Reactor, separation device, treatment device, membrane reactor, reaction method, and hydrogen separation method

Abstract

To provide a reactor, a separation device, a treatment device, and a membrane reactor that enable efficient extraction of hydrogen from a hydrogen-containing substance.SOLUTION: A reactor (100, 100A) includes a first conductive thin film (13), a second conductive thin film (13), and a current supply section (12). The first conductive thin film is induction-heated by a magnetic flux generated by the current supply section. The second conductive thin film is further induction-heated by the portion of the magnetic flux generated by the current supply section which is not offset by the first conductive thin film.SELECTED DRAWING: Figure 1

Description

Technical Field

[0001] The present invention relates to a reactor, a separation device, a treatment device, a membrane reactor, a reaction method, and a hydrogen separation method.

Background Art

[0002] As a hydrogen transport technology, a technology is known in which a hydrogen-containing substance (for example, MCH (methylcyclohexane)), which is a hydrogen carrier, is generated, the hydrogen-containing substance is transported, and hydrogen is extracted from the hydrogen-containing substance by a dehydrogenation reaction. Here, the dehydrogenation reaction is an endothermic reaction, and heat supply is essential. Non-Patent Document 1 discloses that in the production of hydrogen by a methane steam reforming reaction, when the thermal equilibrium temperature (reaction temperature) is increased, the methane conversion rate (hydrogen production rate) increases significantly.

[0003] Conventionally, as a reactor for the above dehydrogenation reaction, a reactor is known in which the dehydrogenation reaction is advanced by external heating that heats a hydrogen-containing substance from the outside of the reactor. In this reactor, specifically, the outer wall surface of a pipe including a flow path through which the hydrogen-containing substance flows is heated, and the hydrogen-containing substance is heated by heat conduction, convection between the pipe wall surface and the gas, and radiation through the outer wall surface.

[0004] In such a reactor, the temperature decreases as the flow rate of the hydrogen-containing substance increases toward the center of the pipe. Further, since it is external heating, the supply of heat to the center of the pipe is insufficient, and the temperature at the center of the pipe is even lower compared to the temperature near the inner wall surface. Therefore, the hydrogen production rate may be non-uniform in a cross section orthogonal to the axial direction in the pipe. Non-Patent Document 2 discloses that a cold spot occurs at the center of a cylindrical pipe when the pipe is heated from the outside in a reactor that causes a dehydrogenation reaction of MCH, as a result of a temperature distribution simulation.

[0005] In addition, it is required to separate (purify) high-purity hydrogen gas as a fuel from a mixed gas with a low hydrogen concentration, such as in a fuel cell vehicle. Conventionally, as a device for separating high-purity hydrogen gas, a separation device equipped with a hydrogen separation membrane that selectively separates hydrogen is known. Here, the hydrogen permeation performance of the hydrogen separation membrane depends on temperature. In particular, in order to maintain the hydrogen permeation performance of metal membranes such as vanadium V membranes and palladium Pd membranes, heating of the hydrogen separation membrane is necessary. Patent Documents 1 and 2 describe that there is a temperature at which the hydrogen permeation performance of the hydrogen separation membrane is optimal.

[0006] As a method for heating the hydrogen separation membrane, external heating is known. Specifically, in external heating, the hydrogen separation membrane is heated through heat conduction of the tube wall surface, convection between the tube wall surface and the mixed gas, convection between the mixed gas and the hydrogen separation membrane, and radiative heat transfer.

[0007] In addition, a membrane reactor that collectively performs a process of generating hydrogen from a hydrogen-containing substance by a dehydrogenation reaction and a process of separating high-purity hydrogen gas from a mixed gas containing hydrogen generated by the dehydrogenation reaction is also known.

Prior Art Documents

Patent Documents

[0008]

Patent Document 1

Patent Document 2

Non-Patent Documents

[0009]

Non-Patent Document 1

Non-Patent Document 2

Summary of the Invention

Problems to be Solved by the Invention

[0010] In the method of causing a dehydrogenation reaction by external heating, in order to improve the hydrogen production rate even at the center of the tube, it is necessary to raise the heating temperature of the external heat source to 1000 - 1100°C. From the perspective of energy conservation, there is room for improvement.

[0011] Also, Patent Documents 1 and 2 do not disclose a specific control method for maintaining the temperature of the hydrogen separation membrane at a temperature at which the hydrogen permeation performance is optimal. If the temperature of the hydrogen separation membrane is maintained at a temperature at which the hydrogen permeation performance is optimal by external heating, there are problems such as high heat transfer resistance due to passing through many heat transfer paths and poor heat responsiveness.

[0012] One aspect of the present invention aims to provide a reactor, a separation device, a treatment device, and a membrane reactor that can efficiently extract hydrogen from a hydrogen-containing substance.

Means for Solving the Problems

[0013] To solve the above problems, a reactor according to Aspect 1 of the present invention includes a flow path, a first conductive thin film disposed in the flow path, a second conductive thin film disposed in the flow path, a conductive wire through which an alternating current flows, and an energizing portion disposed along the flow path. The first conductive thin film is located between the energizing portion and the second conductive thin film. The first conductive thin film is induction-heated by the magnetic flux generated by the energizing portion, and further, the second conductive thin film is induction-heated by the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the energizing portion, thereby advancing the reaction of the substance flowing through the flow path.

[0014] In the reactor according to Aspect 2 of the present invention, in the above Aspect 1, the first conductive thin film and the second conductive thin film are substantially coaxial multi-cylindrical films, and the energizing portion may be a coil wound around the first conductive thin film.

[0015] In the reactor according to Aspect 3 of the present invention, in the above Aspect 1 or 2, the flow path may be filled with a catalyst that promotes the reaction.

[0016] In the reactor according to Aspect 4 of the present invention, in the above Aspect 1 or 2, the periphery of the first conductive thin film and the second conductive thin film may be coated with a catalyst that promotes the reaction.

[0017] To solve the above problems, a processing apparatus according to Aspect 5 of the present invention includes a first flow path, a second flow path, a third flow path, a first conductive thin film located between the first flow path and the second flow path, a second conductive thin film located between the second flow path and the third flow path, and an energizing portion having a conductive wire through which an alternating current flows. The first conductive thin film is located between the energizing portion and the second conductive thin film. The first conductive thin film is induction-heated by the magnetic flux generated by the energizing portion, and further, the second conductive thin film is induction-heated by the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the energizing portion.

[0018] In order to solve the above problems, the separation device according to aspect 6 of the present invention includes a conductive hydrogen separation membrane that selectively separates hydrogen, and an energization unit having a conductive wire through which an alternating current flows, and the hydrogen separation membrane is induction-heated by the magnetic flux generated by the energization unit.

[0019] In the separation device according to aspect 7 of the present invention, in the above aspect 6, the hydrogen separation membrane is a tubular membrane, and the energization unit may be a coil wound around the hydrogen separation membrane.

[0020] In order to solve the above problems, the membrane reactor according to aspect 8 of the present invention includes a first conductive thin film, a second conductive thin film, and an energization unit having a conductive wire through which an alternating current flows. The first conductive thin film is located between the energization unit and the second conductive thin film, and the first conductive thin film is induction-heated by the magnetic flux generated by the energization unit. Further, the second conductive thin film is induction-heated by the magnetic flux that is not canceled by the first conductive thin film among the magnetic fluxes generated by the energization unit. Either one of the first conductive thin film and the second conductive thin film is a hydrogen separation membrane that selectively separates hydrogen.

[0021] In order to solve the above problems, the reaction method according to aspect 9 of the present invention includes a flow path, a first conductive thin film disposed in the flow path, a second conductive thin film disposed in the flow path, and an energization unit having a conductive wire and disposed along the flow path. The first conductive thin film is located between the energization unit and the second conductive thin film. The reaction method uses a reactor, and includes an induction heating step of flowing an alternating current through the conductive wire to induction-heat the first conductive thin film with the magnetic flux generated by the energization unit, and further induction-heating the second conductive thin film with the magnetic flux that is not canceled by the first conductive thin film among the magnetic fluxes generated by the energization unit. By the induction heating step, the reaction of the substance flowing through the flow path is advanced.

[0022] In order to solve the above problems, a hydrogen separation method according to Embodiment 10 of the present invention is a hydrogen separation method using a separation device including a conductive hydrogen separation membrane that selectively separates hydrogen and an energization unit having a conductive wire, and includes an induction heating step of inductively heating the hydrogen separation membrane with magnetic flux generated by the energization unit by passing an alternating current through the conductive wire.

Advantages of the Invention

[0023] According to one aspect of the present invention, hydrogen can be efficiently extracted from a hydrogen-containing substance.

Brief Description of the Drawings

[0024]

Figure 1

Figure 2

Figure 3

Figure 4

Figure 5

Figure 6

Figure 7

Figure 8

Figure 9

Figure 10

Figure 11

Figure 12

BEST MODE FOR CARRYING OUT THE INVENTION

[0025] 〔Embodiment 1〕 (Schematic configuration of reactor 100) FIG. 1 is a diagram schematically showing an example of the configuration of a reactor (reactor 100) according to an embodiment. Reference numeral 1001 in FIG. 1 is a cross-sectional view of reactor 100. Reference numeral 1002 in FIG. 1 is a longitudinal sectional view of reactor 100. As shown in FIG. 1, reactor 100 includes a container 11, a plurality of energization portions 12, and a plurality of conductive thin films 13. Reactor 100 is a device that causes a dehydrogenation reaction to proceed by heating a hydrogen-containing substance to generate hydrogen. In this specification, the hydrogen-containing substance is a substance containing hydrogen as an atom (for example, ammonia, MCH, etc.).

[0026] Container 11 is a pipe member in which a flow path 14 for flowing a hydrogen-containing substance is formed inside. Energization portion 12 has a conductive wire 121 through which an alternating current flows, and is arranged along flow path 14. Conductive thin film 13 is a thin film having conductivity and is arranged in flow path 14. Conductive thin film 13 contains a conductive material such as copper, aluminum, or stainless steel (SUS304). The plurality of conductive thin films 13 include at least a first conductive thin film on the energization portion 12 side and a second conductive thin film on the side opposite to the energization portion 12 side. In other words, the first conductive thin film is located between the energization portion 12 and the second conductive thin film.

[0027] In the example shown in FIG. 1, reactor 100 is a catalyst-packed layer type reactor in which a catalyst-packed layer is formed in flow path 14. That is, the inside of flow path 14 is filled with a catalyst that promotes the dehydrogenation reaction of the hydrogen-containing substance.

[0028] Further, the container 11 is a cylindrical member, and the energizing portion 12 and the conductive thin film 13 are cylindrical members substantially coaxial with the container 11. The plurality of energizing portions 12 include an energizing portion 12a disposed near the inner side with respect to the inner wall surface of the container 11 and an energizing portion 12b disposed near the central portion of the container 11. The plurality of conductive thin films 13 have conductive thin films 13a, 13b, and 13c in order from the outside to the inside of the container 11. That is, the plurality of conductive thin films 13 have a multi-cylindrical film structure.

[0029] Also, the conductive wire 121 of the energizing portion 12 is a coil wound around the first conductive thin film (spirally along the axial direction of the container 11). Specifically, the conductive wire 121 of the energizing portion 12a is a coil wound outside the conductive thin film 13a, and the conductive wire 121 of the energizing portion 12b is a coil wound inside the conductive thin film 13c. The energizing portion 12 further has an insulator portion 122 that houses a winding body around which the conductive wire 121 is wound.

[0030] When an alternating current flows through the conductive wire 121, a magnetic flux is generated around the energizing portion 12. The magnetic flux generated by the energizing portion 12 first links with the first conductive thin film close to the energizing portion 12. Thereby, an induced current (eddy current) is induced in the first conductive thin film, and loss power is generated. That is, the first conductive thin film is induction-heated. Here, the thickness of the first conductive thin film is at least less than the thickness at which an induced current that completely cancels the linking magnetic flux is induced. Therefore, among the magnetic fluxes generated by the energizing portion 12, the magnetic flux not canceled by the first conductive thin film links with the second conductive thin film (when there are a plurality of second conductive thin films, the thin film closest to the energizing portion 12 among the plurality of second conductive thin films) on the side opposite to the energizing portion 12 with respect to the first conductive thin film. Due to such a magnetic flux not canceled by the first conductive thin film, the second conductive thin film is similarly induction-heated.

[0031] In one example shown in FIG. 1, the conductive thin film 13a is induction-heated by the magnetic flux generated by the energizing portion 12a. Further, the conductive thin film 13b is induction-heated by the magnetic flux that was not canceled out by the conductive thin film 13a among the magnetic flux generated by the energizing portion 12a. Furthermore, the conductive thin film 13c is induction-heated by the magnetic flux that was not canceled out by the conductive thin films 13a and 13b among the magnetic flux generated by the energizing portion 12a. Similarly, the conductive thin film 13c is induction-heated by the magnetic flux generated by the energizing portion 12b. Further, the conductive thin film 13b is induction-heated by the magnetic flux that was not canceled out by the conductive thin film 13c among the magnetic flux generated by the energizing portion 12b. Furthermore, the conductive thin film 13a is induction-heated by the magnetic flux that was not canceled out by the conductive thin films 13c and 13b among the magnetic flux generated by the energizing portion 12b.

[0032] According to the above configuration, by induction-heating the plurality of conductive thin films 13, the hydrogen-containing substance flowing through the flow path 14 can be directly heated. Therefore, the dehydrogenation reaction of the hydrogen-containing substance can proceed efficiently. Here, by adjusting the design parameters regarding the plurality of conductive thin films 13 and the control parameters regarding energization, the power distribution to the plurality of conductive thin films 13 can be controlled. Therefore, the power distribution to the plurality of conductive thin films 13 can be made into a desired power distribution (for example, corresponding to the flow rate of the hydrogen-containing substance in the flow path 14). Thereby, heat can be uniformly supplied to the hydrogen-containing substance in the flow path 14, and the dehydrogenation reaction of the hydrogen-containing substance can proceed efficiently. In other words, the non-uniformity of the hydrogen generation rate in the flow path, which occurred in the conventional reactor using external heating (due to insufficient heat supply reaching the central part of the flow path), can be eliminated.

[0033] Examples of design parameters include the material of the conductive thin film 13 (resistivity, relative permeability), film thickness δ, film separation s, etc. Further, when the plurality of conductive thin films 13 have apertures (through-holes) for promoting magnetic flux leakage, the design parameters for the plurality of conductive thin films 13 also include the aperture ratio, the shape of the apertures (aperture distribution, regular holes, porous holes), etc. Examples of the material of the conductive thin film 13 include SUS, Al, Cu, vanadium V, palladium Pd, etc. Examples of control parameters include the current value I (amplitude), frequency f, number of coil turns N, etc. of the alternating current flowing through the conductive wire 121 of the energizing section 12.

[0034] The thickness of the first conductive thin film (thin film thickness δ) may be less than 2 mm. Thereby, the magnetic flux generated by the energizing section 12 is not completely cancelled out by the induced current induced in the first conductive thin film, and also affects the second conductive thin film on the side opposite to the energizing section 12 with respect to the first conductive thin film. That is, the second conductive thin film can be sufficiently induction-heated. Preferably, the thin film thickness δ is 0.8 mm or less.

[0035] For example, by designing the film thickness of the conductive thin film 13b located at a position away from the energizing section 12 with respect to the conductive thin films 13a and 13c to be thick, even the magnetic flux not cancelled out by the conductive thin films 13a and 13c can distribute power to the conductive thin film 13b to the same extent as the conductive thin films 13a and 13c. That is, uniform power distribution is possible. Further, in the case where the flow rate increases as it approaches the inside in the flow path 14, the design parameters and control parameters may be adjusted so that the power distribution to the inner conductive thin film becomes larger in accordance with the gradient of the flow rate. The simulation results of the power distribution to the plurality of conductive thin films will be described later as Example 1 and Example 2.

[0036] Note that the shape of the container 11 is not limited to a cylindrical shape, and may be various cylindrical shapes such as an elliptical cylindrical shape, a square cylindrical shape, a hexagonal cylindrical shape, etc. Similarly, the energizing section 12 and the conductive thin film 13 may also have the above-described cylindrical shapes.

[0037] Further, the energizing portion 12 may be disposed only in the vicinity of the inner side with respect to the inner wall surface of the container 11, or may be disposed only in the vicinity of the central portion of the container 11. Further, the energizing portion 12 may be disposed outside the container 11.

[0038] Further, the conductive thin film 13 does not have to be a cylindrical member, and may be, for example, a plurality of flat films formed from one side to the other side of the inner wall surface of the container 11. The plurality of flat films may be arranged to be parallel to each other. Further, the number of the conductive thin films 13 is not limited to three, and may be two or four or more.

[0039] (Schematic configuration of reactor 100A) FIG. 2 is a diagram schematically showing another example (reactor 100A) of the configuration of the reactor. Reference numeral 2001 in FIG. 2 is a cross-sectional view of the catalyst film 13A of the reactor 100A. Reference numeral 2002 in FIG. 2 is an enlarged view showing a part of the catalyst film 13A of the reactor 100A. Reference numeral 2003 in FIG. 2 is a longitudinal sectional view of the reactor 100A. As shown in FIG. 2, the reactor 100A includes a container 11, an energizing portion 12, and a catalyst film 13A.

[0040] In an example shown in FIG. 2, the reactor 100A is a catalyst film type reactor (catalyst structure) in which a catalyst film 13A is formed in a flow path 14. The catalyst film 13A has a conductive thin film 131A having a honeycomb structure and a catalyst layer 132A covering the periphery of the conductive thin film. That is, a catalyst for promoting the dehydrogenation reaction is coated around the conductive thin film 131A.

[0041] In an example shown in FIG. 2, an outer peripheral portion of the conductive thin film 131A is a first conductive thin film, and a portion inside the outer peripheral portion of the conductive thin film 131A is a second conductive thin film. That is, the outer peripheral portion of the conductive thin film 131A is induction-heated by the magnetic flux generated by the energizing portion 12a. Further, a portion inside the outer peripheral portion of the conductive thin film 131A is induction-heated by the magnetic flux that is not canceled by the outer peripheral portion of the conductive thin film 131A among the magnetic fluxes generated by the energizing portion 12a.

[0042] According to the above configuration, similar to the reactor 100, the dehydrogenation reaction of the hydrogen-containing substance can proceed efficiently. Further, by providing the conductive thin film 131A inside the catalyst film 13A, the heat transfer area can be increased and the thermal conductivity can be improved. That is, the dehydrogenation reaction of the hydrogen-containing substance can proceed more efficiently.

[0043] Note that the reaction caused in the reactors 100 and 100A is not limited to the above-described dehydrogenation reaction, and any reaction that requires heat supply is acceptable.

[0044] Further, the reactors 100 and 100A can also be regarded as a processing device described below. That is, the reactors 100 and 100A are a processing device including a first flow path, a second flow path, a third flow path, a first conductive thin film located between the first flow path and the second flow path, a second conductive thin film located between the second flow path and the third flow path, and an energization unit 12. The flow of substances in the first flow path, the second flow path, and the third flow path does not have to be in the same direction. According to the above configuration, the heat supply to the substances flowing through each flow path can be adjusted according to the flow rate of each flow path. Therefore, the process that requires heat supply to the substances flowing through the first flow path, the second flow path, and the third flow path can be efficiently performed.

[0045] (Configuration of the energization unit 12) FIG. 3 is a diagram showing a detailed configuration of the energization unit 12. Reference numerals 3001 to 3004 in FIG. 3 show some examples of the detailed configuration of the energization unit 12. Note that the energization unit 12 shown in FIGS. 1 and 2 corresponds to the pattern shown by reference numeral 3004 in FIG. 3.

[0046] As shown by reference numeral 3001 in FIG. 3, the energizing portion 12 may have a conductive wire 121 as a coil and an insulating layer 124 covering around the conductive wire 121. Further, as shown by reference numeral 3002 in FIG. 3, the energizing portion 12 may further include a conductive thin film 125 formed so as to surround the conductive wire 121 inside the insulating layer 124 in addition to the conductive wire 121 and the insulating layer 124. Further, as shown by reference numeral 3003 in FIG. 3, the energizing portion 12 may include a conductive wire 121 as a coil, an insulator portion 122 containing a winding body around which the conductive wire 121 is wound, and a conductive thin film 123 formed around the insulator. Further, as shown by reference numeral 3004 in FIG. 3, the energizing portion 12 may include the conductive wire 121 and the insulator portion 122, and may not include the conductive thin film 123.

[0047] According to the configurations shown by reference numerals 3001 and 3004 in FIG. 3, the energizing portion 12 inductively heats the conductive thin film 13 by the magnetic flux generated from the conductive wire 121. Thereby, the hydrogen-containing substance flowing through the flow path 14 can be heated.

[0048] According to the configurations shown by reference numerals 3002 and 3003 in FIG. 3, the energizing portion 12 inductively heats the conductive thin films 123 and 125 included in the energizing portion 12 by the magnetic flux generated from the conductive wire 121. Further, the energizing portion 12 inductively heats the conductive thin film 13 by the magnetic flux that is not canceled by the conductive thin films 123 and 125 among the magnetic flux generated from the conductive wire 121. That is, compared with the configurations shown by reference numerals 3001 and 3004 in FIG. 3, the heat transfer area related to heating the hydrogen-containing substance can be increased, and the thermal conductance can be improved.

[0049] 〔Embodiment 2〕 Other embodiments of the present invention will be described below. For convenience of explanation, members having the same functions as the members described in the above embodiment are denoted by the same reference numerals, and the description thereof will not be repeated.

[0050] (Schematic Configuration of Separation Device 200) FIG. 4 is a cross-sectional view schematically showing an example of the configuration of a separation device (separation device 200) according to an embodiment. As shown in FIG. 4, the separation device 200 includes a container 21, a power supply unit 12, and a hydrogen separation membrane 23. The separation device 200 is a device that separates (purifies) high-purity hydrogen gas from a mixed gas containing hydrogen (unpurified hydrogen gas). Hereinafter, the separated high-purity hydrogen gas is also referred to as purified hydrogen gas.

[0051] The container 21 is a pipe member in which a supply-side flow path 24a through which unpurified hydrogen gas flows and a permeation-side flow path 24b through which purified hydrogen gas flows are formed inside. The hydrogen separation membrane 23 is a conductive thin film that selectively separates hydrogen. The hydrogen separation membrane 23 is, for example, a metal membrane such as a vanadium V membrane and a palladium Pd membrane. The hydrogen separation membrane 23 is disposed between the supply-side flow path 24a and the permeation-side flow path 24b.

[0052] The hydrogen permeation performance of the hydrogen separation membrane 23 depends on temperature. Therefore, in order to improve the hydrogen permeation performance of the hydrogen separation membrane 23, it is important to control the temperature of the hydrogen separation membrane 23. For example, in the case of palladium Pd, the hydrogen permeation coefficient increases as the temperature increases, and in the case of vanadium V, the hydrogen permeation coefficient decreases as the temperature rises. Therefore, it is expected that there is a temperature at which the hydrogen permeation flux of the hydrogen permeation membrane having Pd coated on the V surface takes the maximum value (that is, the hydrogen permeation performance becomes optimal).

[0053] In the example shown in FIG. 4, a pipe 211 having a smaller diameter than the container 21 exists inside the container 21. Unpurified hydrogen gas flows through the pipe 211, and the downstream side of the pipe 211 is open. Thereby, the pipe 211 supplies unpurified hydrogen gas to the inside of the container 21. Hereinafter, the upstream side and the downstream side in the flow direction of the unpurified hydrogen gas in the pipe 211 are simply referred to as the upstream side and the downstream side, respectively.

[0054] Further, the hydrogen separation membrane 23 is a circular membrane located downstream of the opening of the pipe 211 inside the container 21. The hydrogen separation membrane 23 separates the inside of the container 21 into an upstream space and a downstream space. The hydrogen separation membrane 23 selectively separates hydrogen from the unpurified hydrogen gas flowing in the upstream space. As a result, in the downstream space, a purified hydrogen gas that has passed through the hydrogen separation membrane 23 and been separated from the unpurified hydrogen gas is obtained. In other words, the upstream space is the supply-side flow path 24a, and the downstream space is the permeation-side flow path 24b.

[0055] Note that a pump or the like for generating a pressure difference for allowing hydrogen in the unpurified hydrogen gas to permeate through the hydrogen separation membrane 23 is connected to the downstream side of the container 21. Further, the remaining gas in the unpurified hydrogen gas that has not permeated through the hydrogen separation membrane 23 flows downstream of the pipe 211 through the space between the container 21 and the pipe 211 in the radial direction of the container 21.

[0056] Also, the conductive wire 121 of the energization unit 12 is a coil wound outside the hydrogen separation membrane 23. When an alternating current flows through the conductive wire 121, the conductive hydrogen separation membrane 23 is inductively heated. That is, the hydrogen separation membrane 23 functions as the conductive thin film 13 in Embodiment 1.

[0057] According to the above configuration, by inductively heating the hydrogen separation membrane 23 (that is, directly heating the hydrogen separation membrane 23), compared with the case of heating the hydrogen separation membrane 23 by an external heat source, the heat transfer resistance is small, so power supply is facilitated. Therefore, the hydrogen separation membrane 23 can be heated efficiently.

[0058] Also, the hydrogen separation membrane 23 is a thin film and has a small heat capacity, so it has excellent thermal responsiveness. Therefore, the temperature of the hydrogen separation membrane 23 can be controlled at high speed. Accordingly, the hydrogen permeability of the hydrogen separation membrane 23 can be controlled at high speed, and the temperature of the hydrogen separation membrane 23 can be maintained at a temperature at which the hydrogen permeation performance is appropriate (preferably, the hydrogen permeation flux exhibits a maximum value). That is, purified hydrogen gas can be efficiently separated from unpurified hydrogen gas.

[0059] Further, by inductively heating the hydrogen separation membrane 23, the non-uniformity of the temperature distribution in the cross-section orthogonal to the axial direction of the container 21 can be reduced as compared with the case where the hydrogen separation membrane 23 is heated by an external heat source.

[0060] (Schematic Configuration of Separation Device 200A) FIG. 5 is a cross-sectional view schematically showing another example of the configuration of the separation device (separation device 200A). As shown in FIG. 5, the separation device 200A includes a container 21, a current-carrying part 12, and a hydrogen separation membrane 23A.

[0061] In one example shown in FIG. 5, similar to the example shown in FIG. 4, there is a pipe 211 for supplying unpurified hydrogen gas inside the container 21. Here, the hydrogen separation membrane 23A is a cylindrical membrane (for example, a cylindrical membrane) formed so as to surround the pipe 211 and extending upstream from the vicinity on the downstream side of the opening of the pipe 211 inside the container 21. Further, the downstream end of the hydrogen separation membrane 23A is closed. Also, the space between the upstream end of the hydrogen separation membrane 23A and the inner wall surface of the container 21 is closed.

[0062] The unpurified hydrogen gas supplied from the opening of the pipe 211 flows upstream in the space between the pipe 211 and the hydrogen separation membrane 23A. The hydrogen separation membrane 23 selectively separates hydrogen from the unpurified hydrogen gas. As a result, in the space between the hydrogen separation membrane 23A and the container 21, a purified hydrogen gas that has passed through the hydrogen separation membrane 23A and is separated from the unpurified hydrogen gas is obtained. The purified hydrogen gas flows downstream in the space between the hydrogen separation membrane 23A and the container 21. In other words, the space between the pipe 211 and the hydrogen separation membrane 23A is the supply-side flow path 24a, and the space between the hydrogen separation membrane 23A and the container 21 is the permeation-side flow path 24b.

[0063] Further, the conductive wire 121 of the current-carrying part 12 is a coil wound outside the hydrogen separation membrane 23A which is a cylindrical membrane. When an alternating current flows through the conductive wire 121, the conductive hydrogen separation membrane 23A is inductively heated. That is, the hydrogen separation membrane 23A functions as the conductive thin film 13 in Embodiment 1.

[0064] According to the above configuration, the same effects as those in the example shown in FIG. 4 are achieved. Further, since the hydrogen separation membrane 23A is a cylindrical membrane extending in the axial direction of the container 21, the distance between the hydrogen separation membrane 23A and the energization portion 12 can be made substantially uniform. Therefore, the non-uniformity of the temperature distribution in the cross section orthogonal to the axial direction of the container 21 can be further reduced. Also, by increasing the length of the hydrogen separation membrane 23A in the axial direction of the container 21, the hydrogen permeation area can be easily increased.

[0065] (Schematic configuration of the separation device 200C) FIG. 6 is a cross-sectional view schematically showing another example of the configuration of the separation device (separation device 200C). As shown in FIG. 6, the separation device 200C is different from the separation device 200A in that, in addition to the hydrogen separation membrane 23A, it further includes a substantially donut-shaped hydrogen separation membrane 23C that separates the space between the hydrogen separation membrane 23A and the container 21 in the radial direction of the container 21 into an upstream space and a downstream space. Thereby, the hydrogen permeation area can be further increased. A plurality of hydrogen separation membranes 23C may be provided over the axial direction of the container 21. In the example shown in FIG. 6, the separation device 200C includes two hydrogen separation membranes 23C over the axial direction of the container 21.

[0066] (Schematic configuration of the separation device 200B) FIG. 7 is a view schematically showing another example of the configuration of the separation device (separation device 200B). Reference numeral 7001 in FIG. 7 shows a longitudinal cross-sectional view of the separation device 200B. Reference numeral 7002 in FIG. 7 shows a cross-sectional view of the separation device 200B. As shown in FIG. 7, the separation device 200B includes a container 21, a plurality of energization portions 12, and a plurality of hydrogen separation membranes 23B.

[0067] In one example shown in FIG. 7, the plurality of hydrogen separation membranes 23B have hydrogen separation membranes 23Ba, 23Bb, 23Bc, and 23Bd in order from the outside to the inside of the container 21. That is, the plurality of hydrogen separation membranes 23B have a multi-tubular membrane structure. Hereinafter, the space between the inner wall surface of the container 21 and the hydrogen separation membrane 23Ba is referred to as a first flow path 241. Also, the space between the hydrogen separation membrane 23Ba and the hydrogen separation membrane 23Bb is referred to as a second flow path 242. Also, the space between the hydrogen separation membrane 23Bb and the hydrogen separation membrane 23Bc is referred to as a third flow path 243. Also, the space between the hydrogen separation membrane 23Bc and the hydrogen separation membrane 23Bd is referred to as a fourth flow path 244. Also, the space inside the hydrogen separation membrane 23Bd is referred to as a fifth flow path 245.

[0068] The unpurified hydrogen gas flows through the first flow path 241 in the first direction, through the third flow path 243 in the second direction opposite to the first direction, and through the fifth flow path 245 in the first direction. The hydrogen separation membrane 23Ba selectively separates hydrogen from the unpurified hydrogen gas flowing through the first flow path 241. The hydrogen separation membranes 23Bb and 23Bc selectively separate hydrogen from the unpurified hydrogen gas flowing through the third flow path 243. The hydrogen separation membrane 23Bd selectively separates hydrogen from the unpurified hydrogen gas flowing through the fifth flow path 245. The purified hydrogen gas separated from the unpurified hydrogen gas by passing through the hydrogen separation membranes 23Ba and 23Bb flows into the second flow path 242. The purified hydrogen gas separated from the unpurified hydrogen gas by passing through the hydrogen separation membranes 23Bc and 23Bd flows into the fourth flow path 244. In other words, the first flow path 241, the third flow path 243, and the fifth flow path 245 are supply-side flow paths 24a, and the second flow path 242 and the fourth flow path 244 are permeation-side flow paths 24b.

[0069] Also, the conductive wire 121 of the energizing unit 12 is a coil wound outside the hydrogen separation membrane 23Ba and a coil wound inside the hydrogen separation membrane 23Bd. When an alternating current flows through the conductive wire 121, the conductive hydrogen separation membranes 23Ba, 23Bb, 23Bc, and 23Bd are inductively heated. That is, the hydrogen separation membranes 23Ba, 23Bb, 23Bc, and 23Bd function as the conductive thin film 13 in Embodiment 1.

[0070] According to the above configuration, the same effects as those in the example shown in FIG. 4 can be achieved. Further, by forming a plurality of hydrogen separation membranes 23B into a multi-tubular membrane structure, the permeation area of hydrogen can be increased while making the separation device 200B compact.

[0071] Note that, by means of the plurality of energization parts 12, design parameters regarding the hydrogen separation membrane 23B are appropriately set so that the temperatures of all the hydrogen separation membranes 23Ba, 23Bb, 23Bc, and 23Bd can be maintained at a temperature at which the hydrogen permeation performance is appropriate.

[0072] 〔Embodiment 3〕 Other embodiments of the present invention will be described below. For convenience of explanation, members having the same functions as the members described in the above embodiment are denoted by the same reference numerals, and the description thereof will not be repeated.

[0073] (Schematic configuration of the membrane reactor 300) FIG. 8 is a cross-sectional view schematically showing an example of the configuration of a membrane reactor 300 according to an embodiment. FIG. 9 is a cross-sectional view schematically showing another example of the configuration of the membrane reactor 300 according to an embodiment. FIG. 10 is a cross-sectional view schematically showing still another example of the configuration of the membrane reactor 300 according to an embodiment.

[0074] As shown in FIGS. 8 to 10, the membrane reactor 300 includes a container 31, an energization part 12, and a plurality of conductive thin films 33. The membrane reactor 300 is a device that collectively performs a process of generating hydrogen from a hydrogen-containing substance by a dehydrogenation reaction and a process of separating high-purity hydrogen gas from a mixed gas containing hydrogen generated by the dehydrogenation reaction. That is, the membrane reactor 300 is a device having the functions of the reactors 100 and 100A and the separation devices 200, 200A, and 200B described above.

[0075] The container 31 is a pipe member having a supply-side flow path 34a through which a reaction gas containing a hydrogen-containing substance and an unpurified hydrogen gas flow, and a permeation-side flow path 34b through which a purified hydrogen gas flows, formed inside. The energization unit 12 has a conductive wire 121 through which an alternating current flows, and is arranged along the supply-side flow path 34a and the permeation-side flow path 34b. The plurality of conductive thin films 33 are thin films having conductivity. The plurality of conductive thin films 33 have at least a first conductive thin film on the side of the energization unit 12 and a second conductive thin film on the side opposite to the energization unit 12 side. In other words, the first conductive thin film is located between the energization unit 12 and the second conductive thin film.

[0076] The plurality of conductive thin films 33 include a hydrogen separation membrane 331. The hydrogen separation membrane 331 is a conductive thin film that selectively separates hydrogen. The hydrogen separation membrane 331 is arranged between the supply-side flow path 34a and the permeation-side flow path 34b. The remaining conductive thin films 33 are arranged in the supply-side flow path 34a. The remaining conductive thin films 33 have a plurality of through-holes through which the reaction gas and the unpurified hydrogen gas can pass.

[0077] In an example shown in FIGS. 8 to 10, the plurality of conductive thin films 33 are a plurality of flat films formed from one inner wall surface of the container 31 to the other. The first conductive thin film (the hydrogen separation membrane 331 arranged at one end or the conductive thin film arranged at the other end among the plurality of conductive thin films 33) close to the energization unit 12 is induction-heated by the magnetic flux generated by the energization unit 12. Also, the second conductive thin film (the conductive thin film on the other end side with respect to the hydrogen separation membrane 331 or the conductive thin film on the one end side with respect to the conductive thin film arranged at the other end) is induction-heated by the magnetic flux that is not canceled by the first conductive thin film among the magnetic fluxes generated by the energization unit 12. Note that the plurality of conductive thin films 33 may be a plurality of multi-tube films.

[0078] In an example shown in FIG. 8, the membrane reactor 300 is a catalyst-packed layer type reactor in which a catalyst-packed layer 35A is formed in the supply-side flow path 34a. That is, the supply-side flow path 34a is filled with a catalyst that promotes the dehydrogenation reaction of the hydrogen-containing substance.

[0079] In an example shown in FIG. 8, when an alternating current flows through the conductive wire 121 of the energization unit 12, a plurality of conductive thin films 33 (including the hydrogen separation membrane 331) are inductively heated. As a result, the hydrogen-containing substance flowing through the supply-side flow path 34a is heated, and further, by passing through the catalyst-packed layer 35A, the dehydrogenation reaction proceeds. That is, unpurified hydrogen gas is generated. Further, the inductively heated hydrogen separation membrane 331 selectively separates hydrogen from the unpurified hydrogen gas. As a result, a purified hydrogen gas that has passed through the hydrogen separation membrane 331 and is separated from the unpurified hydrogen gas is obtained in the permeation-side flow path 34b.

[0080] In an example shown in FIG. 9, the membrane reactor 300 is a catalyst membrane type reactor in which a catalyst membrane 35B is formed. The catalyst membrane 35B is laminated on the supply-side flow path 34a side of the hydrogen separation membrane 331.

[0081] In an example shown in FIG. 9, when an alternating current flows through the conductive wire 121 of the energization unit 12, a plurality of conductive thin films 33 are inductively heated. As a result, the hydrogen-containing substance flowing through the supply-side flow path 34a is heated, and further, by coming into contact with the catalyst membrane 35B, the dehydrogenation reaction proceeds. That is, unpurified hydrogen gas is generated near the catalyst membrane 35B. Further, the inductively heated hydrogen separation membrane 331 selectively separates hydrogen from the unpurified hydrogen gas generated near the catalyst membrane 35B. As a result, a purified hydrogen gas that has passed through the hydrogen separation membrane 331 and is separated from the unpurified hydrogen gas is obtained in the permeation-side flow path 34b.

[0082] In an example shown in FIG. 10, the membrane reactor 300 is a fluidized bed type reactor having a catalyst 35C that flows in the supply-side flow path 34a.

[0083] In an example shown in FIG. 10, when an alternating current flows through the conductive wire 121 of the energization unit 12, the plurality of conductive thin films 33 are inductively heated. As a result, the hydrogen-containing substance flowing through the supply-side flow path 34a is heated. Here, when the reaction gas flows from the upstream side of the supply-side flow path 34a, the catalyst 35C flows and the hydrogen-containing substance comes into contact with the catalyst. Therefore, the dehydrogenation reaction of the hydrogen-containing substance proceeds. That is, unpurified hydrogen gas is generated. Further, the inductively heated hydrogen separation membrane 331 selectively separates hydrogen from the unpurified hydrogen gas. As a result, in the permeation-side flow path 34b, purified hydrogen gas that has permeated through the hydrogen separation membrane 331 and has been separated from the unpurified hydrogen gas is obtained.

[0084] According to the above configuration, a membrane reactor 300 having the functions of the reactors 100 and 100A and the separation devices 200, 200A, and 200B described above can be provided. Further, the membrane reactor 300 can efficiently advance the dehydrogenation reaction of the hydrogen-containing substance by inductively heating the plurality of conductive thin films 33 including the hydrogen separation membrane 331, and can efficiently separate the purified hydrogen gas from the unpurified hydrogen gas generated by the dehydrogenation reaction.

[0085] 〔Example 1〕 In this Example 1, a simulation of power distribution to the plurality of conductive thin films 13 and the plurality of flow paths 14 with respect to predetermined design parameters and control parameters in the reactor 100 was performed. Here, the plurality of flow paths 14 are flow paths (that is, reaction layers) partitioned by the plurality of conductive thin films 13. In this simulation, the design parameters and control parameters were set as follows.

[0086] The inner diameter of the container 11 was set to 208.3 mm. The material of the container 11 was set to SUS304. Further, inside the container 11, a configuration in which a cylindrical energization unit 12-1, five conductive thin films 13-1 to 13-5, and an energization unit 12-2 were arranged in order from the inside was set. Four flow paths 14-1 to 14-4 are formed by the five conductive thin films 13-1 to 13-5.

[0087] The conductive wires 121 of the energization parts 12-1 and 12-2 were set as copper wires with a diameter of 4 mm. The material of the insulating layer 124 was set as ceramics. The pitch of the conductive wires 121 of the energization parts 12-1 and 12-2 was 7.5 mm, and the number of turns was set as 26. The distance from the outer wall of the container 11 to the axis of the conductive wire 121 of the energization part 12-2 was set as 6 mm. The distance from the axis of the conductive wire 121 of the energization part 12-1 to the axis of the conductive wire 121 of the energization part 12-2 was set as 28 mm.

[0088] The thicknesses of the conductive thin films 13-1 to 13-5 were set as 0.06 mm, 0.15 mm, 0.15 mm, 0.15 mm, and 0.065 mm, respectively. The material of the conductive thin films 13-1 to 13-5 was set as SUS304. The distance between the axis of the conductive wire 121 of the energization part 12-1 and the conductive thin film 13-1, the distance between adjacent conductive thin films 13-1 to 13-5, and the distance between the conductive thin film 13-5 and the axis of the conductive wire 121 of the energization part 12-2 were set as 4 mm.

[0089] The current values passed through the conductive wires 121 of the energization parts 12-1 and 12-2 were set as 50 A and 100 A, respectively.

[0090] Figure 11 is a graph showing the power distribution to the five conductive thin films 13-1 to 13-5 and the container 11 and the power distribution to the four flow paths 14-1 to 14-4 with respect to the above design parameters and control parameters. In Figure 11, the labels 1 to 4 on the horizontal axis respectively show the power loss [W] of the conductive thin films 13-1 to 13-4 on the left side and the power loss [W] of the flow paths 14-1 to 14-4 on the right side. Also, in Figure 11, the labels 5 and 6 on the horizontal axis respectively show the power loss [W] of the conductive thin film 13-5 and the container 11. Here, the power loss of the flow path closest to each energization part is the sum of the power loss of the conductive thin film closest to each energization part and half of the power loss of the other conductive thin film. For example, the power loss of the flow path 14-1 is the sum of the power loss of the conductive thin film 13-1 and half of the power loss of the conductive thin film 13-2. The power loss of the other flow paths is the average value of the power losses of the conductive thin films on both sides.

[0091] As shown in FIG. 11, by designing the design parameters and control parameters as described above (in particular, by designing the film thicknesses of the conductive thin films 13-2 to 13-4 at positions away from the energizing portion 12 to be thick), it was confirmed that uniform power distribution to each of the flow paths 14-1 to 14-4 is possible. That is, it was confirmed that the reactor 100 can achieve uniform power distribution in the cross section orthogonal to the axial direction in the container 11.

[0092] Example 2 In this Example 2, a simulation of power distribution to a plurality of conductive thin films 13 and a plurality of flow paths 14 with respect to predetermined design parameters and control parameters different from those in Example 1 in the reactor 100 was performed. In this simulation, the design parameters and control parameters were set as follows. Unless otherwise specified, members having the same configuration as the members described in Example 1 are given the same reference numerals and their descriptions will not be repeated.

[0093] Inside the container 11, in order from the inside, a cylindrical energizing portion 12-1, five conductive thin films 13-1 to 13-5, an energizing portion 12-2, five conductive thin films 13-6 to 13-10, and an energizing portion 12-3 were arranged. Four flow paths 14-1 to 14-4 are formed by the five conductive thin films 13-1 to 13-5, and four flow paths 14-6 to 14-9 are formed by the five conductive thin films 13-6 to 13-10.

[0094] The energizing portion 12-3 has the same configuration as the energizing portions 12-1 and 12-2 described in Example 1. The distance from the outer wall of the container 11 to the axis of the conductive wire 121 of the energizing portion 12-3 was set to 6.15 mm. The distance from the axis of the conductive wire 121 of the energizing portion 12-2 to the axis of the conductive wire 121 of the energizing portion 12-3 was set to 28 mm.

[0095] The thicknesses of the conductive thin films 13-1 to 13-10 were set to 0.05 mm, 0.14 mm, 0.17 mm, 0.16 mm, 0.08 mm, 0.07 mm, 0.15 mm, 0.17 mm, 0.14 mm, and 0.055 mm, respectively. The distance between the axis of the conductive wire 121 of the energizing section 12-2 and the conductive thin film 13-6, the distances between the conductive thin films 13-6 to 13-10, and the distance between the conductive thin film 13-10 and the axis of the conductive wire 121 of the energizing section 12-3 were set to 4 mm.

[0096] The current values flowing through the conductive wires 121 of the energizing sections 12-1, 12-2, and 12-3 were set to 68 A, 50 A, and 100 A, respectively.

[0097] FIG. 12 is a graph showing the power distribution to the ten conductive thin films 13-1 to 13-10 with respect to the above design parameters and control parameters, and the power distribution to the eight flow paths 14-1 to 14-4, 14-6 to 14-9. In FIG. 12, for the horizontal axis labels 1 to 4, 6 to 9, the loss power [W] of the conductive thin films 13-1 to 13-4, 13-6 to 13-9 is shown on the left side, and the loss power [W] of the flow paths 14-1 to 14-4, 14-6 to 14-9 is shown on the right side. Also, in FIG. 12, for the horizontal axis labels 5, 10, the loss power [W] of the conductive thin films 13-5, 13-10 is shown, respectively.

[0098] As shown in FIG. 12, it was confirmed that by designing the design parameters and control parameters as described above, it is possible to achieve a power distribution such that the loss power increases for the inner flow paths.

[0099] The present invention is not limited to the above-described embodiments, and various modifications are possible within the scope shown in the claims. Embodiments obtained by appropriately combining the technical means disclosed in different embodiments are also included in the technical scope of the present invention.

Explanation of Reference Numerals

[0100] 12 Energizing section 13, 131A, 33 Conductive thin film 14 Flow path 23. 331 Hydrogen separation membrane 100, 100A Reactors 200, 200A, 200B Separators 300 Membrane reactor

Claims

1. A flow path, a first conductive thin film disposed in the flow path, a second conductive thin film disposed in the flow path, a current-carrying portion having a conductive wire through which an alternating current flows, and disposed along the flow path, and comprising: the first conductive thin film is located between the current-carrying portion and the second conductive thin film, a reactor that inductively heats the first conductive thin film with the magnetic flux generated by the current-carrying portion, and further inductively heats the second conductive thin film with the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the current-carrying portion, thereby advancing the reaction of the substance flowing through the flow path.

2. the first conductive thin film and the second conductive thin film are multi-layered cylindrical films, the reactor according to claim 1, wherein the current-carrying portion is a coil wound around the first conductive thin film.

3. the reactor according to claim 1 or 2, wherein the flow path is filled with a catalyst that promotes the reaction.

4. the reactor according to claim 1 or 2, wherein the periphery of the first conductive thin film and the second conductive thin film is coated with a catalyst that promotes the reaction.

5. a first flow path, a second flow path, a third flow path, a first conductive thin film located between the first flow path and the second flow path, a second conductive thin film located between the second flow path and the third flow path, a current-carrying portion having a conductive wire through which an alternating current flows, and comprising: the first conductive thin film is located between the current-carrying portion and the second conductive thin film, a processing apparatus that inductively heats the first conductive thin film with the magnetic flux generated by the current-carrying portion, and further inductively heats the second conductive thin film with the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the current-carrying portion.

6. a conductive hydrogen separation membrane that selectively separates hydrogen, a current-carrying portion having a conductive wire through which an alternating current flows, and comprising: a separation apparatus that inductively heats the hydrogen separation membrane with the magnetic flux generated by the current-carrying portion.

7. the hydrogen separation membrane is a cylindrical film, the separation apparatus according to claim 6, wherein the current-carrying portion is a coil wound around the hydrogen separation membrane.

8. a first conductive thin film, a second conductive thin film, a current-carrying portion having a conductive wire through which an alternating current flows, and comprising: the first conductive thin film is located between the current-carrying portion and the second conductive thin film, the first conductive thin film is inductively heated with the magnetic flux generated by the current-carrying portion, and further the second conductive thin film is inductively heated with the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the current-carrying portion, A membrane reactor, wherein either one of the first conductive thin film and the second conductive thin film is a hydrogen separation membrane that selectively separates hydrogen. **Claim 9** A flow path, A first conductive thin film disposed in the flow path, A second conductive thin film disposed in the flow path, A current-carrying part having a conductive wire and disposed along the flow path, comprising: The first conductive thin film is a reaction method using a reactor positioned between the current-carrying part and the second conductive thin film, An induction heating step of inductively heating the first conductive thin film with the magnetic flux generated by the current-carrying part by passing an alternating current through the conductive wire, and further inductively heating the second conductive thin film with the magnetic flux that is not canceled by the first conductive thin film among the magnetic flux generated by the current-carrying part, A reaction method in which the reaction of the substance flowing through the flow path is advanced by the induction heating step. **Claim 10** A hydrogen separation method using a separation device comprising a conductive hydrogen separation membrane that selectively separates hydrogen and a current-carrying part having a conductive wire, The method comprising an induction heating step of inductively heating the hydrogen separation membrane with the magnetic flux generated by the current-carrying part by passing an alternating current through the conductive wire. ​

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