KR102416196B1 - Device for thermal decomposition of methane - Google Patents

Abstract

The present invention relates to a pyrolyzing device of methane capable of securing operation stability of a pyrolyzing reactor by controlling a temperature for each position of the pyrolyzing reactor when generating hydrogen and carbon by pyrolyzing the methane; maintaining reactivity of methane pyrolysis; and easily separating and discharging hydrogen gas and carbon particles. A configuration of the present invention comprises: a container body; a reaction container; a heat-resistant container; an insulating material; and a cyclone separating device. The container body is made of a stainless material, and has a structure of opening and closing an inner accommodating space through a cover provided in an upper end unit. The reaction container is made of a quartz; is installed in the accommodating space of the container body; has a state of heating catalyst metal filled in an inner reaction space excluding an upper end unit and a lower end unit and melting the same; allows the lower end unit to be connected to a methane supply pipe provided outside of the container body; and connects a hydrogen supply pipe and a hydrogen and carbon discharge pipe in the upper end unit. The heat-resistant container is made of a graphite material with an opened inside to surround the entire reaction container excluding the upper end unit inside the container body; and allows a plurality of heaters to be installed on the outer circumferential surface. The insulating material is interposed between the inner circumferential surface of the container body and the outer circumferential surface of the heat-resistant container in which the heaters are installed, and is installed to form a shape surrounding the entire reaction container. The cyclone separating device is provided outside the container body to be connected to the hydrogen and carbon discharge pipe; and includes: a hydrogen circulation pipe, a hydrogen outlet pipe, and a carbon outlet pipe.

Description

Device for thermal decomposition of methane

The present invention relates to a pyrolysis device for methane, and specifically, in pyrolyzing methane to generate hydrogen and carbon, controlling the temperature for each location of the pyrolysis reactor to ensure operation stability of the pyrolysis reactor, and methane pyrolysis It relates to a thermal decomposition device for methane that can maintain the degree of reactivity of methane and can easily separate and discharge hydrogen gas and carbon particles.

Until now, industries have mostly developed using coal and oil as energy sources, but now, due to the depletion of coal and oil, butane, propane, or natural gas is used in many parts of homes and industries as alternative energy sources based on hydrogen. .

In view of this trend, it is expected that an energy source based on hydrogen will lead the industrial society in the near future.

Hydrogen is the lightest and most abundant element, and is a clean energy source with infinite resources.

Therefore, hydrogen energy technology is recognized as the only alternative that can simultaneously solve the energy and environmental problems of the 21st century.

Therefore, in order to establish a technology for producing, storing and using hydrogen, related research is being conducted very actively around the world under the leadership of technologically advanced countries including the United States, Japan, or Europe.

Methods of hydrogen production technology are broadly classified into three categories: methods based on hydrocarbon substances such as methane steam reforming, partial oxidation of heavy oil, or catalytic cracking of natural gas, and non-hydrocarbons such as thermochemical or electrochemical water cracking. There are a method based on the method and a method combining the above two types.

In particular, as for the hydrogen production method using the thermal decomposition method of methane, a method for obtaining a thermal decomposition rate of 90% or more at a temperature of 1,000° C. or less using a molten metal catalyst method is being studied.

Carbon nanotubes (CNTs) can be produced at low temperatures in the form of carbon produced by pyrolysis, so it can be purified and sold at a high price, which is excellent in economic feasibility.

However, the current hydrogen production method using the pyrolysis method of methane has not reached the stage of manufacturing large-capacity commercial facilities at the level of exploring various possibilities at the laboratory level in terms of the level of technology.

Specifically, methane is thermally decomposed in the vicinity of the bubble generator of the molten metal catalyst (for example, a bismuth (Bi)-based one- or binary-based metal catalyst) and carbon blocks the micropores of the bubble generator, or high temperature ( At about 1,000 ° C.), the mechanical strength of the reactor made of quartz is low, making it difficult to maintain its shape, but it is necessary to improve the phenomenon of carbon fusion as well as irregular growth of the particles due to the high temperature of the upper part of the reactor.

Korean Patent Publication No. 10-2004-0004799 (published on January 16, 2004) Republic of Korea Patent Publication No. 10-2144472 (2020.08.13. Announcement)

An object of the present invention is to prevent clogging of pores due to deposition of carbon in the vicinity of a bubble generator, and to maintain an optimum temperature by supplying sufficient heat to a pyrolysis reactor to promote pyrolysis reaction of methane. to provide the device.

At the same time, the pyrolysis of methane, which suppresses the reaction by lowering the temperature of the upper part of the pyrolysis device to prevent carbon bonding, reinforces the strength of the reactor made of quartz, and forms a structure of a pressure-resistant reactor that withstands operating pressure It will be said that providing a device is also an object of the present invention.

Methane pyrolysis device according to the present invention for achieving the above object, the container body is made of a stainless material, the container body forming a structure in which the receiving space inside can be opened and closed through a cover provided on the upper end; A methane supply pipe made of a quartz material and installed in the receiving space of the vessel body, the catalyst metal filled in the inner reaction space except for the upper end and the lower end is heated to a molten state, and the lower end is provided on the outside of the vessel body and a reaction vessel in which a hydrogen supply pipe and a hydrogen and carbon discharge pipe are connected and installed at the upper end; a heat-resistant container made of a graphite material having an open inner side so as to cover the entire inside of the container body except for the upper end of the reaction container, and a plurality of heaters are installed on the outer circumferential surface; an insulator interposed between the inner circumferential surface of the container body and the outer circumferential surface of the heat-resistant container in which the heater is installed, as well as being installed to form a shape surrounding the entire reaction container; and a cyclone separator provided on the outside of the container body to form a connection with the hydrogen and carbon discharge pipe, and having a hydrogen circulation pipe, a hydrogen outlet pipe and a carbon outlet pipe.

The reaction vessel includes a quartz bubble generating member connected to the methane supply pipe at the lower end thereof, and the bubble generating member is formed with a plurality of bubble generating holes arranged at equal intervals so that the methane supplied from the methane supply pipe is It can be thermally decomposed by the catalytic action of the catalytic metal and the temperature of the catalytic metal surface while rising while forming bubbles with the molten catalytic metal.

In the reaction vessel, the temperature of the section before the methane supplied through the methane supply pipe passes through the bubble generating member and the section in which hydrogen and carbon at the upper end are discharged is 400 ° C. The temperature of the section where methane starts to rise while forming bubbles and the section where methane is thermally decomposed to separate into hydrogen and carbon may be 600° C., and the temperature of the section where methane is thermally decomposed may be 1,000° C.

The reaction vessel may be provided with a cover at the upper end to maintain the seal of the reaction space formed inside, thereby preventing particles of carbon and catalyst metal from scattering in the receiving space inside the vessel body.

The electric heater may be disposed on the outer peripheral surface of the heat-resistant vessel corresponding to the portion filled with the catalyst metal in the reaction vessel.

The hydrogen supply pipe may be connected to the hydrogen circulation pipe, and a blower is installed at a connection portion between the hydrogen supply pipe and the hydrogen circulation pipe, and the hydrogen outlet pipe may be provided in a branched form from the hydrogen circulation pipe.

The cyclone separator may separate and discharge gaseous hydrogen and powdery carbon discharged through the hydrogen and carbon discharge pipe to the hydrogen circulation pipe and the carbon outlet pipe, respectively.

The cyclone separator further includes a carbon transfer and ejector connected to, the carbon transfer and ejector, the screw conveyor is connected to the carbon outlet pipe to transfer the discharged carbon powder; a storage chamber in which the carbon powder transferred by being connected to the screw conveyor is stored; and a discharge valve installed at the lower end of the storage chamber.

According to the configuration of the present invention described above, the operating pressure can be appropriately set through the pressure maintaining action of the container body, the shape and size of the reaction container can be freely designed by applying the heat-resistant container, and a plurality of electric heaters can be applied to It has the effect of controlling the temperature for each section.

And, by controlling the temperature of each section of the reaction vessel, the temperature of the section to which methane is supplied can be controlled to low, thereby suppressing the decomposition reaction of methane to prevent clogging caused by carbon deposition, and in the section where methane is decomposed By maintaining the temperature at about 900 to 1,000 ° C, the decomposition reaction rate of methane can be controlled to more than 95%, and by maintaining the temperature at the upper part of the reaction vessel at about 600 ° C, the bond between the catalyst metal and carbon is suppressed and the separation process is carried out at the same time. There is an effect that can make you lose.

In addition, through the configuration of the hydrogen circulation pipe, carbon powder rides the hydrogen stream, exits the upper part of the reaction vessel and the body body, and has an automatic discharge function that is centrifuged in the cyclone separator, so that continuous operation is possible.

In addition, it is possible to reduce the consumption of operating energy through the application of the insulating material, and to secure the safety of operation by maintaining the temperature of the container body at room temperature, as well as to realize convenient operation.

The pyrolysis device for methane having such an effect can be operated continuously for a long time, and it can also be made small in size, and the product hydrogen can be used for hydrogen fuel cells, etc. An effect that can be obtained as a nanotube or the like and used as a material for various industries can also be expected.

1 to 4 are views schematically showing a pyrolysis device for methane according to the present invention.

Hereinafter, with reference to the accompanying drawings, preferred embodiments for implementing the above-described object of the present invention will be described and operational relationships according to these configurations will be described. do it with

In the present invention, in pyrolysis of methane to generate hydrogen and carbon, the temperature of each position of the pyrolysis reactor is controlled to ensure operation stability of the pyrolysis reactor, and the reactivity of methane pyrolysis can be maintained, and hydrogen gas and It relates to a pyrolysis device for methane that allows for easy separation and discharge of carbon particles.

For this, the configuration of the methane thermal decomposition apparatus according to the present invention is, as shown in FIGS. 1 to 3, the container body 10, the reaction container 20, the heat-resistant container 30, the heat insulating material 40, and the cyclone separator. (50) may be included.

The container body 10 of the present invention is made of a stainless steel material, and has a structure in which the receiving space 12 inside can be opened and closed through the cover 11 provided at the upper end. There is a technical point to it.

The container body 10 may have a structure in which a hydrogen supply pipe 22, which will be described later, and a hydrogen and carbon discharge pipe 23 are connected to the upper part, and a methane supply pipe M is connected to the lower part.

The pressure structure of the container body 10 may function to stably maintain the pressures of methane and hydrogen at an operating pressure (eg, 5 atmospheres) at room temperature or at a temperature above room temperature.

For example, the temperature of the container body 10 is preferably maintained so as not to be higher than about 20 ℃ higher than the ambient temperature of the factory or laboratory.

In addition, inside the pressure structure of the vessel body 10, a reaction vessel 20 made of a quartz material to be described later, which is the main device of the methane thermal decomposition reaction, and a heat-resistant vessel 30 made of a catalytic metal and graphite material, the reaction vessel 20 There are structural features in that the protective structure, the installation of the heater 31, and the high-temperature insulating material 40 can be mounted.

The reaction vessel 20 of the present invention is made of a quartz material that does not react with catalytic metal, methane, carbon and hydrogen, and is installed in the receiving space 12 of the vessel body 10, excluding the upper end and the lower end. The catalyst metal filled in the reaction space 21 is heated to form a molten state, the lower end is connected to the methane supply pipe M provided on the outside of the container body 10, and the hydrogen supply pipe 22 and hydrogen are at the upper end And the carbon discharge pipe 23 may be connected and installed.

The reaction vessel 20 may be provided with a bubble generating member 24 made of a quartz material that is connected to the methane supply pipe M at the lower end thereof, and the bubble generating member 24 is also a catalyst metal similar to the reaction vessel 20 . , through the property of not reacting with methane, carbon and hydrogen, it is possible to maintain its installation shape as it is.

The bubble generating member 24 is formed with a plurality of bubble generating holes 24a arranged at equal intervals to form bubbles with the catalytic metal in a state in which the methane supplied from the methane supply pipe M is melted and rises by buoyancy. It can be thermally decomposed by the temperature of the surface of the catalyst metal and the catalytic action of the catalyst metal, for example, the bubble generating hole 24a may have a diameter of about 5 mm.

By disposing the bubble generating member 24 in which the plurality of bubble generating holes 24a are formed in the lower part of the reaction vessel 20, methane gas can be infiltrated into the molten catalytic metal and can be operated to improve the reactivity. do.

For example, as shown in FIG. 3 , the methane supply pipe M is inserted through the upper portion of the reaction vessel 20 and is integral with the bubble generating member 24 disposed at the lower end of the reaction vessel 20 as a methane supply pipe assembly. It may be provided, and in this case, it is preferable that the methane supply pipe (M) is also made of a quartz material.

In addition, the catalyst metal is heated above the melting point in a state filled with solid powder or small pieces in the reaction vessel 20 to melt and maintain the filled state in a liquid state.

The reaction vessel 20 is provided with a cover 25 at the upper end to maintain the seal of the reaction space 21 formed inside, so that particles of carbon and catalyst metal are scattered in the receiving space 12 inside the vessel body 10 . It can be prevented, and this cover 25 may also be made of a quartz material.

The hydrogen supply pipe 22 and the hydrogen and carbon discharge pipe 23 may be installed to be mounted on the upper end of the reaction vessel 20 .

The reaction vessel 20 is inserted into a heat-resistant container 30 made of a graphite material, which will be described later, can be installed to be mounted on the container body 10, and has a tubular shape having a diameter smaller than the diameter of the heat-resistant container 30 when manufactured. is manufactured and inserted into the inside of the heat-resistant container 30 so that it can be assembled, and after assembling, a catalyst metal is injected into the inner reaction space 21 and heated to increase the temperature, forming a form of close contact with the inner circumferential surface of the heat-resistant container 30 structure can be achieved.

For example, the reaction vessel 20 is formed in a shape that expands the cross-sectional area of the upper end so that hydrogen bubbles and carbon powder are stably separated from the catalyst metal, so that mixing of the catalyst metal into the carbon powder can be suppressed. .

The heat-resistant container 30 of the present invention is made of a graphite material of an open shape so as to surround the entirety except for the upper end of the reaction container 20 from the inside of the container body 10, and a plurality of (eg, For example, three or four) of the heaters 31 may be installed.

The heat-resistant container 30 is installed to be fastened to the container body 10 to support the reaction container 20 at a high temperature, and the inner circumferential surface forms a shape corresponding to the outer circumferential surface of the reaction vessel 20, and the outer circumferential surface is an electric heater It is desirable to have a structure in which the temperature sensor installed in the reaction vessel 20 can pass through, as well as being manufactured so that the installation of 31 and the installation of the heat insulating material 40 to be described later can be facilitated.

For example, the heat-resistant vessel 30 may have a height up to the upper surface of the catalyst metal filled in the reaction vessel 20 as shown in FIGS. 1 to 3 .

As described above, through the organic coupling relationship between characteristics such as thermal conductivity or heat resistance strength of the reaction vessel 20 made of a quartz material and the heat resistant vessel 30 made of a graphite material supporting the reaction vessel 20, it is necessary in the operation process. It becomes possible to control the thermal diffusion.

In addition, it is also possible to control the temperature of the catalyst metal by applying the thermal conductivity of the heat-resistant container 30 made of a graphite material to transfer heat to a region requiring thermal diffusion.

The heater 31 is installed on the outer circumferential surface of the heat-resistant container 30 in order to implement active heat control. make it possible

The heater 31 may be installed to be attached to the outer circumferential surface of the heat-resistant vessel 30, and may have a structure in which the outside is wrapped with an insulating material 40 to be described later, and the catalyst metal in the reaction vessel 20 It is disposed on the outer circumferential surface of the heat-resistant container 30 corresponding to the filled portion to implement a structure for controlling the temperature distribution of the reaction region.

For example, the three electric heaters 31 may be controlled by dividing the reaction area through the electric heater 31 into three equal parts.

The capacity of the electric heater 31 may be calculated as a starting (required for heating time) capacity (P_start) and a required operating capacity (P_operate), and a large value may be selected.

The starting capacity of the electric heater 31 is obtained by obtaining a time constant (τ) from the thermal resistance (R) and the thermal capacity (C) of the pyrolysis reactor (reaction vessel 20), the target temperature (Th) and the ambient temperature (Tamb) Calculate the operating temperature difference (ΔT_operate) from

Since the operating temperature difference is ΔT_operate=R*Qoperate and the starting temperature difference is ΔT_start=n*ΔT_operate=n*R*Qoperate=R*Qstart, Qstart=n*Qoperate.

When the heat of Qstart is injected into the equipment, the time to reach ΔT_operate (t_start) is t_start=-τ*LN[(n-1)/n].

For example, if τ=5 minutes n=1.1, then t_operate=20 minutes (98%), if τ=5 minutes n=1.1, t_start=12 minutes, τ=5 minutes n=1.2, then t_start=9 minutes, τ =5 minutes If n=1.3, then t_start=7.33 minutes.

Approximately three or four of these heaters 31 are mounted and individually (parallel) controlled according to the temperature characteristics of the temperature sensor or device to maintain the optimum temperature for each location.

The insulating material 40 of the present invention is interposed between the inner circumferential surface of the container body 10 and the outer circumferential surface of the heat-resistant container 30 in which the heater 31 is installed, as well as the entire reaction container 20, in order to implement passive heat control. It is installed to form an enveloping shape, thereby suppressing heat loss to the outside, and the temperature of the lower part of the device can be obtained by utilizing the heat conduction of the heat-resistant container 30 .

The insulating material 40 surrounds the outside of the heat-resistant container 30 and the heater 31, and can be installed to be inserted between the upper part of the reaction container 20 and the upper part of the container body 10, and the heat-resistant container 30 The outer peripheral surface is about 1,000 ℃, the inner peripheral surface of the container body 10 is about 20 ℃ it is preferable to use a high-temperature insulating material.

The heat insulating material 40 can be applied to the installation structure for mounting the heat-resistant container 30 to the container body 10 to achieve an installation that is fastened to form an insulating structure, and a structure that reduces the temperature rise of the fastening part in the container body 10 It is desirable to achieve

Meanwhile, the insulator 40 is installed between the heat-resistant container 30 and the container body 10 on which the heater 31 is mounted to reduce the heat loss of the heat-resistant container 30, and to maintain the container body 10 at room temperature. It serves to prevent a decrease in strength.

In this way, temperature control through the electric heater 31 and the heat insulating material 40, as shown in FIGS. 1 and 2, specifically in the reaction vessel 20, the methane supplied through the methane supply pipe (M) is a bubble generating member The temperature of the section (a) before passing through (24) and the section (b) in which hydrogen and carbon at the upper end are discharged is 400° C., and the methane that has passed through the bubble generating member 24 rises while forming bubbles. The temperature of the starting section (c) and the section (d) where methane is thermally decomposed to separate into hydrogen and carbon is 600 ° C, and the temperature of the section (e) where methane is thermally decomposed can be controlled and maintained at 1,000 ° C. .

Here, the above-described temperature for each location or section can be changed, and the technical gist of it is that active and passive temperature control through the heater 31 and the insulator 40 is possible.

However, the lowest temperature among the above-mentioned temperatures is set to a temperature higher than the melting point of the catalyst metal by 100 ° C. It is preferable to set the temperature of the section in which the thermal decomposition is performed to an optimal temperature in the range of 900 to 1,000 °C.

The cyclone separator 50 of the present invention is provided on the outside of the container body 10 to form a connection with the hydrogen and carbon discharge pipe 23, and a hydrogen circulation pipe 51, a hydrogen outlet pipe 52 and a carbon outlet pipe ( 53) may be configured.

Here, the hydrogen supply pipe 22 is connected to the hydrogen circulation pipe 51 , and a blower 54 is installed at the connection portion of the hydrogen supply pipe 22 and the hydrogen circulation pipe 51 , and the hydrogen outlet pipe 52 . may be provided in a branched form in the hydrogen circulation pipe 51 .

The cyclone separator 50 separates and discharges hydrogen and gaseous hydrogen and powdery carbon discharged through the carbon discharge pipe 23 into the hydrogen circulation pipe 51 and the carbon outlet pipe 53, respectively.

Specifically, hydrogen gas and carbon powder generated through thermal decomposition of methane are ejected from the upper portion of the reaction vessel 20, so that the carbon powder is blown into hydrogen gas to be separated in the reaction vessel 20. In the present invention, the operation The hydrogen gas at a pressure (eg, 5 atmospheres) is blown back by the blower 54 to form a structure in which the hydrogen gas mixed with the carbon powder is blown to the outside of the container body 10 .

The carbon powder and hydrogen gas blown out of the container body 10 are separated by a cyclone separator 50 to a significant portion of the carbon powder through the carbon outlet pipe 53, and the blower 54 is operated to operate the reaction vessel 20. The operation of blowing hydrogen gas to the upper part to blow carbon powder can be continuously performed to achieve circulation.

That is, hydrogen generated by thermal decomposition of methane is circulated through the blower 54 to blow carbon powder into the air stream to be discharged.

The hydrogen gas thus generated is discharged through the hydrogen outlet pipe 52 after passing through the cyclone separator 50. At this time, since the discharge pressure must be maintained, the pressure of the container body 10 is higher than the operating pressure (set pressure). It is preferable to have a pressure reaction valve so that hydrogen is discharged through the hydrogen outlet pipe 52 when it is done.

Since the hydrogen discharged from the methane pyrolysis device according to the present invention may contain fine powder carbon particles, it is preferable to also provide a carbon removal filter to discharge through it.

Furthermore, if the pressure of the container for storing the discharged hydrogen is equal to or higher than the operating pressure of the methane pyrolysis device according to the present invention, the generated hydrogen is supplied through the provided hydrogen compression pump and compressed so that it can be stored in the storage container.

In addition, the methane thermal decomposition apparatus according to the present invention may further include a carbon transfer and discharge unit 60 that is connected to the cyclone separator 50 .

The carbon transfer and discharge machine 60 of the present invention, as shown in FIG. 4, is connected to the carbon outlet pipe 53 and connected to the screw conveyor 61 for transferring the discharged carbon powder, and the screw conveyor 61 is connected. It may be configured to include a storage chamber 62 in which the transferred carbon powder is stored, and a discharge valve 63 installed at the lower end of the storage chamber 62 .

Through this, it is possible to continuously discharge carbon without stopping the hydrogen obtaining process through thermal decomposition of methane, for example, the discharge valve 63 applies a rotary valve to discharge the carbon powder transferred to the storage chamber 62 to the outside. can do.

In the present invention, the above embodiment is an example, and the present invention is not limited thereto. Anything that has substantially the same configuration as the technical idea described in the claims of the present invention and achieves the same operation and effect is included in the technical scope of the present invention.

10: container body 11: cover
12: accommodation space 20: reaction vessel
21: reaction space 22: hydrogen supply pipe
23: hydrogen and carbon discharge pipe 24: bubble generating member
24a: bubble generating hole 25: cover
30: heat-resistant container 31: electric heater
40: insulation material 50: cyclone separator
51: hydrogen circulation pipe 52: hydrogen outlet pipe
53: carbon outlet pipe 54: blower
60: carbon transfer and ejector 61: screw conveyor
62: storage chamber 63: discharge valve
M: methane supply pipe

Claims (8)

a container body made of a stainless steel material and having a structure in which the receiving space inside can be opened and closed through a cover provided at an upper end thereof;
A methane supply pipe made of a quartz material and installed in the receiving space of the vessel body, the catalyst metal filled in the inner reaction space except for the upper end and the lower end is heated to a molten state, and the lower end is provided on the outside of the vessel body and a reaction vessel in which a hydrogen supply pipe and a hydrogen and carbon discharge pipe are connected and installed at the upper end;
a heat-resistant container made of a graphite material having an open inner side so as to cover the entire inside of the container body except for the upper end of the reaction container, and a plurality of heaters are installed on the outer circumferential surface;
an insulator interposed between the inner circumferential surface of the container body and the outer circumferential surface of the heat-resistant container in which the heater is installed, as well as being installed to form a shape surrounding the entire reaction container; and
A cyclone separator provided on the outside of the container body to form a connection with the hydrogen and carbon discharge pipe, the cyclone separator having a hydrogen circulation pipe, a hydrogen outlet pipe and a carbon outlet pipe; including,
The methane thermal decomposition device, characterized in that the electric heater is disposed on the outer peripheral surface of the heat-resistant vessel corresponding to the portion filled with the catalyst metal in the reaction vessel.
According to claim 1,
The reaction vessel is provided with a bubble generating member made of quartz material that is connected to the methane supply pipe at the lower end,
The bubble generating member is formed with a plurality of bubble generating holes arranged at equal intervals, and the methane supplied from the methane supply pipe forms bubbles with the catalytic metal in a molten state and rises while rising, the temperature of the catalytic metal surface and the catalytic action of the catalytic metal A pyrolysis device for methane, characterized in that it is pyrolyzed by
3. The method of claim 2,
in the reaction vessel,
The temperature of the section before the methane supplied through the methane supply pipe passes through the bubble generating member and the section in which hydrogen and carbon at the upper end are discharged is 400° C.,
The temperature of the section where methane that has passed through the bubble generating member starts to rise while forming bubbles and the section where methane is thermally decomposed to separate into hydrogen and carbon is 600 ° C,
A pyrolysis device for methane, characterized in that the temperature of the section where methane is thermally decomposed is 1,000 °C.
According to claim 1,
The reaction vessel is provided with a cover at the upper end to maintain the airtightness of the reaction space formed inside to prevent particles of carbon and catalyst metal from scattering in the receiving space inside the vessel body.
delete According to claim 1,
The hydrogen supply pipe is connected to the hydrogen circulation pipe,
A blower is installed at the connection part of the hydrogen supply pipe and the hydrogen circulation pipe,
The hydrogen outlet pipe is a pyrolysis device for methane, characterized in that provided in a branched form from the hydrogen circulation pipe.
7. The method of claim 6,
The cyclone separator separates and discharges gaseous hydrogen and powdery carbon discharged through the hydrogen and carbon discharge pipe to the hydrogen circulation pipe and the carbon outlet pipe, respectively.
According to claim 1,
Further comprising a carbon transfer and discharge unit connected to the cyclone separator,
The carbon transfer and discharge device,
a screw conveyor connected to the carbon outlet pipe to transport the discharged carbon powder;
a storage chamber in which the carbon powder transferred by being connected to the screw conveyor is stored; and
A pyrolysis device for methane comprising a; a discharge valve installed at the lower end of the storage chamber.

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