Carbon peeling system

Abstract

To peel off solid carbon from a catalyst particle by simple processing.SOLUTION: A carbon peeling system 100 includes: a peeling tank 250 that stores catalyst particles with solid carbon attached thereto; a fluidizing gas supply part 160 that forms a fluidized bed of the catalyst particles by supplying an inert gas to the peeling tank 250; and an injection part 280 that includes one or a plurality of nozzles 282 and injects an inert gas to the fluidized bed formed in the peeling tank 250.SELECTED DRAWING: Figure 2

Description

[Technical Field]

[0001] The present disclosure relates to a carbon stripping system. [Background technology]

[0002] Technologies that use hydrogen as a fuel have been attracting attention in order to reduce carbon dioxide emissions, which are a cause of global warming. Technologies that produce hydrogen without emitting carbon dioxide have been developed by thermally decomposing hydrocarbons in the presence of catalyst particles to produce solid carbon.

[0003] In the above-mentioned technology using catalyst particles, solid carbon is generated on the surface of the catalyst particles, and as hydrocarbons continue to be thermally decomposed, the surface of the catalyst particles becomes covered with solid carbon, which reduces the functionality of the catalyst particles.

[0004] Therefore, as a technology for peeling off solid carbon from the surface of catalyst particles, a technology has been developed in which catalytic particles in which iron is supported as a catalyst on the surface of non-porous zirconia beads are used to perform thermal decomposition of hydrocarbons (for example, Patent Document 1).

[0005] In the technology of Patent Document 1, first, used catalyst particles are oxidized at high temperatures to separate the iron (specifically, iron and iron oxide) together with the solid carbon from the surface of the beads. Next, a magnet is used to separate the solid carbon and iron from the beads, and the beads are recovered. The surfaces of the recovered beads are then coated with new iron to regenerate the catalyst particles. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] Japanese Patent Publication No. 2021-155233 Summary of the Invention [Problem to be solved by the invention]

[0007] However, the conventional technology of coating zirconia beads with a catalyst, such as that described in Patent Document 1, requires oxidation treatment at high temperatures, separation treatment using a magnet, and coating treatment, which results in a high processing load for regenerating the catalyst particles.

[0008] In view of these problems, the present disclosure aims to provide a carbon stripping system that can strip solid carbon from catalyst particles through a simple process. [Means for solving the problem]

[0009] In order to solve the above problems, a carbon stripping system according to one embodiment of the present disclosure includes a stripping vessel that contains catalyst particles having solid carbon attached thereto, a fluidizing gas supply unit that supplies an inert gas to the stripping vessel to form a fluidized bed of the catalyst particles, and an injection unit that has one or more nozzles and injects the inert gas into the fluidized bed formed in the stripping vessel.

[0010] The carbon stripping system may further include a cyclone that separates the solid-gas mixture of solid carbon and inert gas discharged from the stripping tank, and either or both of the fluidizing gas supply unit and the injection unit may supply the inert gas separated by the cyclone to the stripping tank.

[0011] The carbon stripping system may further include a pyrolysis device that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank, a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the pyrolysis device, a catalyst discharge unit that discharges the catalyst particles having solid carbon attached thereto that are produced in the pyrolysis device into the stripping tank, a cyclone that separates the solid-gas mixture of solid carbon and inert gas discharged from the stripping tank, and a first heat exchanger that exchanges heat between the solid carbon separated by the cyclone and the raw material gas, and the raw material gas supply unit may supply the raw material gas that has been heat exchanged by the first heat exchanger to the pyrolysis device.

[0012] The carbon stripping system may further include a pyrolysis apparatus that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank, a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the pyrolysis apparatus, a catalyst discharge unit that discharges the catalyst particles having solid carbon attached thereto that are produced in the pyrolysis apparatus into the stripping tank, a cyclone that performs solid-gas separation on the solid-gas mixture of solid carbon and inert gas discharged from the stripping tank, and a second heat exchanger that exchanges heat between the raw material gas and the inert gas separated by the cyclone, and the raw material gas supply unit may supply the raw material gas that has been heat exchanged by the second heat exchanger to the pyrolysis apparatus.

[0013] The carbon stripping system further includes a pyrolysis device that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank, a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the pyrolysis device, and a catalyst discharge unit that discharges the catalyst particles with solid carbon attached thereto that are produced in the pyrolysis device into the stripping tank, and the fluidizing gas supply unit may supply an inert gas into the stripping tank so that the flow rate of the inert gas in the stripping tank is greater than the flow rate of the raw material gas in the pyrolysis device, thereby forming a fluidized bed of catalyst particles.

[0014] In order to solve the above problem, another carbon stripping system according to one embodiment of the present disclosure includes a pyrolysis device that accommodates catalyst particles, a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the pyrolysis device, a stripping tank that accommodates catalyst particles having solid carbon attached thereto, a fluidizing gas supply unit that supplies an inert gas into the stripping tank so that the flow rate of the inert gas in the stripping tank is greater than the flow rate of the raw material gas in the pyrolysis device, thereby forming a fluidized bed of catalyst particles, and a catalyst discharge device that discharges the catalyst particles having solid carbon attached thereto, which are produced in the pyrolysis device, into the stripping tank. [Effects of the Invention]

[0015] According to the present disclosure, it is possible to separate solid carbon from catalyst particles by a simple process. [Brief explanation of the drawings]

[0016] [Figure 1] FIG. 1 is a diagram illustrating a carbon peeling system according to a first embodiment. [Figure 2] FIG. 2 is a diagram illustrating the carbon peeling device and the fluidizing gas supply unit according to the first embodiment. [Figure 3] FIG. 3 is a diagram illustrating the flow of catalyst particles caused by the inert gas injected from the nozzle. [Figure 4] FIG. 4 is a diagram illustrating an ejection section according to a first modified example. [Figure 5] FIG. 5 is a diagram illustrating an ejection section according to a second modified example. [Figure 6] FIG. 6 is a cross-sectional view taken along line VI-VI in FIG. 5 as seen from above. [Figure 7] FIG. 7 is a diagram illustrating an ejection section according to a third modified example. [Figure 8] FIG. 8 is a diagram illustrating a carbon peeling device and a fluidizing gas supply unit according to the second embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0017] Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. Dimensions, materials, and other specific numerical values ​​shown in the embodiments are merely examples for ease of understanding and do not limit the present disclosure unless otherwise specified. In this specification and drawings, elements having substantially the same functions and configurations are designated by the same reference numerals to avoid redundant explanation. Elements not directly related to the present disclosure are not shown.

[0018] [First embodiment: carbon stripping system 100] Fig. 1 is a diagram illustrating a carbon stripping system 100 according to a first embodiment. As shown in Fig. 1, the carbon stripping system 100 includes a pyrolysis device 110, a raw material gas supply unit 120, a purification device 130, a catalyst discharge device 140, a carbon stripping device 150, a fluidizing gas supply unit 160, a cyclone 170, a first heat exchanger 172, a second heat exchanger 174, a bag filter 176, an exhaust device 178, and a catalyst supply device 180.

[0019] In FIG. 1 and in FIGS. 2 and 8 described below, solid arrows indicate the flow of solids, dashed arrows indicate the flow of gas, and dashed arrows indicate the flow of a solid-gas mixture.

[0020] The thermal decomposition device 110 thermally decomposes hydrocarbons to produce hydrogen and solid carbon. Hereinafter, methane will be taken as an example of hydrocarbon. In this embodiment, the thermal decomposition device 110 accommodates catalyst particles supplied from a catalyst supply device 180 (described later) and thermally decomposes methane using the catalyst particles. For example, in the thermal decomposition device 110, a fluidized bed of catalyst particles is formed by a raw material gas MG (described later). The thermal decomposition device 110 also includes a heating device (not shown), which heats the catalyst particles to, for example, about 900°C.

[0021] The catalyst particles are a catalyst that promotes the thermal decomposition reaction shown in the following formula (1). CH4→C + 2H2…Formula (1) The catalyst particles are, for example, iron-based catalysts (iron, iron ore), and have a particle size of, for example, 50 μm or more and 1000 μm or less, preferably 100 μm or more and 300 μm or less.

[0022] The raw material gas supply unit 120 supplies the raw material gas MG to the thermal decomposition apparatus 110. The raw material gas MG is a gas containing at least hydrocarbons. In this embodiment, the raw material gas supply unit 120 supplies the raw material gas MG to the thermal decomposition apparatus 110 after heat exchange by the second heat exchanger 174 and the first heat exchanger 172, which will be described later.

[0023] The raw material gas MG is, for example, liquefied natural gas (LNG). The raw material gas supply unit 120 is, for example, a blower. When the raw material gas supply unit 120 is a blower, the suction side of the blower is connected to a supply source of the raw material gas MG. In addition, the discharge side of the blower is connected to the thermal decomposition device 110.

[0024] In the thermal decomposition device 110, a mixed gas containing at least hydrogen (H), unreacted methane (CH), and solid carbon is generated. The mixed gas generated in the thermal decomposition device 110 is supplied to the purification device 130. The purification device 130 separates hydrogen from the mixed gas.

[0025] Furthermore, as the thermal decomposition reaction of methane progresses in the thermal decomposition device 110, solid carbon adheres to the surfaces of the catalyst particles. Therefore, when the amount of solid carbon adhering to the catalyst particles reaches a predetermined amount or more, or when the residence time of the catalyst particles in the thermal decomposition device 110 reaches a predetermined time or more, the catalyst discharger 140 discharges the catalyst particles with solid carbon attached thereto, which have been produced in the thermal decomposition device 110, into a stripping tank 250 of the carbon stripping device 150, which will be described later. Note that in this embodiment, the catalyst discharger 140 continuously discharges, for example, the catalyst particles with solid carbon attached thereto into the stripping tank 250. The catalyst discharger 140 transports the catalyst particles at a pressure of, for example, normal pressure to several kPa.

[0026] The carbon stripping device 150 strips solid carbon from the catalyst particles to which the solid carbon has adhered, which are produced in the pyrolysis device 110 .

[0027] 2 is a diagram illustrating the carbon separation apparatus 150 and the fluidizing gas supply unit 160 according to the first embodiment. As shown in FIG. 2, the carbon separation apparatus 150 includes a separation tank 250 and an injection unit 280.

[0028] The peeling tank 250 is a container that contains catalyst particles with solid carbon attached thereto, which are produced by the pyrolysis device 110. In this embodiment, the peeling tank 250 has, for example, a container section 252 and a bottom section 262.

[0029] The accommodation section 252 is a section that accommodates catalyst particles with solid carbon attached thereto and forms a fluidized bed of catalyst particles. The shape of the accommodation section 252 may be cylindrical or rectangular.

[0030] The bottom 262 is a portion that extends continuously downward from the lower end of the storage section 252. The horizontal cross-sectional area of ​​the bottom 262 gradually decreases, for example, from top to bottom. Similar to the storage section 252, the bottom 262 stores catalyst particles with solid carbon attached thereto. In addition, an outlet 262a is formed on the lower surface of the bottom 262. In this embodiment, the outlet 262a is formed in approximately the center of the bottom 262. The outlet 262a has a size that allows the catalyst particles to pass through. An outlet pipe 264 is connected to the outlet 262a.

[0031] The fluidizing gas supply unit 160 supplies an inert gas IG to the stripping vessel 250 to form a fluidized bed of catalyst particles (e.g., a bubbling fluidized bed). The inert gas IG is, for example, nitrogen gas, helium gas, argon gas, or carbon dioxide gas. The fluidizing gas supply unit 160 includes, for example, one or more air diffusers 162, a first blower 164, and a second blower 166.

[0032] The air diffuser 162 is provided within the accommodation section 252 and the bottom section 262. Specifically, the air diffuser 162 is provided within the catalyst particles accommodated within the accommodation section 252 and the bottom section 262. The air diffuser 162 is provided within the accommodation section 252 and the bottom section 262 so that its central axis is horizontal. A plurality of ventilation holes are formed in the air diffuser 162. The ventilation holes have a size that allows the inert gas IG to pass through but does not or has difficulty allowing the catalyst particles to pass through.

[0033] The first blower 164 supplies the inert gas IG to the diffuser pipe 162. The first blower 164 is, for example, a forced draft fan (FDF). The suction side of the first blower 164 is connected to a supply source of the inert gas IG. The discharge side of the first blower 164 is connected to the diffuser pipe 162. The first blower 164 may supply the inert gas IG to the diffuser pipe 162 so that the flow rate of the inert gas IG in the stripping tank 250 is equal to the flow rate of the raw material gas MG in the pyrolysis apparatus 110, or may supply the inert gas IG to the diffuser pipe 162 so that the flow rate of the inert gas IG in the stripping tank 250 is different from the flow rate of the raw material gas MG in the pyrolysis apparatus 110.

[0034] In this embodiment, the first blower 164 supplies the inert gas IG to an injector 280, which will be described later. The discharge side of the first blower 164 is connected to the injector 280 in addition to the air diffuser 162.

[0035] The second blower 166 supplies the inert gas IG separated by the cyclone 170 (described later) to the air diffuser 162 and the injection unit 280 via the first blower 164. The suction side of the second blower 166 is connected to the bag filter 176. The discharge side of the second blower 166 is connected between the suction side of the first blower 164.

[0036] The injection unit 280 has one or more nozzles 282. The injection unit 280 injects an inert gas I into the fluidized bed formed in the accommodation unit 252. This allows the injected inert gas I to peel off solid carbon from the catalyst particles.

[0037] The injector 280 injects the inert gas IG with a momentum greater than the momentum of the catalyst particles that form the fluidized bed in the storage unit 252. For example, the momentum of the inert gas IG injected by the injector 280 is at least twice, preferably at least five times, and more preferably at least ten times the momentum of the catalyst particles in the storage unit 252. This makes it possible to enhance the effect of the injected inert gas IG in stripping solid carbon from the catalyst particles.

[0038] For example, when the momentum of the catalyst particles is 2500 [Nm], the momentum of the inert gas IG injected by the injection unit 280 is 27000 [Nm].

[0039] The flow velocity of the inert gas IG injected by the injection part 280 is, for example, equal to or less than the speed of sound (343 [m / s]).

[0040] Furthermore, the diameter of the opening of the nozzle 282 is determined, for example, based on the diameter of the container 252. For example, the diameter of the opening of the nozzle 282 is determined so as to satisfy the following formula (2). (Va / U0)^0.5 ≦ dr / dn ≦ 5×(Va / U0)^0.5 …Equation (2) In the above formula (2), dr represents the diameter [m] of the accommodation section 252. dn represents the diameter [m] of the opening of the nozzle 282. Va represents the flow velocity [m / s] of the inert gas IG injected from the opening of the nozzle 282. U0 represents the superficial velocity [m / s] of the fluidizing gas supplied into the accommodation section 252.

[0041] Furthermore, the distance L between the opening of the nozzle 282 and the upper surface of the fluidized bed is preferably more than 0 and not more than 20 times the diameter dn of the opening of the nozzle 282. This makes it possible to enhance the effect of the injected inert gas IG in stripping solid carbon from the catalyst particles. The upper surface of the fluidized bed is where the bubbles burst in the fluidized bed.

[0042] In this embodiment, the inert gas IG is ejected from the nozzle 282 in a vertical direction, for example.

[0043] Fig. 3 is a diagram illustrating the flow of catalyst particles caused by the inert gas IG injected from the nozzle 282. In Fig. 3, solid black arrows indicate the flow of the inert gas IG injected from the nozzle 282. Also, in Fig. 3, hollow arrows indicate the flow of catalyst particles toward the outlet 262a.

[0044] 3, for example, the opening of the nozzle 282 is preferably disposed directly above the discharge port 262a, and the direction of the inert gas IG sprayed from the nozzle 282 is preferably vertical. This allows the jet of inert gas IG to collide evenly with the upper surface of the fluidized bed, thereby enhancing the effect of the sprayed inert gas IG in stripping solid carbon from the catalyst particles. Then, the catalyst particles from which the solid carbon has been removed can be guided to the discharge port 262a.

[0045] In this way, by providing the injection unit 280, the injected inert gas IG can efficiently separate solid carbon from the catalyst particles.

[0046] Returning to FIG. 2 , the catalyst particles from which solid carbon has been removed are extracted from the peeling tank 250 by the catalyst supply device 180 and supplied to the pyrolysis device 110. The catalyst supply device 180 transports the catalyst particles at a pressure of, for example, atmospheric pressure to several kPa. In this embodiment, the catalyst supply device 180 includes a screw feeder 182, a rotary valve 184, a hopper 186, and a rotary valve 188. The screw feeder 182 is connected to the discharge pipe 264 and the rotary valve 184. The screw feeder 182 transports the catalyst particles from the peeling tank 250 to the hopper 186. The rotary valve 184 adjusts the amount of catalyst particles transported from the peeling tank 250 to the hopper 186. The hopper 186 is provided above the pyrolysis device 110. The catalyst particles stored in the hopper 186 are supplied to the pyrolysis device 110 by their own weight. The rotary valve 188 adjusts the amount of catalyst particles delivered from the hopper 186 to the pyrolysis device 110 .

[0047] Meanwhile, in the storage section 252, the solid carbon separated from the catalyst particles is supplied to the cyclone 170 together with the inert gas IG.

[0048] Returning to FIG. 1 , the cyclone 170 separates the solid-gas mixture of solid carbon and inert gas IG discharged from the stripping tank 250. The solid carbon separated by the cyclone 170 is supplied to a first heat exchanger 172. The inert gas IG separated by the cyclone 170 is supplied to a second heat exchanger 174.

[0049] The first heat exchanger 172 exchanges heat between the solid carbon separated by the cyclone 170 and the raw material gas MG. The first heat exchanger 172 heats the raw material gas MG with the heat contained in the solid carbon. This cools the solid carbon. The cooled solid carbon is transported to a downstream solid carbon utilization facility. The solid carbon is used as a nanocarbon material or mixed into structural materials such as asphalt and concrete. In this embodiment, the first heat exchanger 172 exchanges heat between the raw material gas MG after heat exchange by the second heat exchanger 174 and the solid carbon.

[0050] The second heat exchanger 174 exchanges heat between the inert gas IG separated by the cyclone 170 and the raw material gas MG. The second heat exchanger 174 heats the raw material gas MG with the heat of the inert gas IG. This cools the inert gas IG. The cooled inert gas IG is supplied to the bag filter 176.

[0051] The bag filter 176 removes dust from the inert gas IG. The exhaust device 178 exhausts the inert gas IG from the bag filter 176. The exhaust device 178 is, for example, an induced draft fan (IDF).

[0052] As described above, the carbon stripping system 100 according to this embodiment includes the stripping vessel 250, the fluidizing gas supply unit 160, and the injection unit 280. This allows a fluidized bed of catalyst particles to be formed in the stripping vessel 250, while an inert gas Ig is injected into the fluidized bed of catalyst particles. Therefore, solid carbon can be stripped from catalyst particles by a simple process of simply injecting the inert gas Ig.

[0053] The injector 280 also injects the inert gas IG toward the upper surface of the fluidized bed. This allows the inert gas IG to be injected into the dilute layer formed above the fluidized bed. The dilute layer is the region in the fluidized bed where bubbles burst. The density of catalyst particles in the dilute layer is lower than that in the lower part of the dilute layer. Therefore, by injecting the inert gas IG into the dilute layer, it is possible to suppress the attenuation of the jet flow and increase the energy imparted from the jet flow to the catalyst particles. This makes it possible to efficiently peel off solid carbon from the catalyst particles.

[0054] As described above, the fluidizing gas supply unit 160 (second blower 166) supplies the inert gas IG separated by the cyclone 170 to the stripping tank 250 through the air diffuser 162. This allows the inert gas IG to be reused, thereby reducing the cost of the inert gas IG.

[0055] Similarly, the fluidizing gas supply unit 160 (second blower 166) supplies the inert gas IG separated by the cyclone 170 to the stripping tank 250 through the injection unit 280. This allows the inert gas IG to be reused, thereby reducing the cost of the inert gas IG.

[0056] As described above, the carbon peeling system 100 also includes the first heat exchanger 172. This allows the raw material gas MG to be preheated by the solid carbon separated by the cyclone 170. This allows the heating energy required by the heating device 220 of the pyrolysis device 110 to be reduced.

[0057] As described above, the carbon peeling system 100 also includes the second heat exchanger 174. This allows the raw material gas MG to be preheated by the inert gas IG separated by the cyclone 170. This allows the heating energy required by the heating device 220 of the pyrolysis device 110 to be reduced.

[0058] [Variations] Fig. 4 is a diagram illustrating a jetting unit 280 according to a first modified example. As shown in Fig. 4, the nozzle 282 of the jetting unit 280 according to the first modified example is provided in the stripping tank 250 at an angle relative to the vertical direction. Therefore, the jetting direction of the inert gas IG jetted from the nozzle 282 of the jetting unit 280 according to the first modified example is a direction intersecting the vertical direction.

[0059] In this way, by injecting the jet of inert gas (IG) into the fluidized bed at an angle, the contact area between the jet and the fluidized bed can be increased. This makes it possible to increase the number of catalyst particles that collide with the jet of inert gas (IG). Therefore, it is possible to further enhance the effect of the injected inert gas (IG) in stripping solid carbon from the catalyst particles.

[0060] Fig. 5 is a diagram illustrating an injection unit 280 according to a second modified example. Fig. 6 is a diagram showing a cross section taken along line VI-VI in Fig. 5 as viewed from above. For ease of understanding, catalyst particles are omitted from Fig. 6.

[0061] As shown in FIGS. 5 and 6, when the storage section 252 has a large horizontal cross-sectional area and the stripping tank 250 has multiple bottom sections 262 and multiple discharge ports 262a, the carbon stripping system 100 may have the same number of injection units 280 as the number of discharge ports 262a. Furthermore, when the discharge port 262a is formed approximately at the center of the bottom section 262 as shown in FIGS. 5 and 6, for example, it is preferable that the openings of the multiple nozzles 282 are each positioned directly above the multiple discharge ports 262a, and the direction of the inert gas IG sprayed from the nozzles 282 is vertical. This allows the jet of inert gas IG to collide evenly with the upper surface of the fluidized bed, thereby enhancing the effect of stripping solid carbon from the catalyst particles by the injected inert gas IG. Then, the catalyst particles from which the solid carbon has been removed can be guided to each of the multiple discharge ports 262a.

[0062] Fig. 7 is a diagram illustrating a spray unit 280 according to a third modified example. As shown in Fig. 7, when the discharge outlet 262a is formed eccentrically from approximately the center of the bottom 262, for example, the opening of the nozzle 282 may be disposed at a different horizontal position from the discharge outlet 262a. Even in this case, it is preferable that the openings of the nozzle 282 be provided approximately evenly on the upper surface of the fluidized bed.

[0063] This allows the jet of inert gas (IG) to collide evenly with the upper surface of the fluidized bed, enhancing the effect of the injected inert gas (IG) in stripping solid carbon from the catalyst particles. The catalyst particles from which the solid carbon has been removed can then be guided to each of the multiple outlets 262a.

[0064] [Second embodiment] 8 is a diagram illustrating a carbon peeling apparatus 350 and a fluidizing gas supply unit 360 according to the second embodiment. As shown in FIG. 8, the carbon peeling apparatus 350 according to the second embodiment includes a peeling tank 250 but does not include an injection unit 280. The fluidizing gas supply unit 360 includes one or more air diffusers 162, a first blower 364, and a second blower 166. Note that components that are substantially the same as those in the carbon peeling system 100 described above are denoted by the same reference numerals, and description thereof will be omitted.

[0065] The first blower 364 of the fluidizing gas supply unit 360 supplies the inert gas IG to the diffuser pipe 162. In this embodiment, the first blower 364 supplies the inert gas IG to the diffuser pipe 162 so that the flow rate of the inert gas IG in the stripping vessel 250 is greater than the flow rate of the raw material gas MG in the pyrolysis apparatus 110. The first blower 364 supplies the inert gas IG to the diffuser pipe 162 so that the flow rate of the inert gas IG in the stripping vessel 250 is, for example, 1.5 to 10 times the flow rate of the raw material gas MG in the pyrolysis apparatus 110 and is equal to or greater than the minimum fluidization speed of the catalyst particles before the solid carbon is stripped.

[0066] As a result, the carbon peeling device 150 according to the second embodiment can increase the frictional force between catalyst particles due to the fluidized bed without including the injection unit 280. Therefore, the peeling tank 250 can efficiently peel off solid carbon adhering to the surfaces of the catalyst particles.

[0067] Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the above-described embodiments. It is clear that a person skilled in the art can conceive of various modifications or alterations within the scope of the claims, and it is understood that these also naturally fall within the technical scope of the present disclosure.

[0068] For example, in the first and second embodiments, the fluidizing gas supply units 160, 360 supply the inert gas IG separated by the cyclone 170 to the stripping vessel 250. However, the fluidizing gas supply units 160, 360 do not have to supply the inert gas IG separated by the cyclone 170 to the stripping vessel 250. In this case, the fluidizing gas supply units 160, 360 supply only new inert gas IG to the stripping vessel 250.

[0069] Similarly, the fluidizing gas supply unit 160 does not have to supply the inert gas IG separated by the cyclone 170 to the injection unit 280. In this case, the fluidizing gas supply unit 160 supplies only new inert gas IG to the injection unit 280.

[0070] In the first embodiment described above, the case where the raw material gas MG is supplied to the first heat exchanger 172 after heat exchange with the second heat exchanger 174 has been exemplified. However, the raw material gas MG may be supplied to the second heat exchanger 174 after heat exchange with the first heat exchanger 172. The raw material gas MG is preferably heat exchanged in order from the heat exchanger with the lowest temperature of the raw material gas MG after heat exchange.

[0071] In the first embodiment, the carbon peeling system 100 includes the first heat exchanger 172. However, the first heat exchanger 172 is not an essential component.

[0072] In the first embodiment, the carbon peeling system 100 includes the second heat exchanger 174. However, the second heat exchanger 174 is not an essential component.

[0073] Furthermore, in the first embodiment, the first blower 164 may supply the inert gas IG to the air diffuser 162 so that the flow rate of the inert gas IG in the stripping tank 250 is greater than the flow rate of the raw material gas MG in the pyrolysis apparatus 110. This increases the frictional force between the catalyst particles due to the fluidized bed. Therefore, the stripping tank 250 can more efficiently strip solid carbon adhering to the surfaces of the catalyst particles.

[0074] In the first embodiment, the fluidizing gas supply unit 160 supplies the inert gas IG to the spray unit 280. However, an inert gas supply unit separate from the fluidizing gas supply unit 160 may be provided, and the inert gas supply unit may supply the inert gas IG to the spray unit 280. Furthermore, the inert gas IG supplied from the air diffuser 162 into the stripping tank 250 and the inert gas IG supplied from the spray unit 280 into the stripping tank 250 may be different types of inert gas IG.

[0075] Furthermore, in the second modified example described above, an example was given in which the same number of ejection units 280 as the number of discharge ports 262a are provided. However, there is no limit to the number of ejection units 280. For example, when there is one discharge port 262a, the plurality of ejection units 280 may be arranged so that the openings of the plurality of nozzles 282 are arranged on a concentric circle centered on the discharge port 262a.

[0076] Furthermore, the jet of inert gas IG injected from the nozzle 282 gradually expands at a predetermined injection angle (for example, 7°). Therefore, multiple injection units 280 may be arranged based on the injection angle and the distance L between the opening of the nozzle 282 and the upper surface of the fluidized bed so that the jet collides evenly with the upper surface of the fluidized bed.

[0077] In the first embodiment, the second blower 166 sucks in the inert gas IG from between the bag filter 176 and the exhaust device 178. This reduces the capacity of the exhaust device 178. However, the second blower 166 may suck in the inert gas IG from the discharge side of the exhaust device 178. In this case, the second blower 166 can suck in the inert gas IG at high pressure, so the pressure-boosting capacity of the second blower 166 can be reduced.

[0078] In the first embodiment, the discharge side of the second blower 166 is connected to the suction side of the first blower 164. This makes it possible to suppress pulsation of the inert gas IG supplied to the carbon peeling device 150. However, the discharge side of the second blower 166 may be connected to the discharge side of the first blower 164.

[0079] This disclosure can, for example, contribute to Sustainable Development Goal (SDG) 7: "Ensure access to affordable, reliable, sustainable and modern energy." [Explanation of symbols]

[0080] IG Inert Gas MG raw material gas 100 Carbon Stripping System 110 Pyrolysis equipment 120 Raw material gas supply unit 140 Catalyst discharge device 160 Fluidization gas supply section 170 Cyclone 172 1st heat exchanger 174 Second heat exchanger 250 Peeling tank 280 Injection part 360 Fluidization gas supply section

Claims

1. a stripping vessel for accommodating catalyst particles having solid carbon attached thereto; a fluidizing gas supply unit that supplies an inert gas to the stripping tank to form a fluidized bed of the catalyst particles; an injection unit having one or more nozzles and configured to inject an inert gas into the fluidized bed formed in the stripping tank; A carbon stripping system comprising:

2. a cyclone for separating a solid-gas mixture of the solid carbon and the inert gas discharged from the stripping tank, The carbon stripping system according to claim 1 , wherein either or both of the fluidizing gas supply unit and the injection unit supply the inert gas separated by the cyclone to the stripping tank.

3. a pyrolysis device that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank; a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the pyrolysis apparatus; a catalyst discharge device that discharges the catalyst particles having solid carbon attached thereto, which are generated in the pyrolysis device, into the peeling tank; a cyclone for separating a solid-gas mixture of the solid carbon and the inert gas discharged from the stripping tank into solid and gas; a first heat exchanger for exchanging heat between the solid carbon separated by the cyclone and the raw material gas; Further equipped with The carbon peeling system according to claim 1 , wherein the raw material gas supplying unit supplies the raw material gas that has been heat exchanged by the first heat exchanger to the pyrolysis device.

4. a pyrolysis device that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank; a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the pyrolysis apparatus; a catalyst discharge device that discharges the catalyst particles having solid carbon attached thereto, which are generated in the pyrolysis device, into the peeling tank; a cyclone for separating a solid-gas mixture of the solid carbon and the inert gas discharged from the stripping tank into solid and gas; a second heat exchanger for exchanging heat between the inert gas separated by the cyclone and the raw material gas; Further equipped with The carbon peeling system according to claim 1 , wherein the raw material gas supplying unit supplies the raw material gas that has been heat exchanged by the second heat exchanger to the pyrolysis device.

5. a pyrolysis device that accommodates catalyst particles having an amount of solid carbon attached thereto that is equal to or less than the amount of solid carbon attached to the catalyst particles accommodated in the stripping tank; a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the pyrolysis apparatus; a catalyst discharge device that discharges the catalyst particles having solid carbon attached thereto, which are generated in the pyrolysis device, into the peeling tank; Further equipped with 3. The carbon stripping system according to claim 1, wherein the fluidizing gas supply unit supplies the inert gas into the stripping tank so that the flow rate of the inert gas in the stripping tank is greater than the flow rate of the raw material gas in the pyrolysis apparatus, thereby forming a fluidized bed of the catalyst particles.

6. a pyrolysis device containing catalyst particles; a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the pyrolysis apparatus; a stripping vessel for accommodating the catalyst particles having solid carbon attached thereto; a fluidizing gas supply unit that supplies the inert gas into the stripping tank so that the flow rate of the inert gas in the stripping tank is greater than the flow rate of the raw material gas in the pyrolysis apparatus, thereby forming a fluidized bed of the catalyst particles; a catalyst discharge device that discharges the catalyst particles having the solid carbon attached thereto, which are produced in the pyrolysis device, into the stripping tank; A carbon stripping system comprising:

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