production technology, etc.

[0150]

[0151] F. Acid-base production device including a self-pH-balancing bipolar membrane (BPM)

[0152] Then, with reference to FIGS. 25 and 26, an acid-base production apparatus including a self-pH-balancing bipolar membrane according to one embodiment of the present document will be described.

[0153] FIG. 25 is a block diagram illustrating an acid-base production apparatus including a self-pH-balancing anode membrane according to one embodiment of the present document, and FIG. 26 is a drawing illustrating an example of an acid-base production apparatus including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0154] Referring to FIG. 25, the acid-base production device (50) may include two self-pH-balancing anode membranes (BPM) (10), a reaction chamber (51), a bio-anode electrode (52), a cathode electrode (53), and a cation exchange membrane (CEM) (54).

[0155] Here, the bio-anode electrode (52) can be made of electrochemically active bacteria.

[0156] And, the cathode electrode (53) can be positioned opposite the bio-anode electrode (52).

[0157] And, two self-pH-balancing anode membranes (BPM) (10) can be placed between the bio-anode electrode (52) and the cathode electrode (53).

[0158] And, a cation exchange membrane (CEM) (54) can be placed between two self-pH-balancing bipolar membranes (BPM) (10).

[0159] That is, the acid-base production device (50) can simultaneously produce acid and base through two self-pH-balancing anode membranes (BPM) (10) and a cation exchange membrane (CEM) (54). Referring to FIG. 26 for a more detailed explanation, by adding a cation exchange membrane (CEM) (54) between two self-pH-balancing anode membranes (BPM) (10), acid and basic chemicals can be simultaneously produced, and additionally, high-purity hydrogen can be produced. Furthermore, a low-energy consumption system can be designed by utilizing a bio-anode electrode. In addition, the acid-base production device (50) may be used in conjunction with low-energy consumption acid and base production technology, pretreatment technology for removing inorganic and organic contaminants in seawater-based systems such as seawater desalination, seawater electrolysis, and salinity gradient power generation utilizing acid and base, distributed organic waste resource treatment and resource recovery facilities (smart cities, etc.), and renewable energy-linked green hydrogen production technology.

[0160]

[0161] G. Microbial electrochemical battery including a self-pH-balancing bipolar membrane (BPM)

[0162] Then, with reference to FIG. 27, a microbial electrochemical battery including a self-pH-balancing anode membrane according to one embodiment of the present document will be described.

[0163] FIG. 27 is a drawing for illustrating an example of a microbial electrochemical battery including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0164] Referring to FIG. 27, a microbial electrochemical battery (MEB) including a self-pH-balancing anode membrane (BPM) (10) is composed of a microbial electrolysis cell (MEC) and a microbial fuel cell (MFC), and can perform charging (additional external power injection) and discharging (electricity production) operations as follows.

[0165] - Charging: (Left) Bio anode / acetate consumption vs. (Right) Bio cathode: CO2 and H2 + Reduces to produce acetic acid

[0166] - Discharge: (Right) Bio anode / acetate consumption vs. (Left) Bio cathode CO2 and H2 + Reduces to produce acetic acid

[0167] Furthermore, the purpose of the MEC-MFC charge / discharge system is to establish a sustainable energy-resource circulation system by utilizing CO2 and organic matter as resources through electrochemical energy conversion, producing high-value compounds (e.g., acetic acid) through charging (MEC), and recovering energy (electricity production) through discharging (MFC). In addition, in the microbial electrochemical battery (MEB), the positive membrane (BPM) utilizes electrons generated from the microbial electrode to [distribute] the H of both electrolytes. + (Proton) and OH -It plays an important role in maintaining acidic and alkaline conditions by separating (hydroxide ions). In addition, conventional electrochemical processes utilizing anode membranes (BPM) require additional voltage for water splitting, resulting in high energy consumption; however, in the process according to one embodiment of this document, an auxiliary voltage can be additionally used through the electrochemical activity of microorganisms, making a low-energy consumption process possible. Furthermore, it is possible to form a tube-shaped membrane or to utilize a conventional flat membrane structure by assembling it into a tube shape.

[0168]

[0169] H. e-fuel production device including a self-pH-balancing bipolar membrane (BPM)

[0170] Then, with reference to FIG. 28, an e-fuel production apparatus including a self-pH-balancing anodic membrane according to one embodiment of the present document will be described.

[0171] FIG. 28 is a drawing for illustrating an example of an e-fuel production device including a self-pH-balancing anode membrane according to one embodiment of the present document.

[0172] Referring to FIG. 28, an e-fuel production device including a self-pH-balancing anode membrane (BPM) (10) supplies CO2 generated from the MEC-BPM Bio-anode to the reduction electrode section, thereby enabling the production of liquid and gaseous chemicals with various C, H, and O compositions. In other words, the e-fuel production device is a low-energy consumption system utilizing a Bio-anode, capable of performing carbon resource recovery (reuse). At this time, the liquid fuel has the advantage of being easy to store, and the gaseous fuel can be applied in various ways, such as the main components of natural gas.

[0173] In addition, low-energy consumption CO2 resource recovery technology can be developed through the e-fuel production device, and the e-fuel production device can be utilized in distributed organic waste resource treatment and recovery facilities (such as smart cities), and renewable energy-linked carbon resource recovery facilities. Furthermore, the Tubular BPM-MEC structure can be utilized. Also, it is configured in a cartridge form, making replacement easy and offering excellent assembly capabilities. Additionally, it is possible to produce a tubular membrane or to utilize existing flat membrane structures by assembling them into a tubular form.

[0174]

[0175] I. Nitrate production device including a self-pH-balancing bipolar membrane (BPM)

[0176] Then, with reference to FIG. 29, a nitrate production apparatus including a self-pH-balancing anodic membrane according to one embodiment of the present document will be described.

[0177] FIG. 29 is a drawing for illustrating an example of a nitrate production device including a self-pH-balancing anodic membrane according to one embodiment of the present document.

[0178] Referring to FIG. 29, a nitrate production device including a self-pH-balancing anode membrane (BPM) (10) can sequentially precipitate / separate / recover ions according to the pH of the inorganic salt solution and ultimately improve the purity of the nitrate. That is, the inorganic salt recovery mechanism according to pH and the applications of nutrients / inorganic salts are as follows.

[0179] ≥ pH 8.5-9.5 : Mg 2+ + NH4 + + PO4 3- + 6H2O ⇔ MgNH4PO46H2O - Inorganic salt / Fertilizer

[0180] ≥ pH 9 : Ca 2+ + CO2 + H2O ⇔ CaCO3 + 2H + - Inorganic salt

[0181] ≥ pH 10 : Mg 2+ + 2OH- ⇔ Mg(OH)2- inorganic salt / fertilizer

[0182] In addition, the development of a highly selective nitrate conversion anode can improve nitrate yield (conventional: Pt-based, strategic: non-precious metals, etc.). Through this, it can be utilized for the fertilization of nutrients in agriculture, fisheries, and livestock farming.

[0183]

[0184]

[0185] Then, with reference to FIGS. 30 to 46, an electrochemical device capable of increasing capacity (large area) and an electrochemical module using the same according to another embodiment of the present document will be described in detail.

[0186] Another embodiment of this document relates to an electrochemical device capable of large capacity (large area) and an electrochemical module using the same.

[0187] In particular, according to another embodiment of this document, the invention relates to an electrochemical device capable of producing hydrogen more effectively using microbial electrochemical technology and an electrochemical module utilizing the same, as it can be utilized as a hydrogen production device capable of recovering energy from organic waste resources using electrochemically active bacteria.

[0188] In addition, according to another embodiment of the present document, the invention relates to an electrochemical device capable of increasing the capacity of at least one of an energy conversion device including a fuel cell and a water electrolysis device, an energy storage device including a battery and a capacitor, an electrochemical reaction device, a wastewater treatment and resource recovery device, an electrochemical bioreactor including a microbial electrochemical device, an electrochemical desalination device including an electrodialysis device, a carbon dioxide conversion device, a metal electrodeposition and resource recovery device, a reverse electrodialysis device, and a microbial reverse electrodialysis electrolysis device, and an electrochemical module using the same.

[0189] FIG. 30 is an exploded view of an electrochemical device (10) according to another embodiment of the present document, in particular a hydrogen production device (10, hereinafter referred to as a 'hydrogen production device') using organic waste resources.

[0190] Referring to FIG. 30, an electrochemical device (10) according to another embodiment of the present invention comprises: an ion exchange membrane (100) having a first surface (101) and a second surface (102) opposite to the first surface (101); a first intermediate plate (200a) having a first mounting space (210a) mounted with a plurality of first split electrodes (300a) positioned to face the first surface (101); a first end plate (500a) positioned to surround the first mounting space (210a); a second intermediate plate (200b) having a second mounting space (210b) mounted with a plurality of second split electrodes (300b) having different polarity from the first split electrodes (300a) positioned to face the second surface (102); and a second end plate (500b) positioned to surround the second mounting space (210b).

[0191] A gasket (110) may be disposed between the ion exchange membrane (100) and the first intermediate plate (200a) and between the ion exchange membrane (100) and the second intermediate plate (200b), respectively.

[0192] In addition, although not shown, a gasket may be placed between each end plate and the intermediate plate.

[0193] Here, the ion exchange membrane (100) may include a bipolar membrane, a cation exchange membrane, an anion exchange membrane, or a porous composite membrane. It is not limited thereto, and various types of separators used in electrochemical devices may be applied.

[0194] In the following, the configuration of an electrochemical device using an anode membrane as the ion exchange membrane (100) is described, but it should be understood that not only an anode membrane but also various other ion exchange membranes or separation membranes described above can be applied.

[0195] Additionally, in other embodiments of this document, terms such as ion exchange membrane (100), anode membrane (100), and separator (100) may be used interchangeably.

[0196] Specifically, the anode membrane (100) is composed of a cation exchange layer and an anion exchange layer, and when current is applied to the anode electrode and the cathode electrode, water decomposition, i.e., H2O, occurs at the junction of the cation exchange layer and the anion exchange layer. + Wow OH - It is a membrane that is decomposed and through which cations and anions cannot move through the anode membrane (100).

[0197] The anion exchange layer of the above-mentioned anode membrane (100) may be positioned to face the first split electrode (300a), and the cation exchange layer may be positioned to face the second split electrode (300b).

[0198] The first surface (101) of the above ion exchange membrane (100) may face the first split electrode (300), and the second surface (102) may face the second split electrode (300).

[0199] FIG. 31 is a drawing showing first and second intermediate plates (200a, 200b) and first and second partition members (230a, 230b) of an electrochemical device (10) according to another embodiment of the present document; FIG. 32 is a drawing showing a plurality of first and second partition members (230a, 230b) shown in FIG. 31; FIG. 33a is a drawing showing first and second intermediate plates (200a, 200b) equipped with first and second partition members shown in FIG. 31; FIG. 33b is a front view of first and second intermediate plates equipped with first and second partition members shown in FIG. 31.

[0200] The first and second intermediate plates (200a, 200b) have the same structure and configuration. In addition, the first and second partition members (230a, 230b) have the same structure and configuration.

[0201] Referring to FIGS. 31 to 33, the first intermediate plate (200a) includes a first surface (201), a second surface (202) opposite to the first surface, and a side (203) connecting the first surface (201) and the second surface (202), and has a first mounting space (210a) formed by penetrating at least a portion of the first surface and the second surface.

[0202] The first intermediate plate (200a) includes a plurality of first partition members (230a) for partitioning the first mounting space (210a) into a plurality of zones (S1).

[0203] Each of the above first divided electrodes (300a) can be supported by the first partition member (230a).

[0204] The second intermediate plate (200b) includes a first surface (201), a second surface (202) opposite to the first surface, and a side (203) connecting the first surface (201) and the second surface (202), and has a second mounting space (210b) formed by penetrating at least a portion of the first surface and the second surface.

[0205] The second intermediate plate (200b) includes a plurality of second partition members (230b) for partitioning the second mounting space (210b) into a plurality of zones (S2).

[0206] Each of the above second divided electrodes (300b) can be supported by a second partition member (230b).

[0207] The first and second mounting spaces (210a, 210b) may each be provided with a predetermined first length (L1) along the width direction (W) of the first and second intermediate plates (200a, 200b) and a predetermined second length (L2) along the length direction (L).

[0208] The first partition member (230a) may be detachably mounted to the first intermediate plate (200a) or formed integrally with the first intermediate plate (200a).

[0209] The second partition member (230b) may be detachably mounted to the second intermediate plate (200b) or formed integrally with the second intermediate plate (200b).

[0210] Each of the above plurality of first and second partition members (230a, 230b) can be formed to extend along the longitudinal direction.

[0211] The plurality of first partition members (230a) each include one or more horizontal partition members (231a, which may be referred to as the 'first horizontal partition member') and vertical partition members (232a, which may be referred to as the 'first vertical partition member').

[0212] The above one or more horizontal partition members (231a) and vertical partition members (232a) may be arranged to intersect each other within the first mounting space (210a).

[0213] The plurality of second partition members (230b) each include one or more horizontal partition members (231b, which may be referred to as 'second horizontal partition member') and vertical partition members (232b, which may be referred to as 'second vertical partition member').

[0214] The above one or more horizontal partition members (231b) and vertical partition members (232b) may be arranged to intersect each other within the second mounting space (210b).

[0215] Each of the first and second partition members (230a, 230b) includes a protrusion (237) provided to be fitted into the first and second intermediate plates (200a, 200b).

[0216] Here, the protrusion (237) formed on the first partition member (230a) may be referred to as the first protrusion, and the protrusion (237) formed on the second partition member (230b) may be referred to as the second protrusion.

[0217] The above protrusion (237) may be provided to protrude from both ends of each partition member (230a, 230b), that is, the horizontal partition member and the vertical partition member, to form a predetermined step along the height direction (H) so as to be secured by being caught.

[0218] The first and second intermediate plates (200a, 200b) may each be provided with a groove (220) into which a protrusion (237) is fitted.

[0219] The above protrusion (237) and the groove (220) can be provided in corresponding shapes so as to be fitted together.

[0220] Here, the groove (220) formed in the first intermediate plate (200a) may be referred to as the first groove, and the groove (220) formed in the second intermediate plate (200b) may be referred to as the second groove.

[0221] The above-mentioned groove (220) may be spaced apart at a predetermined interval along the circumferential direction of the inner surface of each of the first and second mounting spaces (210a, 210b).

[0222] In particular, the above-mentioned groove (220) may be provided to correspond to the number of one or more horizontal partition members (231a, 231b) and vertical partition members (232a, 232b).

[0223] In addition, the first and second partition members (230a, 230b) each include a fitting groove (239) for fixing each other when arranged to intersect each other.

[0224] Here, the fitting groove (239) formed in the first partition member (230a) may be referred to as the first fitting groove, and the fitting groove (239) formed in the second partition member (230b) may be referred to as the second fitting groove.

[0225] The above-mentioned fitting grooves (239) may be provided in multiple numbers at a predetermined distance from each other along the longitudinal direction of each partition member.

[0226] In particular, the fitting groove (239) of the horizontal partition member (231a, 231b) may be provided on the lower side with respect to the height direction (H), and the fitting groove (239) of the vertical partition member (232a, 232b) may be provided on the upper side with respect to the height direction (H).

[0227] When the horizontal and vertical partition members intersect each other and their respective fitting grooves are fitted and fixed, the height (H) is equal to the height (H) of each partition member, thereby allowing for the formation of multiple zones (S1, S2).

[0228] The thickness (T) of the side of the first and second intermediate plates (200a, 200b) may be the same as the height (H) of the first and second partition members (230a, 230b).

[0229] The first and second partition members (230a, 230b) each have a passage (235) that fluidly connects two adjacent zones.

[0230] Each of the horizontal section member (231a) and the vertical section member (232a) of the first section member (230a) is arranged at a predetermined interval along the longitudinal direction and has a plurality of passages (235, which may be referred to as 'first passages') that are penetrated to allow fluid movement.

[0231] Likewise, each of the horizontal section member (231b) and the vertical section member (232b) of the second section member (230b) is arranged at a predetermined interval along the longitudinal direction and has a plurality of passages (235, which may be referred to as 'second passages') that are penetrated to allow fluid movement.

[0232] In addition, when the protrusions (237) of the first and second partition members (231a, 231b) are fitted and assembled into the groove (220), the length (L3) of the horizontal partition members (231a, 231b) of the first and second partition members is the same as the width direction length (L1) of the first and second mounting spaces (210a, 210b), and the length (L4) of the vertical partition members (232a, 232b) is the same as the length direction length (L2) of the first and second mounting spaces (210a, 210b).

[0233] As described above, first and second divided electrodes (300a, 300b) are respectively disposed inside the plurality of zones (S1, S2) formed in the first and second mounting spaces (210a, 210b) by the first and second partition members (231a, 231b).

[0234] In addition, according to another embodiment of the present document, the first intermediate plate (200a) has a plurality of zones (S1) located at the edge of the first mounting space (210a) and a plurality of first flow holes (240a) each provided to be fluidly movable.

[0235] Additionally, the second intermediate plate (200b) has a plurality of zones (S2) located at the edge of the second mounting space (210b) and a plurality of second flow holes (240b) each provided to be fluidly movable.

[0236] Each of the plurality of first and second flow holes (240a, 241b) may be formed as a fluid passage having an inlet and an outlet formed by penetrating at least a portion of the side area to allow fluid movement, with a plurality of zones located at the edge of each mounting space. The plurality of first flow holes (240a) and second flow holes (240b) may be arranged at a predetermined interval on each side (2031, which may be referred to as the 'first side') along the longitudinal direction of each intermediate plate, and may be arranged in the central area of ​​each zone.

[0237] That is, a plurality of first flow holes (240a) and second flow holes (240b) can be placed in each of the central regions of each section (lengthwise edge section) partitioned along the edge along the lengthwise direction (L) of the intermediate plate.

[0238] The uppermost and lowermost flow holes among the plurality of first flow holes (240a) and second flow holes (240b) provided on the first side include a plurality of branch holes (241a, 241b) that are extended along each side (2032, which may be referred to as the 'second side') following the width direction of each intermediate plate and branched to each zone side.

[0239] That is, a plurality of branch holes (241a, 241b) disposed on the second side (2032) can be fluidly connected to each section (edge ​​section in the width direction) partitioned along the edge following the width direction (W) of the intermediate plate.

[0240] Here, the flow hole formed at the top may be referred to as the upper flow hole (2401a, 2401b) and the flow hole formed at the bottom may be referred to as the lower flow hole (2402a, 2402b).

[0241] Each of the upper and lower flow holes is formed by penetrating at least a portion of the first side and extending along the width direction, and is provided with a plurality of branch holes (241a, 241b) branched toward each respective area. Accordingly, a fluid inlet is formed on the first side, and an outlet can be formed on the inner side of the second side where the branch holes are formed.

[0242] For example, as shown in FIG. 33, two branch holes may be provided that are fluidly connected to each zone formed at the edge in the width direction of the intermediate plate, and one flow hole may be provided that is fluidly connected to the center area of ​​each zone formed at the edge in the length direction, but is not limited thereto, and the number of flow holes and branch holes may be appropriately selected and formed according to the length and width directions of the intermediate plate.

[0243] The first intermediate plate (200a) may include a first storage unit (not shown) for supplying a fluid (e.g., organic waste resources, a first inflow solution) to a first mounting space (210a) in which a first split electrode is disposed.

[0244] The first storage unit may be fluidly connected to one or more selected flow holes among the first flow holes (240a). Here, the one or more flow holes (which may be referred to as the first inlet flow holes) fluidly connected to the first storage unit may be the bottom flow holes (2402a) formed at the bottom.

[0245] The above-mentioned first storage unit can be connected to receive a fluid (first effluent solution) discharged through the first mounting space.

[0246] That is, the first storage unit may be fluidly connected to one or more of the first flow holes (which may be referred to as the first outflow flow hole) among the remaining first flow holes, excluding the first inflow flow hole of the first intermediate plate. Here, the first outflow flow hole may be the upper flow hole (2401a) formed at the uppermost part of the first intermediate plate.

[0247] That is, the first inflow solution supplied from the first storage unit is supplied through the first inflow flow hole, and the first outflow solution can flow to the first storage unit by passing through the first mounting space (210a) and being discharged through the first outflow flow hole. Here, the first outflow solution discharged through the first outflow flow hole may contain gases generated by a reaction within the first mounting space (210a), such as hydrogen, carbon dioxide, or methane, and the gases contained in the first storage unit can be utilized as resources by separating the gas and liquid as needed.

[0248] Likewise, the second intermediate plate (200b) may include a second storage unit (not shown) for supplying a fluid (e.g., an electrolyte for hydrogen production, a second inflow solution) to a second mounting space (210b) in which a second split electrode is disposed.

[0249] The second storage unit may be fluidly connected to one or more selected flow holes among the second flow holes (240b). Here, the one or more flow holes (which may be referred to as second inlet flow holes) fluidly connected to the second storage unit may be lower flow holes (2402b) formed at the lowest end of the second intermediate plate.

[0250] The above second storage unit can be connected to receive a fluid (second effluent solution) discharged through the second mounting space.

[0251] That is, the second storage unit may be fluidly connected to one or more second flow holes (which may be referred to as second outflow flow holes) among the remaining second flow holes, excluding the second inflow flow hole of the second intermediate plate. Here, the second outflow flow hole may be an upper flow hole (2401a) formed at the uppermost part of the second intermediate plate.

[0252] That is, the fluid supplied from the second storage unit is supplied through the second inlet flow hole, passes through the second mounting space (210b), and is discharged through the second outlet flow hole to flow into the second storage unit. Here, the discharged water (second outlet solution) discharged through the second outlet flow hole may contain a gas, for example, high-purity (99% or higher) hydrogen, generated by a reaction within the second mounting space (210b), and the gas contained in the second storage unit can be utilized as a resource by gas-liquid separation.

[0253] Each of the above first and second storage units may be a storage tank having a sealed predetermined space.

[0254] In addition, a first partition member (230a) is mounted on the first intermediate plate (200a) to form a plurality of zones (S1), and a second partition member (230b) is mounted on the second intermediate plate (200b) to form a plurality of zones (S2), thereby supporting an ion exchange membrane (100) disposed between the first intermediate plate (200a) and the second intermediate plate (200b). That is, each partition member can fix the ion exchange membrane (100) at a constant level from both sides with the ion exchange membrane (100) in between.

[0255] In existing large-area microbial electrolysis cells (MECs), there was a problem in that the membrane (100) could not be fixed evenly, and there was a problem in that it was difficult to control the flow rate of both chambers during long-term continuous operation.

[0256] Accordingly, according to another embodiment of the present document, a cross-shaped partition (first and second partition members) for fixing the ion exchange membrane (anode membrane / separator) in the center is installed within the chamber (intermediate plate), thereby providing the effect of fixing the ion exchange membrane (anode membrane) consistently.

[0257] In particular, within each zone (S1, S2), the effect of fixing the ion exchange membrane (anode) can be maximized by applying constant pressure in the direction of the ion exchange membrane (anode) from both electrodes (first split electrode and second split electrode) within the zero-gap structure.

[0258] In addition, referring to FIG. 33b, the first and second intermediate plates (200a, 200b) may include one or more connecting members (280) for circulating fluid introduced into each zone (S1, S2).

[0259] The above connecting member (280) can optionally connect two flow holes (240a) formed on the first side in a fluidly movable manner as needed. (Indicated by the dotted line in FIG. 33b)

[0260] FIG. 34 is a drawing showing first and second divided electrodes (300a, 300b) according to another embodiment of the present document, FIG. 35 is a drawing showing the first and second divided electrodes (300a, 300b) shown in FIG. 34 in a stacked state, FIG. 36 is a drawing showing a mesh member according to another embodiment of the present document, and FIG. 37 is a partial enlarged view showing a divided electrode mounted within a zone according to another embodiment of the present document.

[0261] First, the first split electrode (300a) and the second split electrode (300b) have different polarities, but their structure and configuration may be the same.

[0262] Each of the first split electrodes (300a) may be an anode electrode, and each of the second split electrodes (300b) may be a cathode electrode.

[0263] Conversely, each of the first split electrodes (300a) may be a cathode electrode, and each of the second split electrodes (300b) may be an anode electrode.

[0264] For example, if the first split electrode (300a) is an anode electrode, electrochemically active microorganisms can be cultured on the surface of the anode electrode accommodated in each section (S1) of the first intermediate plate. The electrochemically active microorganisms form a biofilm on the surface of the anode electrode to decompose organic waste resources supplied from the outside, such as livestock wastewater, food wastewater, alcohol wastewater, industrial and domestic wastewater, etc. When the generated electrons are sent to the anode electrode, they move to the cathode electrode (second split electrode) electrically connected to the anode electrode, where the reduction of hydrogen ions occurs at the cathode electrode to generate hydrogen gas.

[0265] (A) of FIG. 34 shows a first divided electrode (300a) and a second divided electrode (300b) of a first type, and (B) shows a first divided electrode (300a) and a second divided electrode (300b) of a second type.

[0266] As shown in (A) of FIG. 34, the first and second divided electrodes (300a, 300b) of the first type may each be composed of a flat electrode having a predetermined thickness, and as shown in (B), may be composed of a plurality of electrode penetration holes (310) that penetrate the electrode to allow fluid to flow through, having a predetermined thickness.

[0267] The first and second divided electrodes (300a, 300b) are each composed of a flat electrode having a predetermined first thickness or an electrode having an electrode through hole, so that one electrode can be inserted into each section (S1, S2), and each is composed of a flat electrode having a second thickness thinner than the first thickness or an electrode having an electrode through hole, so that a plurality of them can be stacked and inserted into each section (S1, S2).

[0268] Referring to FIGS. 34 to 37, the first and second divided electrodes (300a, 300b) of the first type can be stacked and arranged in multiple numbers within each section (S1, S2).

[0269] The first and second split electrodes (300a, 300b) of the second type above can be stacked and arranged in multiple numbers within each zone (S1, S2).

[0270] Accordingly, each of the first and second divided electrodes (300a, 300b) may include one selected from a flat electrode (first type electrode, 3001a, 3001b) and an electrode having a plurality of electrode through holes (310) (second type electrode, 3002a, 3002b), and in each section, a flat electrode or an electrode having a plurality of electrode through holes (310) may be selectively stacked and arranged.

[0271] In addition, when a fluid flows into each zone while a plurality of electrodes with a plurality of electrode penetration holes (310) formed as described above are stacked and inserted into each zone, the contact area with the fluid is increased as the fluid passes through the electrode penetration holes (310), thereby enabling more effective production of the product when electrochemically active microorganisms are cultured on the electrode surface described later. That is, large-scale production can be achieved more easily.

[0272] When a flat electrode or an electrode having a plurality of electrode through holes (310) is stacked and arranged in each of the above sections (S1, S2), a mesh member may be inserted between two selected adjacent electrodes.

[0273] For example, referring to FIG. 35, a plurality of electrodes of the first type (first and second divided electrodes) may be stacked as in (A), or a plurality of electrodes of the second type (first and second divided electrodes) may be stacked as in (B).

[0274] In particular, when each electrode is stacked, a mesh member (400) can be inserted between two selected adjacent electrodes. This has the effect of making the flow of fluid flowing in toward the side smoother.

[0275] For example, when four first-type electrodes are stacked, a mesh member (400) may be placed between two stacked electrodes and two stacked electrodes, but is not limited thereto and may be placed between two selected adjacent electrodes as needed.

[0276] Additionally, when four second-type electrodes are stacked, a mesh member (400) may be placed between two stacked electrodes, but is not limited thereto, and may be placed between two selected adjacent electrodes as needed.

[0277] As described above, the mesh member (400) placed between the stacked electrodes forms a gap (g) between two adjacent electrodes, thereby facilitating the flow of fluid entering from the upper, lower, left, and right sides, and enabling the production of the product to be more effective.

[0278] Additionally, each zone (S1) formed by the first section member (230a) includes a mesh member (400) disposed between the first end plate (500a) and the first section electrode (300a) to support the first section electrode (300a) inserted into the zone.

[0279] In particular, by forming multiple passages in each partition member to facilitate the flow of fluid entering from the side, the partition member supports multiple divided electrodes while simultaneously enabling smoother fluid flow. (See FIG. 37)

[0280] Likewise, each zone (S2) formed by the second section member (230b) includes a mesh member (400) disposed between the second end plate (500b) and the second section electrode (300b) to support the second section electrode (300b) inserted into the zone.

[0281] Specifically, referring to FIG. 36, a mesh member (400) according to another embodiment of the present document includes a first type of mesh member (401) and a second type of mesh member (402).

[0282] The first type of mesh member (401) has a through hole (410) having a predetermined diameter in the center.

[0283] The mesh member (402) of the second type above is not provided with a through hole (410).

[0284] The first type of mesh member (401) above may be positioned between the first end plate (500a) and the first split electrode (300a) and inserted into each zone (S1), and may be positioned between the second end plate (500b) and the second split electrode (300b) and inserted into each zone (S2).

[0285] The second type of mesh member can be placed between the electrodes or between the first split electrode (300a) and the ion exchange membrane (100).

[0286] FIG. 38 is a drawing showing first and second end plates (500a, 500b) according to another embodiment of the present document, and FIG. 39 is a drawing showing the state in which first and second current collectors are mounted on each end plate according to another embodiment of the present document.

[0287] Referring to FIGS. 38 and 39, the first and second end plates (500a, 500b) each have a first surface (501) facing the ion exchange membrane (100), a second surface (502) opposite to the first surface, and a side (503) connecting the first surface (501) and the second surface (502).

[0288] The first end plate (500a) has a plurality of first through holes (510a) facing each section (S1) of the first mounting space (210a), and a first current collector (530a) is mounted in each of the first through holes (510a), and the first current collector (530a) can be provided to be electrically connected to each of the first split electrodes (300a).

[0289] The second end plate (500b) has a plurality of second through holes (510b) facing each section (S2) of the second mounting space (210b), and a second current collector (530b) is mounted in each second through hole (510b), and the second current collector (530b) can be provided to be electrically connected to each of the second split electrodes (300b).

[0290] Specifically, each of the first and second through holes (510a, 510b) may be through holes formed by penetrating the first surface and the second surface, and each through hole may be provided at a position corresponding to the center area of ​​each zone (S1, S2).

[0291] A first fastening part (512) may be provided on the inner surface of each of the above-mentioned through holes (510a, 510b) so that each current collector is spirally connected.

[0292] The first fastening part (512) above may be formed with screw threads.

[0293] The first and second current collectors (530a, 530b) each include a current collector (531), a cap (533), and a fixing member (535).

[0294] Specifically, the first and second current collectors (530a, 530b) each have an insertion hole (532) into which a current collector (531) is inserted, and each includes a cap (533) inserted into each through hole (510a, 510b) and a fixing member (535) provided to fix the current collector inserted into the cap (533).

[0295] Each of the above-mentioned collectors (531) has a head portion (5311) that contacts the first divided electrode (300a) and the second divided electrode (300b), respectively, and a body portion (5313) that extends from the head portion (5311) and has at least a portion of its area inserted into the insertion hole (532) of the cap (533).

[0296] Each head portion (5311) of the above-mentioned collector (531) has a protrusion (5315) that is inserted into a through hole (410) provided in the mesh member (401).

[0297] The above cap (533) may be provided with a second fastening part (534) to be fastened to the first fastening part (512) of the through hole (510a, 510b) of the end plate, provided in at least a portion of the outer surface. The second fastening part (534) may be at least a portion of a predetermined length provided on the end side of the cap (533).

[0298] The second fastening part (534) above may be formed with screw threads that can be screw-coupled with the first fastening part.

[0299] The above cap (533) includes a third fastening part (5321) formed on the inner circumference of the insertion hole (532) and fastened to the current collector. The third fastening part (5321) may be formed as a screw thread.

[0300] The above cap (533) includes a fifth fastening part (5323) formed on the inner circumference of the other end side and fastened to a fixing member (535). The fifth fastening part (5323) may be formed with screw threads.

[0301] At least a portion of the body portion (5313) of the above-mentioned collector (531) includes a fourth fastening portion (5312) that is inserted into the insertion hole (532) of the cap (533) and screw-coupled with the third fastening portion (5321). The fourth fastening portion (5312) may be formed with screw threads to enable screw-coupled with the third fastening portion. The fourth fastening portion (5312) may be formed with screw threads having a predetermined length extending from one end of the body portion (5313) toward the other end.

[0302] The fourth fastening portion (5312) of each of the first and second current collectors is provided to adjust the depth of insertion into the third fastening portion (5321), thereby adjusting the insertion depth of the fourth fastening portion (5312) to control the pressure applied to the mesh member and / or the split electrode side. By doing so, a zero-gap structure can be formed so that the first split electrode, the ion exchange membrane, and the second split electrode are in close contact with each other.

[0303] The above fixing member (535) may be provided to fix the contact between the current collector (531) and each divided electrode, and specifically, the head portion (5311) of the current collector may be provided to further improve the contact with each mesh member (400). It may also be coupled to the other end of the cap (533).

[0304] The above fixing member (535) may be provided to fix the insertion depth at which each current collector is fastened.

[0305] The above fixing member (535) may be provided to penetrate the interior, and the other end of the body portion (5313) of the current collector may be fixed so as to pass through the interior of the fixing member (535) and be exposed to the outside.

[0306] The above-mentioned fixing member (535) may be provided with a sixth fastening part (5351) arranged to be spirally coupled with the fifth fastening part (5323) of the cap (533). The sixth fastening part (5351) may be provided in at least a portion of the end portion of the fixing member (535) and formed with a screw thread capable of spirally coupling with the fifth fastening part.

[0307] The fourth fastening part (5312) of the above-mentioned current collector (531) can be mounted by adjusting the insertion depth into the third fastening part (5321), thereby applying further pressure toward the mesh member (401) or electrode side to improve contact.

[0308] The head portion (5311) may be provided as a circular plate, and contact can be improved by applying further pressure toward the mesh member (401) or electrode side by an area of ​​the head portion (5311).

[0309] FIG. 40 is a magnified partial view of a portion of a mesh member (401) and a current collector (531) according to another embodiment of the present document.

[0310] Referring to FIG. 40, as shown in (B) of FIG. 40, the head portion (5311) of the current collector (531) of the first and second current collectors (500a, 500b) is provided to have a predetermined first diameter (R1), and the protrusion (5315) formed by extending from the head portion (5311) may be provided to have a second diameter (R2) smaller than the first diameter (R1).

[0311] Accordingly, the through hole (410) of the mesh member (401) into which the protrusion (5315) is inserted may be provided to have a third diameter (R3) larger than the second diameter (R2). (R1 <R3<R2)

[0312] As described above, by adjusting the size of the through hole of the mesh member, the head portion of the current collector, and the diameter of the protrusion, the protrusion of the current collector is inserted into the through hole of the mesh member to fix the mesh member, and the head portion presses the mesh member with an area equal to the wide diameter, thereby further fixing the divided electrode and simultaneously making close contact with the ion exchange membrane (anode membrane), so that the gap that may be formed between the ion exchange membrane (anode membrane) and the electrode is eliminated or reduced, thereby forming a zero gap.

[0313] In particular, by adjusting the insertion depth of the fourth fastening part of the current collector into the third fastening part of the cap and sequentially pressing the mesh member and the electrode, the gap can be further eliminated, thereby enabling the formation of a zero gap.

[0314] An electrochemical device (10) according to another embodiment of the present document having the above configuration can be utilized as a hydrogen production device for generating hydrogen.

[0315] FIG. 41 is a side view showing the assembled state of an electrochemical device (10) according to another embodiment of the present document, and FIG. 42 is a schematic diagram showing the reaction occurring within the electrochemical device (10) according to another embodiment of the present document.

[0316] Referring to FIGS. 30, 41 and 42, a first end plate (500a), a first intermediate plate (200a), an anode film (100), a second intermediate plate (200b), and a second end plate (500b) can be arranged and assembled in sequence.

[0317] Here, a first partition member (230a) is mounted inside the first intermediate plate (200a) to form a plurality of zones (S1), and within each zone (S1), a mesh member (401), a first split electrode (200a), and a mesh member (402) can be arranged and assembled in sequence.

[0318] Additionally, a second partition member (230b) is mounted inside the second intermediate plate (200b) to form a plurality of zones (S2), and a second split electrode (200b) and a mesh member (401) can be arranged and assembled in sequence within each zone (S2).

[0319] In particular, a mesh member (400) disposed adjacent to the first end plate (500a) and the second end plate (500b) is disposed with a mesh member (401) having an electrode through hole (310). At this time, each of the first current collector (530a) and the second current collector (530b) disposed facing each other is fastened to the first and second end plates (500a, 500b) respectively, and as they press each of the mesh members (401), a zero gap can be formed between the electrode and the anode film.

[0320] Here, the mesh member (400) may be a titanium mesh (Ti-mesh), but is not limited thereto. Additionally, the first split electrode may be an anode electrode in which electrochemically active microorganisms are cultured, and the second split electrode may be a cathode electrode.

[0321] Additionally, if the first split electrode is an anode electrode in which electrochemically active microorganisms are cultured, mesh members may be placed on both sides with the anode electrode in between; however, if the anode electrode is a metal electrode, mesh members (402) between the first split electrode and the ion exchange membrane may not be placed.

[0322] That is, the mesh member (402) can be selectively arranged according to the shape of the first divided electrode and the second divided electrode.

[0323] Additionally, the first end plate (500a) is positioned to surround the first mounting space (210a) on the second side (202) of the first intermediate plate (200a), and the second end plate (500b) is positioned to surround the second mounting space (210b) on the second side (202) of the second intermediate plate (200b).

[0324] In the state assembled as described above, livestock wastewater as an organic waste resource may be introduced through one or more of the multiple flow holes (240a) of the first intermediate plate (200a), and fresh water as an electrolyte for hydrogen production may be introduced through one or more of the multiple flow holes (240b) of the second intermediate plate (200b).

[0325] At this time, power can be supplied to each of the first and second collectors.

[0326] The wastewater flowing into the first intermediate plate (200a) flows into a portion of the area (S1) formed at the edge of the first intermediate plate, passes through the passage (235) formed in the first partition member, flows into an adjacent area, and comes into contact with each of the first divided electrodes and the anode membrane.

[0327] At the same time, fresh water flowing into the second intermediate plate (200b) flows into a portion of the area (S2) formed at the edge of the second intermediate plate, passes through the passage (235) formed in the second partition member, flows into an adjacent area, and comes into contact with each of the second divided electrodes and the anode membrane.

[0328] At this time, the water (H2O) contained in each fluid in contact with the anode membrane (100) is hydroxide ions (OH). - ) and hydrogen ions (H + Separated into ) and hydroxide ions move to the first split electrode side, and hydrogen ions move to the second split electrode side.

[0329] As described above, hydrogen ions moved to the second split electrode side can form hydrogen gas by the second split electrode and be discharged to the outside.

[0330] Due to the aforementioned zero-gap structure, the hydrogen production volume increases at the same current density, resulting in an increase in hydrogen production efficiency.

[0331] In other words, by minimizing the distance between the first and second split electrodes, the internal resistance of the stack is reduced, allowing hydrogen ions migrated from the anode membrane to be utilized directly at the second split electrode. Accordingly, there is an advantage in that energy loss can be minimized due to excellent hydrogen ion concentration and ion transportability.

[0332] Here, the electrolyte for hydrogen production may include, but is not limited to, fresh water, seawater, concentrated brine, industrial wastewater, etc.

[0333] Additionally, each of the first current collectors (530a) can be electrically connected to the first divided electrode through each mesh member (401), and each of the second current collectors (530b) can be electrically connected to the second divided electrode through each mesh member (401).

[0334] In addition, the second current collector (530b) provided at a position corresponding to each first current collector (530a) can be electrically connected to each other and can be connected asymmetrically to increase current density and improve hydrogen productivity as needed.

[0335] For example, 20 first current collectors electrically connected to the anode electrode and 1 second current collector electrically connected to the cathode electrode may be electrically connected. In this case, when the electrodes are electrically connected symmetrically, the current density can be improved from an average of 4 A / m2 to 10 A / m2. The number of electrically connected current collectors can be selected as needed.

[0336] In addition, each of the first and second current collectors is electrically connected to a power source and can supply power to each divided electrode placed inside the device.

[0337] FIGS. 43 and FIGS. 44 are diagrams showing the flow path of a fluid flowing inside an intermediate plate with the aforementioned fluid introduced.

[0338] When fluid is introduced into the lower flow holes (2402a, 2402b) formed at the lower ends of the first intermediate plate and the second intermediate plate, the fluid is filled from the bottom by gravity, and the introduced fluid can come into uniform direct contact with each electrode and the anode membrane.

[0339] In addition, the fluid can flow uniformly in the left-right and up-down directions through a connecting member for circulating the fluid.

[0340] Meanwhile, FIG. 45 is an electrochemical device (11) according to another embodiment of the present document, which can be used as an electrodialysis device (ED), a reverse electrodialysis device (RED), a microbial reverse electrodialysis electrolysis device, and a water electrolysis device.

[0341] First, an electrolysis device (11) according to another embodiment of the present document can be configured by selectively placing an ion exchange membrane at a position placed on the anode membrane shown in FIG. 30 as needed. Accordingly, configurations identical to those shown in FIG. 30 use the same reference numerals, their descriptions are omitted, and the above-mentioned content can be applied in the same way.

[0342] Referring to FIG. 45, the electrolysis device (11) comprises: an ion exchange membrane section (150) having one or more ion exchange membranes (140) having a first surface (141) and a second surface (142) opposite to the first surface (141); a first intermediate plate (200a) having a first mounting space (210a) arranged to face the first surface (141) and having a plurality of first split electrodes (300a) mounted thereon; a first end plate (500a) arranged to surround the first mounting space; a second intermediate plate (200b) having a second mounting space (210b) arranged to face the second surface (142) and having a plurality of second split electrodes (300b) having different polarities from the first split electrodes (300a) mounted thereon; and a second end plate (500b) arranged to surround the second mounting space (210b). The ion exchange membrane section (140) It includes a cation exchange membrane and an anion exchange membrane arranged to partition one or more fluid flow paths.

[0343] More specifically, when the electrolysis device (11) is used as an electrodialysis (ED) device, one or more cation exchange membranes and one or more anion exchange membranes may be alternately arranged in the ion exchange membrane section (150) to form one or more flow paths through which fluid flows between each ion exchange membrane.

[0344] Here, both the arrangement of ion exchange membranes and the fluids typically used in electrodialysis (ED) can be applied.

[0345] For example, a cation exchange membrane, an anion exchange membrane, a cation exchange membrane, an anion exchange membrane, and a cation exchange membrane may be arranged in sequence in the ion exchange membrane section (150).

[0346] In addition, an anion exchange membrane, a cation exchange membrane, an anion exchange membrane, a cation exchange membrane, and an anion exchange membrane may be arranged in sequence on the ion exchange membrane portion (150).

[0347] In the state arranged as described above, fluid is supplied to each flow path, and ions are selectively passed through the ion exchange membrane by an electric field formed by supplying electricity through the first and second current collectors, thereby allowing desalination, purification, concentration, and recovery of ionic substances through separation.

[0348] In addition, when the electrolysis device (11) is used as a reverse electrodialysis (RED) device, an ion exchange membrane section (150) is placed as in an electrodialysis (ED) device, and a fluid having a concentration difference (e.g., seawater and fresh water) is supplied to the flow path formed inside, respectively, and electricity can be produced by the concentration difference of the fluid flowing through the flow path.

[0349] Here, both the arrangement of ion exchange membranes and the fluids typically used in reverse electrodialysis (RED) can be applied.

[0350] In particular, when the electrolysis device (11) is used as a microbial reverse electrodialysis device, a cation exchange membrane and an anion exchange membrane are alternately arranged in the ion exchange membrane section, similar to a reverse electrodialysis (RED) device, and electricity is produced by the concentration difference of the fluid flowing through the flow path, and hydrogen can be produced internally using the produced electricity.

[0351] In addition, when the electrolysis device (11) is used as a water electrolysis device, a cation exchange membrane or an anion exchange membrane may be arranged in the ion exchange membrane section (150) to produce hydrogen.

[0352] FIG. 46 is a drawing showing an electrochemical module (10a) using an electrochemical device (10) according to another embodiment of the present document and an electrochemical module (11a) using an electrochemical device (11) according to yet another embodiment of the present document.

[0353] In the following, the configuration of the aforementioned electrochemical device (10) and the configuration of the electrochemical device (11) can all be applied in the same way.

[0354] Referring to FIG. 46, an electrochemical module (10a) according to another embodiment of the present invention comprises: a bipolar membrane (100) having a first surface and a second surface opposite to the first surface; a first intermediate plate (200a) arranged to face the first surface and having a first mounting space on which a plurality of first split electrodes are mounted; a first end plate (500a) arranged to surround the first mounting space; a second intermediate plate (200b) arranged to face the second surface and having a second mounting space on which a plurality of second split electrodes having different polarities from the first split electrodes are mounted; and a second end plate (500b) arranged to surround the second mounting space. The first end plate (500a) has a plurality of first through holes facing each section of the first mounting space, and a first current collector is mounted in each of the first through holes, and the first current collector is provided to be electrically connected to the first split electrode. The second end plate (500b) has a plurality of first through holes facing each section of the second mounting space. The apparatus comprises one or more electrochemical devices (10) having multiple second through holes, each second through hole having a second current collector mounted thereon, and the second current collector being configured to be electrically connected to a second split electrode, wherein each electrochemical device (10) includes a first power connection connector (13) for electrically connecting multiple first current collectors mounted on a first end plate (500a) and a second power connection connector (14) for electrically connecting multiple second current collectors mounted on a second end plate (500b), and the first power connection connector (13) and the second power connection connector (14) are electrically connected to a power source.

[0355] Here, the first power connection connector (13) and the second power connection connector (14) can be electrically connected.

[0356] As described above, by using a power connection connector, the entire house can be electrically connected more easily.

[0357] Additionally, an electrochemical module (11a) according to another embodiment of the present document comprises an ion exchange membrane section (150) having one or more ion exchange membranes having a first surface and a second surface opposite to the first surface, a first intermediate plate (200a) having a first mounting space having a plurality of first split electrodes mounted thereon and positioned to face the first surface, a first end plate (500a) positioned to surround the first mounting space, a second intermediate plate (200b) having a second mounting space having a plurality of second split electrodes having a polarity different from the first split electrodes mounted thereon and positioned to face the second surface, and a second end plate (500b) positioned to surround the second mounting space, wherein the ion exchange membrane section (150) comprises a cation exchange membrane and an anion exchange membrane arranged to partition one or more fluid flow paths, and the first end plate (500a) has a plurality of first through holes facing each section of the first mounting space, and a first current collector is mounted in each of the first through holes. A first current collector is provided to be electrically connected to a first split electrode, and a second end plate (500b) has a plurality of second through holes facing each section of a second mounting space, and a second current collector is mounted in each of the second through holes, and the second current collector is provided to be electrically connected to a second split electrode, and includes one or more electrochemical devices (11), each electrochemical device (11) includes a first power connection connector (13) for electrically connecting a plurality of first current collectors mounted on the first end plate and a second power connection connector (14) for electrically connecting a plurality of second current collectors mounted on the second end plate, and the first power connection connector and the second power connection connector are electrically connected to a power source.

[0358] Here, the first power connection connector (13) and the second power connection connector (14) can be electrically connected.

[0359] As described above, by using a power connection connector, the entire collection can be electrically connected more easily.

[0360] Additionally, the first power connection connector (13) can electrically connect selected first current collectors, and the second power connection connector (14) can electrically connect selected second current collectors.

[0361] Gaskets and spacers, etc., which are placed in an electrochemical device according to another embodiment of this document to form a fluid path or prevent fluid leakage, have been omitted for the convenience of explanation.

[0362]

[0363] The embodiments of this document are intended to illustrate technical concepts, and the scope of the technical concepts of the embodiments of this document is not limited by these embodiments. The scope of protection of the embodiments of this document shall be interpreted by the claims below, and all technical concepts within an equivalent scope shall be interpreted as being included within the scope of rights of the embodiments of this document.

[0364]

[0365] < Explanation of Symbols >

[0366] 10: Self-pH-balancing bipolar membrane,

[0367] 11: Cation exchange layer,

[0368] 12 : Catalyst layer,

[0369] 13: Anion exchange layer,

[0370] 20 : Microbial electrolytic cell,

[0371] 21: Reaction chamber,

[0372] 22 : Anode electrode,

[0373] 23 : Cathode electrode,

[0374] 30: Hydrogen production device,

[0375] 31 : Cathode electrode,

[0376] 32 : Bio-anode electrode,

[0377] 40: Resource recovery device,

[0378] 41: Cation exchange membrane,

[0379] 42 : Cathode electrode,

[0380] 43 : Bio-anode electrode,

[0381] 50 : Acid-base production device,

[0382] 51 : Reaction chamber,

[0383] 52 : Bio-anode electrode,

[0384] 53 : Cathode electrode,

[0385] 54: Cation exchange membrane,

Claims

1. As a bipolar membrane (BPM) used in a microbial electrolysis cell (MEC), Cation exchange layer (CEL); and anion exchange layer (AEL); Includes, The above bipolar membrane (BPM) is, Cylindrical, Self-pH-balancing bipolar membrane.

2. In Paragraph 1, The above bipolar membrane (BPM) is, The cation exchange layer (CEL) and the anion exchange layer (AEL) are interlocked by double electrospinning, Self-pH-balancing bipolar membrane.

3. In Paragraph 1, The above cation exchange layer (CEL) is, Forming the outer surface of the above-mentioned bipolar membrane (BPM) in a cylindrical shape, and The above anion exchange layer (AEL) is, Forming the interior of the above-mentioned bipolar membrane (BPM) in a cylindrical shape, Self-pH-balancing bipolar membrane.

4. In Paragraph 1, The above bipolar membrane (BPM) is, A catalyst layer disposed between the cation exchange layer (CEL) and the anion exchange layer (AEL); A self-pH-balancing bipolar membrane further comprising 5. In Paragraph 4, The above catalyst layer is, Composed of organic-inorganic nanocomposite materials that aid in water splitting, Self-pH-balancing bipolar membrane.

6. A method for manufacturing a bipolar membrane (BPM) used in a microbial electrolysis cell (MEC), wherein A step of forming an anion exchange layer (AEL) that forms the interior of the cylindrical bipolar membrane (BPM); and A step of forming a cation exchange layer (CEL) that forms the outer surface of the cylindrical anode membrane (BPM); A method for manufacturing a self-pH-balancing anodic membrane comprising 7. In Paragraph 6, The above cation exchange layer (CEL) and the above anion exchange layer (AEL) are, Interlocked by double electrospinning, Method for manufacturing a self-pH-balancing bipolar membrane.

8. In Paragraph 6, A step of forming a catalyst layer disposed between the cation exchange layer (CEL) and the anion exchange layer (AEL); A method for manufacturing a self-pH-balancing bipolar membrane comprising further 9. In Paragraph 8, The above catalyst layer is, Composed of organic-inorganic nanocomposite materials that aid in water splitting, Method for manufacturing a self-pH-balancing bipolar membrane.

10. A microbial electrolytic cell comprising a self-pH-balancing anode membrane as described in any one of claims 1 to 5.

11. A hydrogen production apparatus comprising a self-pH-balancing anodic membrane as described in any one of claims 1 to 5.

12. A resource recovery device comprising a self-pH-balancing anodic membrane as described in any one of claims 1 to 5.

13. An acid-base production device comprising a self-pH-balancing bipolar membrane as described in any one of claims 1 to 5.

14. A microbial electrochemical battery comprising a self-pH-balancing anode membrane as described in any one of claims 1 to 5.

15. An e-fuel production device comprising a self-pH-balancing anodic membrane as described in any one of claims 1 to 5.

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