Methane prolysis reactor

Abstract

The present invention relates to a methane pyrolysis reactor. According to an embodiment of the present invention, a methane pyrolysis reactor may be provided, comprising: a reaction section in which the pyrolysis of methane gas and the generation of carbon particles take place; a gas inlet section for supplying fluidized gas to the reaction section; and a separation section for separating the carbon particles generated in the reaction section.

Description

Technology Field

[0001] The present invention relates to a methane pyrolysis reactor. Background Technology

[0002] Generally, among methane pyrolysis processes, the dry pyrolysis method using solid catalysts is considered the technology with the highest potential for industrial application due to its advantages, such as the simplicity of the device configuration, ease of operation, scalability to a continuous process, and the ability to directly produce high-purity hydrogen. However, in the dry pyrolysis method, carbon decomposed from methane is continuously deposited on the surface of catalyst particles or the reactor walls during the pyrolysis reaction. This carbon deposition causes catalyst deactivation, leading to problems such as reduced reaction rates, lower hydrogen yields, and increased frequency of process interruptions.

[0003] To address this, a technology applying a fluidized-bed reactor has been proposed. However, problems remain with this fluidized-bed method. Since the solid carbon generated during the methane pyrolysis reaction has a much lower density and smaller particle size than the catalyst particles, it exists mixed with the catalyst particles inside the reactor. Consequently, during the process of escaping, the catalyst particles are either discharged along with the solid carbon, or conversely, carbon accumulates inside the reactor, causing the layer structure to collapse and the fluidization state to become unstable.

[0004] Therefore, a technology is required that actively utilizes the physical and fluid dynamic properties (Umf, density, particle size, etc.) of catalyst particles and generated carbon particles in the methane pyrolysis process to form a natural layered structure within the reactor, selectively discharge only carbon particles via top overflow, and stably maintain only the catalyst particles inside the reactor. In particular, leveraging the fact that the minimum fluidization velocity (Umf) of carbon particles is overwhelmingly lower than that of catalyst particles, a velocity-based selective separation technology based on the difference in fluidization initiation points between carbon and catalyst is necessary. Since this technology can directly separate and discharge only carbon from the reactor itself without relying on existing external separation devices, it holds significant value in terms of process stability, continuity, catalyst lifespan, and reduced equipment maintenance costs. The problem to be solved

[0005] The embodiments of the present invention were invented against the background described above and aim to provide a methane pyrolysis reactor that efficiently discharges only carbon particles via an overflow method without loss of catalyst particles in the methane pyrolysis reactor, thereby improving the reliability of the high-purity hydrogen production process. means of solving the problem

[0006] According to one aspect of the present invention, a methane pyrolysis reactor may be provided, comprising: a reaction section in which the pyrolysis of methane gas and the generation of carbon particles take place; a gas inlet section for supplying fluidized gas to the reaction section; and a separation section for separating the carbon particles generated in the reaction section. Effects of the invention

[0007] The embodiments of the present invention provide a methane pyrolysis reactor that efficiently discharges only carbon particles via an overflow method without loss of catalyst particles in the methane pyrolysis reactor, and has the effect of improving the reliability of the high-purity hydrogen production process. Brief explanation of the drawing

[0008] FIG. 1 is a cross-sectional view of a methane pyrolysis reactor according to a first embodiment of the present invention. Figure 2 is a graph showing the fluidization rate of carbon particles and catalyst particles. Figure 3 is a graph showing the degree of mixing of catalyst particles and carbon particles according to the flow rate of the fluidizing gas. Figure 4 is a graph showing the height of the carbon particle layer according to the flow rate ratio of the fluidizing gas. FIG. 5 is a cross-sectional view of a methane pyrolysis reactor according to a second embodiment of the present invention. FIG. 6 is another cross-sectional view of a methane pyrolysis reactor according to a second embodiment of the present invention. Specific details for implementing the invention

[0009] Hereinafter, specific embodiments for implementing the technical concept of the present invention will be described in detail with reference to the drawings.

[0010] In addition, in describing the present invention, if it is determined that a detailed description of related known components or functions may obscure the essence of the invention, such detailed description is omitted.

[0011] Furthermore, when it is mentioned that one component is 'supplied,' 'communicated,' or 'connected' to another component, it should be understood that while it may be directly supplied, communicated, or connected to that other component, there may also be other components present in between.

[0012] The terms used in this specification are used merely to describe specific embodiments and are not intended to limit the invention. Singular expressions include plural expressions unless the context clearly indicates otherwise.

[0013] Furthermore, it should be noted in advance that expressions such as "upper side," "lower side," and "side" in this specification are described based on the drawings, and may be expressed differently if the orientation of the object changes. For the same reason, some components in the attached drawings may be exaggerated, omitted, or schematically depicted, and the size of each component does not entirely reflect its actual size.

[0014] Additionally, terms including ordinal numbers, such as first, second, etc., may be used to describe various components, but such components are not limited by such terms. These terms are used solely for the purpose of distinguishing one component from another.

[0015] The meaning of "comprising" as used in the specification is to specify certain characteristics, regions, integers, steps, actions, elements, and / or components, and does not exclude the existence or addition of other specific characteristics, regions, integers, steps, actions, elements, components, and / or groups.

[0016] Hereinafter, the specific configuration of a methane pyrolysis reactor according to an embodiment of the present invention will be described with reference to FIGS. 1 to 5. Referring to FIG. 1, a methane pyrolysis reactor (1) according to an embodiment of the present invention can pyrolyze methane gas (CH4) to produce hydrogen gas (H2) and solid carbon (C). The methane pyrolysis reactor (1) may include a gas inlet section (10), a reaction section (20), a separation section (30), and a control section (40).

[0017] The gas supply unit (4) can supply fluidizing gas to the methane pyrolysis reactor (1). The fluidizing gas supplied by the gas supply unit (4) may include methane gas. The fluidizing gas may further include a diluent gas for controlling flow. The diluent gas supplied by the gas supply unit (4) may be an inert gas. For example, the diluent gas may be nitrogen gas.

[0018] The gas inlet section (10) can receive fluidizing gas from the gas supply section (4). Additionally, the gas inlet section (10) can supply fluidizing gas to the reaction section (20). This gas inlet section (10) can be positioned below the reaction section (20).

[0019] The gas inlet section (10) may include a supply body (110), an inlet (120), and a gas dispersion plate (130).

[0020] Fluidized gas supplied from the gas supply unit (4) can flow in the supply unit body (110). In other words, methane gas or diluted gas can flow in the supply unit body (110). The fluidized gas or diluted gas contained in the supply unit body (110) can flow to the reaction unit (20). The supply unit body (110) may have a shape that extends in one direction. The cross-section of the supply unit body (110) may be a circle or a rectangle. The supply unit body (110) may have a shape in which the cross-sectional area narrows towards the bottom.

[0021] The inlet port (120) may provide a passage for supplying fluidizing gas from the gas supply unit (4) to the gas inlet unit (10). The inlet port (120) may be positioned on the lower side of the supply unit body (110). One side of the inlet port (120) may be in communication with the gas supply unit (4), and the other side may be in communication with the supply unit body (110). The inlet port (120) may be provided as a single port or as a plurality of ports. The inlet port (120) may be equipped with a backflow prevention device or a flow regulator to maintain the pressure of the incoming gas. Meanwhile, the supply speed of the fluidizing gas described below may be the speed of the empty bed based on the diameter of the supply unit body (110).

[0022] The gas dispersion plate (130) can be configured to uniformly supply fluidized gas to the reaction section (20). The gas dispersion plate (130) can be positioned on the upper side of the supply section body (110). This gas dispersion plate (130) can have a plate shape. Additionally, the edge of the gas dispersion plate (130) can be connected to the inner edge of the upper side of the supply section body (110). Furthermore, the gas dispersion plate (130) can physically block the flow of catalyst particles (2) from the reaction section (20) toward the supply section body (110), thereby preventing backflow of the catalyst particles (2).

[0023] For example, the gas distribution plate (130) may be formed from sintered metal, a perforated plate with fine holes, or a nozzle distributor having a plurality of fine nozzles. By forming the open surface area ratio of the fine holes or fine nozzles to about 10% or less, a constant differential pressure can be generated when supplying fluidizing gas. Through this differential pressure, the gas distribution plate (130) can uniformly supply fluidizing gas to the reaction section (20).

[0024] In the reaction section (20), methane gas is decomposed by heat, and carbon particles (3) can be generated. The reaction section (20) may be positioned above the gas inlet section (10). Catalyst particles (2) may be contained in the reaction section (20), and methane gas, fluidized gas, and carbon particles (3) may flow inside. The reaction section (20) may be cylindrical or rectangular in shape. The temperature in the reaction section (20) may be maintained at approximately 700 degrees or more and 900 degrees or less. This reaction section (20) may be heated by an external heater or plasma.

[0025] In the reaction section (20), a fluidizing gas may be flowed so that the catalyst particles (2) are suspended. In the reaction section (20), the catalyst particles (2) and carbon particles (3) may have different degrees of suspension due to differences in density. Depending on the difference in the degree of suspension of these catalyst particles (2) and carbon particles (3), a plurality of layered structures may be formed.

[0026] The minimum fluidization velocity may be the minimum velocity of the gas required for solid particles to float against gas drag and for fluidization to begin. The minimum fluidization velocity may include the catalytic minimum fluidization velocity and the carbon minimum fluidization velocity. The catalytic minimum fluidization velocity may be the minimum fluidization velocity of the catalytic particles (2), and the carbon minimum fluidization velocity may be the minimum fluidization velocity of the carbon particles (3).

[0027] Referring to FIG. 2, the graph shows the differential pressure according to the fluidization gas velocity of the catalyst particles (2) and carbon particles (3). Each graph shows the differential pressure when the height of the particle layer of the catalyst particles (2) and carbon particles (3) is varied to 1 / 3 and 2 / 3. In the graph of FIG. 2, the black dots indicate that when the height of the particle layer of the catalyst particles (2) and carbon particles (3) is greater than or equal to the minimum fluidization velocity of the catalyst, the catalyst particles (2) can maintain a floating state. When the fluidization gas velocity is greater than or equal to the minimum fluidization velocity of the carbon, the carbon particles (3) can maintain a floating state. In addition, the minimum fluidization velocity of the catalyst particles and the minimum fluidization velocity of the carbon particles may differ. FIG. 2 shows the minimum fluidization velocity when the catalyst particles (2) are silica, olivine, and zirconia. For example, the minimum fluidization velocity of the carbon particles (3) may be about 0.77 cm / s (see upper left of FIG. 2), the minimum fluidization velocity of silica may be about 8 cm / s (see upper right of FIG. 2), the minimum fluidization velocity of olivine may be about 22 cm / s (see lower left of FIG. 2), and the minimum fluidization velocity of zirconia may be about 9 cm / s (see lower right of FIG. 2). In other words, the minimum fluidization velocity of the catalyst may be greater than the minimum fluidization velocity of the carbon. As the flow rate of the fluidizing gas increases, the carbon particles (3) become floated first. Therefore, while the fluidizing gas is flowing, a layered structure may be formed in the reaction section (20) in which the carbon particles (3) float above the catalyst particles (2). The reaction section (20) may include a first region (210), a second region (220), a third region (230), and an outlet (240).

[0028] The first region (210) may be a region where the catalyst particles (2) exist in a stable or floating state. In other words, the catalyst particles (2) may be in a stable state in the first region (210) before the fluidizing gas is supplied. In other words, the catalyst particles (2) may be submerged and not floating in the first region (210) before the fluidizing gas is flowed. For example, the catalyst particles (2) may be silica, olivine, and zirconia. The catalyst particles (2) fixed in the first region (210) may be floating when the fluidizing gas is supplied at a rate greater than or equal to the minimum catalytic fluidization rate. The rate at which this fluidizing gas is supplied may be between 0.5 times and 2 times the minimum catalytic fluidization rate. The first region (210) may be connected to the gas dispersion plate (130). The first region (210) may be extended in one direction. The length of the first region (210) in one direction may be longer than the length in the other direction. For example, the length of the first region (210) in one direction may be at least 2 times and no more than 3 times the length in the other direction.

[0029] In the second region (220), catalyst particles (2) and carbon particles (3) produced by the thermal decomposition of methane gas may be mixed. In other words, the thermal decomposition of methane gas may begin in the lower part of the second region (220). In this second region (220), the fluidized gas and catalyst particles (2) may be thermally decomposed to produce carbon particles (3) and hydrogen gas.

[0030] The second region (220) may be positioned above the first region (210). The second region (220) may be cylindrical or rectangular in shape that communicates with the first region (210). The second region (220) may extend in one direction. The other direction of the second region (220) may be perpendicular to this one direction.

[0031] Referring to FIG. 3, the degree of mixing of the catalyst particles (2) and carbon particles (3) can be controlled by the flow rate of the fluidizing gas. When the flow rate of the fluidizing gas is less than or equal to twice the minimum fluidization speed of the catalyst particles, the mixing index (MI) is maintained at approximately 0.2 or less, allowing the separated state to be maintained. On the other hand, when the flow rate of the fluidizing gas increases to more than three times the minimum fluidization speed of the catalyst particles (2), a completely mixed state can be achieved where the mixing index (MI) approaches 1. In this state where the catalyst particles (2) and carbon particles (3) are mixed, it may be difficult to selectively separate only the carbon particles (3). Considering the mixing index of the catalyst particles (2) and carbon particles (3), the speed of the fluidizing gas can be set to between 0.5 times and 2 times the minimum fluidization speed of the catalyst particles (2) to allow the carbon particles (3) to be separated.

[0032] The third region (230) may exist in a state where carbon particles (3) are suspended. The third region (230) may be positioned above the second region (220). The third region (230) may be cylindrical or rectangular in shape that communicates with the second region (220). One direction of the third region (230) may be a direction that communicates with the second region (220). The other direction of the third region (230) may be perpendicular to this one direction. The length of the third region (230) in one direction may be shorter than the length of the first region (210) in one direction and the length of the second region (220) in one direction.

[0033] The outlet (240) can provide a passage for carbon particles (3) to be discharged from the reaction section (20) to the outside. In other words, the outlet (240) can provide a passage for carbon particles (3) to be discharged from the third area (230) to the discharge line (310). The third area (230) and the separation section (30) can be connected to each other through the outlet (240).

[0034] The separation section (30) can separate carbon generated in the reaction section (20) to the outside. One side of the separation section (30) is in communication with the third region (230), and the other side of the separation section (30) can be in communication with the outside. Referring again to FIG. 1, the separation section (30) is shown as being formed integrally with the gas inlet section (10) and the reaction section (20), but is not necessarily limited thereto and may be formed separately. The separation section (30) may include a discharge line (310), a discharge hopper (320), and a separation plate (330).

[0035] The discharge line (310) may provide a passage through which carbon particles (3) are discharged to the outside from the discharge port (240). The discharge line (310) may be cylindrical in shape extending from the discharge port (240). Along the discharge line (310), carbon particles (3) may be discharged to the discharge hopper (320) by gravity. One side of the discharge line (310) may be in communication with the discharge port (240), and the other side of the discharge line (310) may be in communication with the discharge hopper (320).

[0036] The discharge hopper (320) can discharge carbon particles (3) to the outside from the discharge line (310). The discharge hopper (320) may have a discharge opening that narrows toward the bottom. One side of the discharge hopper (320) is connected to the discharge line (310), and the other side of the discharge hopper (320) is connected to the outside.

[0037] The separator plate (330) may be configured to prevent the catalyst particles (2) from being discharged to the outside and to allow the carbon particles (3) to enter. The separator plate (330) may have a shape that extends upward from the discharge line (310) toward the center of the third region (230). In other words, the separator plate (330) may be extended at an angle so that the inner end is positioned higher than the outer end. The inner end of the separator plate (330) may be positioned higher than the degree to which the catalyst particles (2) float, so that the catalyst particles (2) are not discharged to the discharge port (240).

[0038] The operation and effects of the methane pyrolysis reactor (1) according to the first embodiment having the configuration described above will be explained below. The methane pyrolysis reactor (1) has the effect of selectively separating carbon particles (3) generated during the pyrolysis process of methane gas without loss of catalyst particles (2).

[0039] In the gas inlet section (10), fluidizing gas is uniformly supplied from the lower side of the reaction section (20) so that the catalyst particles (2) and carbon particles (3) can be stably separated. The gas dispersion plate (130) maintains a constant differential pressure to prevent backflow of the catalyst particles (2).

[0040] Referring to FIG. 4, when the fluidizing gas is supplied such that the ratio of the fluidizing gas flow rate (Ug / Umf, carbon) to the flow rate of the carbon particles (3) is approximately 1.5, the height of the third region (230) where the carbon particles (3) are suspended can increase by approximately 2.6 times (120~130 mm) compared to the initial height (80 mm). Since the expanded height of the carbon particles (3) is maintained stably without changing at a predetermined flow rate, the height of the third region (230) and the outlet (240) can be set to selectively separate only the carbon particles (3). In other words, the outlet (240) is positioned at the height where the carbon particles (3) are suspended, so that the catalyst particles (2) are not lost and the carbon particles (3) are stably discharged.

[0041] Meanwhile, in addition to this configuration, a methane pyrolysis reactor according to a second embodiment of the present invention may be provided. Hereinafter, a second embodiment of the present invention will be described with reference to FIGS. 5 and 6. In describing the second embodiment, the differences when compared with the above-described embodiment will be described mainly, and identical descriptions will be taken from the above-described embodiment.

[0042] The methane pyrolysis reactor (1) may further include a control unit (40). The control unit (40) can control the degree of extension in one direction or movement in the up and down direction of the separator plate (330). This control unit (40) may include a detection sensor (41), a movement assist member (42), and a controller (43).

[0043] The detection sensor (41) can detect the concentration of catalyst particles (2) or carbon particles (3) in the reaction section (20). The detection sensor (41) can be placed on the inner wall of the methane pyrolysis reactor (1). The detection sensor (41) can transmit information regarding the presence of catalyst particles (2) or carbon particles (3) in the third area (230) to the controller (43).

[0044] The movement assist member (42) can support the separation plate (330) and the discharge line (310) from the outside of the reaction unit (20) so that they can move in a sliding manner relative to the reaction unit (20). The movement assist member (42) may be in a form that surrounds the outer surface of the discharge line (310). One side of the movement assist member (42) may be connected to the discharge line (310), and the other side may be connected to the reaction unit (20). For example, the movement assist member (42) may be configured so that the discharge line (310) extends relative to the reaction unit (20) in the direction in which the reaction unit (20) extends (up and down direction in the drawing). In other words, the height of the discharge line (310) in the up and down direction relative to the inlet (120) can be adjusted by the sliding movement of the movement assist member (42) in the up and down direction. As another example, the movement assist member (42) may be configured so that the separator plate (330) extends in the direction in which the separator plate (330) extends relative to the reaction part (20) (in the diagonal direction in the drawing). In other words, the length of the separator plate (330) protruding into the reaction part (20) can be adjusted by the diagonal sliding movement of the movement assist member (42).

[0045] The controller (43) can adjust one or more of the degree of unidirectional extension of the separator plate (330) and the degree of vertical movement of the discharge line (310). The controller (43) can receive information from the detection sensor (31) regarding the presence of catalyst particles (2) or carbon particles (3) in the third region (230). The controller (43) can adjust the movement of the separation unit (30) in real time so that only carbon particles (3) are discharged from the reaction unit (20) to the separation unit (30) and catalyst particles (2) are not discharged.

[0046] Referring again to FIG. 5, the controller (43) can control the separator plate (330) to move in an extended direction to prevent the external discharge of the catalyst particle (2) when the catalyst particle (2) is detected in the third region (230). By the controller (43), the carbon particle (3) in the third region (230) may be separated into the separation section (30), and the catalyst particle (2) may not be separated into the separation section (30). For example, when the catalyst particle (2) is detected in the third region (230), the controller (43) can control the separator plate (330) to be further drawn in along the movement assist member (42) in the direction in which the discharge line (310) extends. The controller (43) can adjust the separator plate (330) to be drawn in the opposite direction to discharge more carbon particles (3) when the catalyst particles (2) are not detected in the third region (230) and only carbon particles (3) are detected.

[0047] Referring to FIG. 6 as another example, the controller (43) can adjust the discharge line (310) to move upward along the moving assist member (42) when catalyst particles (2) are detected in the third area (230). The controller (43) can adjust the separator plate (330) to move downward to discharge more carbon particles (3) when catalyst particles (2) are not detected and only carbon particles (3) are detected in the third area (230). The controller (43) can be implemented by a computing device including a microprocessor, and since the method of implementation is obvious to those skilled in the art, further detailed description is omitted.

[0048] The operation and effects of the methane pyrolysis reactor (1) according to the second embodiment having the configuration described above will be explained below. A controller (43) detects catalyst particles (2) and adjusts the height of the separator plate (330) so that carbon particles (3) are stably separated while the catalyst particles (2) are not lost, thereby effectively controlling the process.

[0049] Although the embodiments of the present invention have been described above as specific embodiments, they are merely examples and the present invention is not limited thereto, but should be interpreted as having the broadest scope in accordance with the technical concept disclosed in this specification. Those skilled in the art may implement patterns of shapes not specified by combining or substituting the disclosed embodiments, and this also does not deviate from the scope of the present invention. Furthermore, those skilled in the art may easily modify or alter the disclosed embodiments based on this specification, and it is evident that such modifications or alterations also fall within the scope of the rights of the present invention. Explanation of the symbols

[0050] 1: Methane pyrolysis reactor 2: Catalyst particles 3: Carbon particles 4: Gas supply unit 10: Gas inlet section 110: Supply section body 120: Inlet 130: Gas dispersion plate 20: Reaction section 210: First region 220: Area 2 230: Area 3 240: Outlet 30: Separator 310: Discharge line 320: Discharge hopper 330: Separator 40: Control unit 41: Detection sensor 42: Movement assist member 43: Controller

Claims

Claim 1 A reaction unit in which the pyrolysis of methane gas and the generation of carbon particles take place; a gas inlet unit for supplying fluidizing gas to the reaction unit; a separation unit for separating the carbon particles generated in the reaction unit; and a control unit are included, wherein the reaction unit comprises: a first region in which catalyst particles for the methane pyrolysis reaction exist in a suspended state; a second region disposed above the first region, in which the fluidizing gas is supplied from the gas inlet unit and the catalyst particles and the generated carbon particles are mixed; and a third region disposed above the second region in which the generated carbon particles exist in a suspended state, wherein the separation unit includes a separation plate having one side communicating with the third region and preventing the catalyst particles from being discharged from the third region, and the control unit comprises: a detection sensor for detecting the carbon particles or catalyst particles; and a movement assist member for assisting the movement of the separation plate. A methane pyrolysis reactor comprising a controller that receives concentration information of the carbon particles or the catalyst particles from the detection sensor and controls the movement of the separation plate so that the carbon particles are separated into the separation section and the catalyst particles are not separated into the separation section. Claim 2 A methane pyrolysis reactor according to claim 1, wherein the fluidizing gas comprises methane gas, and the gas inlet part is formed with an inlet for introducing the fluidizing gas and a gas dispersion plate for controlling the supply of the fluidizing gas. Claim 3 A methane pyrolysis reactor according to claim 1, wherein the reaction unit includes an outlet for discharging the carbon particles generated in the reaction unit to the separation unit. Claim 4 In claim 3, the separation unit further comprises a discharge hopper for discharging carbon particles from the reaction unit to the outside and a discharge line providing a passage for flow from the discharge port to the discharge hopper, a methane pyrolysis reactor. Claim 5 delete Claim 6 delete Claim 7 A methane pyrolysis reactor according to claim 1, wherein the reaction part is cylindrical or rectangular in shape, the vertical length of the first region is longer than the horizontal length, and the vertical length of the first region is at least 2 times and no more than 3 times the horizontal length. Claim 8 A methane pyrolysis reactor according to claim 1, wherein the vertical length of the third region is shorter than the vertical length of the first region and the vertical length of the second region. Claim 9 A methane pyrolysis reactor according to claim 1, wherein the gas inlet further supplies a diluent gas to control the supply of catalyst particles or the fluidizing gas. Claim 10 A methane pyrolysis reactor according to claim 1, wherein the catalyst particles are suspended at the minimum catalytic fluidization rate, and the fluidized gas flows at a rate of 0.5 times or more and 2 times or less the minimum catalytic fluidization rate. Claim 11 delete Claim 12 In claim 4, the discharge port is in communication with a part of the reaction section, and the separator plate is formed by extending from the discharge line in the direction of the third region, a methane pyrolysis reactor. Claim 13 A reaction unit in which the pyrolysis of methane gas and the generation of carbon particles take place; a gas inlet unit for supplying fluidizing gas to the reaction unit; a separation unit for separating the carbon particles generated in the reaction unit; and a control unit are included, wherein the reaction unit comprises: a first region in which catalyst particles for the methane pyrolysis reaction exist in a suspended state; a second region disposed above the first region, in which the fluidizing gas is supplied from the gas inlet unit and the catalyst particles and the generated carbon particles are mixed; and a third region disposed above the second region in which the generated carbon particles exist in a suspended state, wherein the reaction unit comprises an outlet for discharging the carbon particles generated in the reaction unit to the separation unit, and the separation unit comprises: a discharge hopper for discharging the carbon particles from the reaction unit to the outside; and a discharge line providing a passage for flow from the outlet to the discharge hopper. A methane pyrolysis reactor, wherein one side is in communication with the third region and includes a separator plate that prevents the catalyst particles from being discharged from the third region, and the control unit includes a sensing sensor that detects the carbon particles or catalyst particles; a movement assisting member that assists the movement of the separator plate; and a controller, wherein the movement assisting member assists the movement of the discharge line, and the controller controls the movement of the discharge line so that the carbon particles are separated into the separation unit and the catalyst particles are not separated into the separation unit.

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