KR20240062164A - Regenerative Turquoise Hydrogen production system - Google Patents

Abstract

The present invention includes a preheater (200) for preheating methane; A solid-phase heat exchanger (300) that heats the methane preheated in the preheater (200) through heat exchange; and a reactor (410, 420) that directly pyrolyzes the heated methane to produce hydrogen and solid carbon and includes a heat storage material, wherein the hydrogen produced in one of the reactors includes: The solid carbon generated in one of the reactors is introduced into the solid-gas heat exchanger 300 and exchanged heat, and methane direct pyrolysis is performed in one of the reactors 410 and 420, and the reactor 410, 420), the other provides a blue-green hydrogen production system in which some of the heat-exchanged hydrogen is reacted to store heat, and one of the reactors and the other reactor are operated alternately.

Description

Regenerative Turquoise Hydrogen production system

The present invention relates to hydrogen production equipment and production methods.

Depending on the production method, hydrogen is classified into gray hydrogen produced from fossil fuels, green hydrogen produced using water electrolysis, and turquoise hydrogen produced through direct pyrolysis of methane.

Gray hydrogen requires heat and water during production, while green hydrogen requires water and electricity during production, and both generate a large amount of greenhouse gas (CO2). In contrast, blue-green hydrogen is produced through a direct thermal decomposition reaction in which CH4 is decomposed into two H2 and C(s), so it theoretically has the advantage of no greenhouse gas (CO2) emissions during the hydrogen acquisition process.

Blue-green hydrogen is a recently researched concept, and the production system for it has not yet been established. However, theoretically, it is reported that energy is needed to allow the reactor to reach about 1200 degrees Celsius to produce blue-green hydrogen through direct pyrolysis of methane, so this energy is required. Greenhouse gases may be emitted during the production process. However, if the induction heating method using renewable energy power or the hydrogen combustion method that reuses some of the blue-green hydrogen is used, even the greenhouse gases emitted when generating the energy needed to produce blue-green hydrogen can be minimized or suppressed. can do. As an example of a hydrogen combustion method, if hydrogen is produced using about 15% of the actual hydrogen produced as fuel, blue-green hydrogen can be produced without any other energy such as electricity. In theory, to produce 1 ton of blue-green hydrogen, 4,712 kg of methane is directly pyrolyzed to produce 3,526 kg of carbon and 1,184 kg of hydrogen, of which 184 kg of hydrogen is used as fuel. If 184kg (about 15%) of 1,184kg of hydrogen is used as fuel, 1 ton of hydrogen is produced as a carbon-free fuel.

In this way, producing blue-green hydrogen using induction heating or hydrogen combustion has the advantage of being environmentally friendly, but a high level of combustion control is required due to the high reactivity of hydrogen. Moreover, even in this environment, a difficult process is required that must organically and comprehensively consider various aspects to ensure stable productivity and increase energy efficiency.

For example, direct pyrolysis of methane requires the reactor to reach a significant temperature of approximately 1200 degrees Celsius, so technology is needed to efficiently control the energy required to reach or maintain that temperature. At the same time, devices are needed to maintain stable productivity despite various environmental variables.

Review relevant patent literature. As mentioned above, since patent literature on blue-green hydrogen cannot yet be confirmed, patent literature related to general hydrogen production was reviewed.

U.S. Patent No. 10,577,242 discloses an apparatus for producing high purity hydrogen with a biomass pyrolysis unit, and discloses a system in which three hydrogen generation units have a loop and generate continuously. Among the three units, heat from the unit that is not operating is used as waste heat. This is not a literature on blue-green hydrogen. In addition, although alternating reactions are carried out in three reactors, a separate raw material preheating process is not performed and hydrogen combustion is not used, so energy efficiency is low and a lot of greenhouse gases are expected to be emitted.

Korean Patent No. 10-2211017 discloses a technology for securing hydrogen and carbon by pyrolyzing biogas using solar energy and steam. It is close to green hydrogen and leads to securing heat storage performance using heat storage materials.

Korean Patent No. 10-1832136 relates to a regenerative combustion steam reforming device, which desulfurizes hydrocarbons as raw materials and purifies high-purity hydrogen in the PSA unit using flowing steam. Preheating is performed using a heat exchanger, but the disadvantage is that productivity is not high due to the use of one reactor.

US Patent No. 10,577,242 Korean Patent No. 10-2211017 Korean Patent No. 10-1832136

The present invention was created to solve the above problems.

We would like to propose a highly productive blue-green hydrogen production system by utilizing a thermal storage system and a pyrolysis system together.

A temperature of over 1200 degrees is required for direct pyrolysis of methane, and a lot of energy is required to achieve this, and greenhouse gases can also be generated significantly. The present invention minimizes greenhouse gas emissions and also minimizes and improves efficiency of the energy required to maintain temperature. I would like to propose a system that can do this.

One embodiment of the present invention to solve the above problems includes a preheater 200 for preheating methane; A solid-phase heat exchanger (300) that heats the methane preheated in the preheater (200) through heat exchange; and a reactor (410, 420) that directly pyrolyzes the heated methane to produce hydrogen and solid carbon and includes a heat storage material, wherein the hydrogen produced in one of the reactors includes: The solid carbon generated in one of the reactors is introduced into the solid-gas heat exchanger 300 and exchanged heat, and methane direct pyrolysis is performed in one of the reactors 410 and 420, and the reactor 410, 420), the other provides a blue-green hydrogen production system in which some of the heat-exchanged hydrogen is reacted to store heat, and one of the reactors and the other reactor are operated alternately.

In addition, it is preferable to further include a hydrogen turbine or PSA (Pressure Swing Absorption) 600 through which another part of the heat-exchanged hydrogen flows into the solid-phase heat exchanger 300.

In addition, it is preferable to further include a carbon storage tank 500 into which solid-phase carbon that has been heat-exchanged flows into the solid-phase heat exchanger 300.

In addition, it is preferable that water vapor and nitrogen are generated as heat storage occurs in the other reactor, and the generated water vapor and nitrogen flow into the preheater 200 to provide heat.

In addition, it is preferable to further include a Heat Recovery Steam Generator (HRSG) 700 in which water vapor and nitrogen that provide heat from the preheater 200 are introduced and heat is recovered.

In addition, the heat storage material included in the reactors 410 and 420 preferably includes solid carbon generated in one of the reactors.

In addition, the heated methane discharged from the solid-phase heat exchanger 300 flows to any one of the reactors 410 and 420 by the first valve V1, and flows to any one of the reactors 410 and 420. The hydrogen generated in each flows into one pipe by the second valve (V2) and then flows into the solid-phase heat exchanger 300, and the solid phase generated in one of the reactors 410 and 420, respectively. Carbon is preferably introduced into one pipe through the third valve (V3) and then into the solid-phase heat exchanger (300).

In addition, the heat-exchanged hydrogen discharged from the solid-gas heat exchanger 300 is divided into the part and the other part by the fourth valve V4, and the part of the hydrogen is transferred to another one of the reactors 410 and 420. It flows and reacts for heat storage, and the other part of the hydrogen flows to the hydrogen turbine or PSA (600), and the part of the hydrogen flows only to one of the reactors (410, 420) by the fifth valve (V5). It is desirable to float.

In addition, it is preferable that the water vapor and nitrogen generated in the other one of the reactors 410 and 420 are introduced into one pipe through the sixth valve V6 and then flow to the preheater 200.

In addition, each of the reactors (410, 420) is equipped with a sensor (S1, S2) that measures the internal temperature, and in the sensor provided in any one of the reactors (410, 420) where methane direct thermal decomposition is performed When the temperature measured for a predetermined period of time tends to decrease, it is preferable that one of the reactors is switched to a reactor in which heat storage is performed and the other reactor is switched to a reactor in which direct methane thermal decomposition is performed.

In addition, a sensor (S3) for measuring the internal temperature is provided in the pipe connecting the second valve (V2) and the solid-phase heat exchanger (300), and the temperature measured by the sensor (S3) for a predetermined time When there is a decreasing trend, it is preferable that one of the reactors is switched to a reactor in which heat storage is performed and the other reactor is switched to a reactor in which direct methane thermal decomposition is performed.

According to the present invention, the following effects are achieved.

Without a heat storage system, energy efficiency is low because energy must be constantly supplied to maintain a temperature of about 1200 degrees Celsius for direct pyrolysis of methane. However, the present invention has excellent energy efficiency due to the warming effect through the heat storage system.

Since part of the produced hydrogen is used as fuel, there are no greenhouse gas emissions during this process. In particular, the temperature of the hydrogen produced in the reactor reaches about 1200 degrees Celsius, and the heat is used to preheat methane through a heat exchanger. Even though the temperature is lowered in this process, it reaches about 200 degrees Celsius, so the highly reactive hydrogen can be used as heat storage. It flows into the reactor and shows high reactivity. The reaction of hydrogen generates water vapor and nitrogen at a temperature of about 500 degrees Celsius, and this heat is also used for preheating methane and heat recovery in the HRSG, so the overall energy efficiency of the system is considerably excellent.

Rather than simply using a reactor containing a heat storage material, two or more reactors are operated alternately so that hydrogen is produced in one and heat storage is performed in one or more of the other reactors, so if the productivity of the reactor that produces hydrogen decreases. By detecting this and switching the reactor, a decrease in productivity of the entire system can be prevented and stable productivity can be maintained. Additionally, the complexity of operation can be avoided by automating switching using multiple sensors.

Multiple valves and control methods were adopted so that most of the flow pipes could be operated as one, even though two or more reactors were used. As a result, piping maintenance is less complicated and initial investment costs are reduced.

Since gas phase hydrogen and solid phase carbon are separated within the reactor, there is no need to provide a separate carbon separation device in the system.

Figure 1 schematically shows a system according to the invention.
Figures 2 and 3 show an operation method of the system according to the present invention.
Figure 4 shows productivity when utilizing a system according to the present invention.

Hereinafter, the present invention will be described in more detail with reference to the drawings.

Note that the hydrogen produced below refers to blue-green hydrogen produced by direct thermal decomposition of methane.

The temperature of each fluid material is explained below, but please note that this is only an example for explanation purposes and that the temperatures may change depending on surrounding environmental conditions during actual system operation.

1. Description of the system

Referring to Figure 1, a blue-green hydrogen production system according to the present invention will be described.

The system according to the present invention includes an LNG storage tank 100 in which liquefied natural gas (LNG) containing methane is stored, a preheater 200 for preheating the methane transferred from here to room temperature, and methane preheated to about 300 degrees Celsius. A solid-phase heat exchanger (300) that heats by heat exchange, two or more reactors (410, 420) that directly pyrolyze the heated methane and store heat through alternating operation, and solid-phase carbon produced by direct pyrolysis of methane. A carbon storage tank (500) collected after heat exchange, a hydrogen turbine or PSA (Pressure Swing Absorption) (600) collected after heat exchange of gaseous hydrogen generated by direct pyrolysis of methane, and a reaction of hydrogen for heat storage. It includes a Heat Recovery Steam Generator (HRSG) 700 to recover latent heat from the generated water vapor and nitrogen after heat exchange for preheating.

The preheater 200 performs the function of preheating methane at room temperature until it flows to about 300 degrees Celsius.

The heat source for the preheater 200 is water vapor and nitrogen at about 500 degrees Celsius generated by a reaction of hydrogen in a heat storage reactor among the reactors 410 and 420. As will be described later, one of the reactors (410, 420) performs direct thermal decomposition of methane to produce hydrogen and carbon, and the other of the reactors (410, 420) reacts with a portion of the hydrogen produced here to produce heat storage. In the process of reacting hydrogen and air for heat storage, water vapor and nitrogen at about 500 degrees Celsius are generated, and these flow to the preheater 200 to provide heat. After providing heat to the preheater (200), the water vapor and nitrogen become less than 200 degrees Celsius, and they flow to the HRSG (200) to recover more latent heat and increase energy efficiency.

The solid-vapor phase heat exchanger 300 performs a heat exchange function to allow the methane at about 300 degrees Celsius introduced from the preheater 200 to reach about 900 degrees Celsius.

The heat source for the solid-vapor phase heat exchanger 300 is solid-phase carbon and gaseous hydrogen at about 1200 degrees Celsius produced by direct pyrolysis of methane in the reactors 410 and 420. In other words, both solid carbon and gaseous hydrogen exchange heat. As will be described later, one of the reactors (410, 420) performs direct thermal decomposition of methane to generate hydrogen and carbon at about 1200 degrees Celsius, which flow into one solid-phase heat exchanger (300) to provide heat. . The gas-phase hydrogen and solid-phase carbon heat-exchanged in the solid-phase heat exchanger (300) are at about 200 degrees Celsius, and they flow to the hydrogen turbine or PSA (600) and carbon storage tank (500), respectively, to be used in the downstream process. At this time, some of the hydrogen flows into the reactor that performs heat storage and becomes fuel for heat storage.

In one embodiment of the present invention, solid carbon stored in the carbon storage tank 500, that is, carbon generated by the present system, can be directly used as a heat storage material for the reactors 410 and 420. Through this, operating costs required for facility investment and replacement can be reduced.

The reactors (410, 420) can perform a heat storage function by including a heat storage material, and provide thermal insulation performance during direct pyrolysis of methane.

The reactors 410 and 420 are composed of two or more reactors and are operated alternately. If one reactor performs direct thermal decomposition of methane, the other reactor performs heat storage through a reaction using some of the generated hydrogen. That is, if one of the reactors 410 and 420 is a reactor that performs heat storage (hereinafter, “thermal storage reactor”), the other is a reactor that performs methane direct pyrolysis (hereinafter, “methane direct pyrolysis reactor”). However, note that in the switching process described later, two functions may be performed simultaneously.

Although two reactors are shown in the drawing, the number may be three or more. For example, if direct thermal decomposition of methane is performed in one reactor, thermal storage may be performed in one or more other reactors.

In the reactors 410 and 420, gaseous hydrogen and solid carbon are produced through direct thermal decomposition of methane. The reactors 410 and 420 according to the present invention adopt separate pipes for discharging gaseous hydrogen and solid phase carbon. By forcing gaseous and solid materials into the pipe, there is no need to install a separate carbon separation device at the rear of the reactors (410, 420).

The thermal storage reactor utilizes a portion of the hydrogen produced in the system of the present invention. When hydrogen is produced by the methane direct pyrolysis reactor, it is heat exchanged in the solid-phase heat exchanger (300) to reach about 200 degrees Celsius, and some of it flows to the hydrogen turbine or PSA (600) and the other part flows to the thermal storage reactor.

When hydrogen at about 200 degrees Celsius flows into the thermal storage reactor, a reaction occurs with air, and heat is generated accordingly, which is stored in the thermal storage material contained in the reactor. Since hydrogen at about 200 degrees Celsius, rather than hydrogen at room temperature, is introduced, reactivity is excellent and heat storage performance is also excellent.

During the hydrogen reaction process, water vapor and nitrogen of about 500 degrees Celsius are generated, which flow to the preheater 200 and become a heat source, where the temperature is lowered to about 200 degrees Celsius or less, which then flows to the HRSG (700) to generate heat. This is retrieved once more.

Meanwhile, when methane at a temperature of about 900 degrees Celsius is introduced into the methane direct pyrolysis reactor, thermal decomposition occurs, producing gaseous hydrogen and solid carbon, and the temperature reaches about 1200 degrees Celsius. They flow to the solid-phase heat exchanger 300 through different pipes and exchange heat.

The solid-phase carbon heat-exchanged in the solid-phase heat exchanger 300 becomes about 200 degrees Celsius and is stored in the carbon storage tank 500.

Hydrogen heat-exchanged in the solid-phase heat exchanger 300 also becomes about 200 degrees Celsius and flows into the hydrogen turbine or PSA 600, and some of it flows into the heat storage reactor and is utilized, as described above.

Meanwhile, the system according to the present invention builds a system using multiple valves to ensure smooth productivity by enabling automated operation and reducing the number of pipes that must be managed.

A first valve (V1) is provided in the pipe that flows to the methane direct pyrolysis reactor after heat exchange in the solid-phase heat exchanger 300. By controlling the first valve (V1), the methane direct pyrolysis reactor and the thermal storage reactor can be selected.

The lines through which the hydrogen generated in each reactor (410, 420) is discharged flow into one pipe through the second valve (V2) and then into the solid-phase heat exchanger (300). Likewise, the solid carbon generated in each reactor (410, 420) flows into one pipe through the third valve (V3) and then flows into the solid-phase heat exchanger (300).

A fourth valve (V4) is provided in the pipe through which the heat-exchanged hydrogen discharged from the solid-phase heat exchanger 300 is discharged to the hydrogen turbine or the downstream process of the PSA 600 to separate a portion of the hydrogen and transfer it to the heat storage reactor. Accordingly, by controlling the fourth valve V4, the ratio of hydrogen to be transferred to the heat storage reactor can be adjusted, and further, the degree of heat storage can be adjusted.

A fifth valve (V5) is provided in the pipe through which hydrogen is transferred to the thermal storage reactor, and by controlling the fifth valve (V5), it is possible to select which reactor it will flow into.

Water vapor and nitrogen generated in the heat storage reactor are introduced into one pipe by the sixth valve (V6) and then flow to the preheater (200).

Meanwhile, as described above, the thermal storage reactor and the methane direct pyrolysis reactor are operated alternately. For this purpose, sensors (S1, S2) are provided in each reactor to measure the temperature and the temperature of the hydrogen transported from each reactor. A sensor (S3) is further provided to measure the temperature. Here, the sensor (S3) must be installed in the pipe connecting the second valve (V2) and the solid-phase heat exchanger (300) to measure the internal temperature, and through this, only one sensor (S3) can be used to determine which reactor (410, 420), the temperature of the hydrogen discharged can be measured.

It is currently possible to switch between the methane direct pyrolysis reactor and the thermal storage reactor using sensors (S1, S2, and S3), which will be described later.

2. Description of system operation method

A method of operating a system according to the present invention will be described with reference to FIGS. 2 and 3.

Figure 2 shows a case where the first reactor 410 is a methane direct thermal decomposition reactor and the second reactor 420 is a thermal storage reactor.

Methane at room temperature is transferred from the LNG storage tank 100 to the preheater 200, where the methane is preheated to about 300 degrees Celsius. The preheated methane is transferred to the solid-phase heat exchanger 300 and heated to about 900 degrees Celsius.

By controlling the first valve V1, methane at about 900 degrees Celsius flows only into the first reactor 410. The first reactor 410 has a temperature of about 1200 degrees Celsius, and direct thermal decomposition of methane occurs to produce gaseous hydrogen and solid carbon. These are also about 1200 degrees Celsius.

Hydrogen at about 1200 degrees Celsius is transferred to the solid-phase heat exchanger (300) through a separate pipe. At this time, the second valve (V2) is controlled to prevent communication with the second reactor (420).

Hydrogen at about 1200 degrees Celsius transferred to the solid-phase heat exchanger (300) is heat exchanged to about 200 degrees Celsius, and is transferred to a hydrogen turbine or PSA (600) for use. At this time, the fourth valve (V4) is controlled to transfer some of the hydrogen to the second reactor (420). The transfer rate can be determined depending on the environment of the thermal storage reactor. For example, while examining the temperature measured by the sensor S2 in the second reactor 420, which is a heat storage reactor, if it is lower than the average, it can be controlled to transfer more hydrogen, and vice versa. The transport pipe is provided with a fifth valve (V5) to prevent communication with the first reactor (410).

More air is introduced into the second reactor 420 and reacts with hydrogen to generate heat. In this process, the heat storage material of the second reactor 420 accumulates heat.

During the heat storage process in the second reactor 420, water vapor and nitrogen of about 500 degrees Celsius are generated, and these are transferred to the preheater 200 to supply heat to the preheater 200. This pipe is provided with a sixth valve (V6) to prevent communication with the first reactor (410).

Meanwhile, the solid carbon at about 1200 degrees Celsius generated in the first reactor 410 is also transferred to the solid-phase heat exchanger 300 through a separate pipe. Since the gaseous hydrogen generated in the first reactor 410 is separated through a separate pipe, a separate carbon separation device is not required. Additionally, the third valve (V3) provided in the corresponding pipe is controlled to prevent communication with the second reactor (420).

The solid-phase carbon at about 1200 degrees Celsius transferred to the solid-phase heat exchanger 300 is heat-exchanged to about 200 degrees Celsius, and is transferred to the carbon storage tank 500 for use.

In one embodiment, the carbon in the carbon storage tank 500 may be used as a heat storage material for the reactors 410 and 420.

During this reaction process, when the productivity of the first reactor 410 begins to decrease, the reactors 410 and 420 are switched. The specific switching method will be described later.

Switching is performed by changing the control direction of all valves (V1, V2, V3, V4, V5, V6), and when switching is completed, the second reactor 420 is a methane direct pyrolysis reactor and the first reactor is a methane direct pyrolysis reactor, as shown in FIG. (410) becomes a heat storage reactor. The flow of each material after the change is similar to the case where the above-described first reactor 410 is a methane direct pyrolysis reactor, so detailed description will be omitted.

3. Description of switching method

Using sensors (S1, S2) provided in each of the reactors (410, 420) and a sensor (S3) provided in the pipe through which hydrogen flows to the solid-phase heat exchanger (300), the methane direct pyrolysis reactor and the thermal storage reactor are Explains how to switch.

For example, when direct thermal decomposition of methane is started in the first reactor 410, the temperature measured by the sensor S1 increases to about 1200 degrees Celsius and is maintained at this level. In the second reactor 420, since the direct pyrolysis of methane has been completed, the temperature continues to decrease at about 1200 degrees Celsius, but the decrease trend is not high due to the heat storage material in the second reactor 420, and at the same time, the temperature of hydrogen at about 200 degrees Celsius Since the inflow began to react, the temperature measured by the sensor (S2) decreases from about 1200 degrees Celsius, but remains at about 500 degrees Celsius.

In this state, the first reactor 410 continues to perform direct pyrolysis of methane, and when the productivity of direct pyrolysis of methane in the reactor begins to decrease, the temperature measured by the sensor S1 begins to gradually decrease around 1200 degrees Celsius. . Since the temperature of the hydrogen produced in the reactor is similar to the temperature inside the reactor, this temperature decrease is also detected by the sensor (S3) provided in the pipe through which the hydrogen is discharged.

That is, if, as a result of measurement for a certain period of time, it is confirmed that the temperature measured by the sensor (S1) or sensor (S3) has a decreasing trend at around 1200 degrees Celsius, it is recognized that the productivity of the first reactor 410 is decreasing. Thus, the reactor is switched. Accordingly, the first reactor 410 is now ready for thermal storage, and the second reactor 420 is ready for direct methane pyrolysis.

This process is also the same in the case of direct thermal decomposition of methane in the second reactor 420, and as a result of measurement for a certain period of time, the temperature measured by the sensor (S2) or sensor (S3) tends to decrease around about 1200 degrees Celsius. If this is confirmed to be maintained, it is recognized that the productivity of the second reactor 420 is decreasing, and the reactor can be controlled to switch.

Due to this switching, even if the hydrogen productivity of the current methane direct pyrolysis reactor is lowered, overall productivity decline or instability can be prevented by switching to a thermal storage reactor in which heat is maintained and a reactor in which methane direct pyrolysis is performed. Figure 4 shows this. When the productivity of a specific reactor begins to decrease, this is detected and switched through sensors (S1, S2, and S3), indicating that the overall productivity of the system can be maintained stably.

100: LNG storage tank
200: Preheater
300: Solid-vapor heat exchanger
410: first reactor
420: second reactor
500: Carbon storage tank
600: Hydrogen turbine or PSA
700:HRSG
V1~V6: Valves
S1~S3: Sensor

Claims (11)

A preheater (200) for preheating methane;
A solid-phase heat exchanger (300) that heats the methane preheated in the preheater (200) through heat exchange; and
A blue-green hydrogen production system that directly pyrolyzes the heated methane to produce hydrogen and solid carbon, and includes reactors 410 and 420 including heat storage materials,
Hydrogen generated in one of the reactors and solid carbon generated in one of the reactors are introduced into the solid-phase heat exchanger 300 and exchange heat,
In one of the reactors (410, 420), direct thermal decomposition of methane is performed, and in the other of the reactors (410, 420), some of the heat-exchanged hydrogen is reacted and heat storage is achieved. One reactor is operated alternately,
Blue-green hydrogen production system.
According to claim 1,
It further includes a hydrogen turbine or PSA (Pressure Swing Absorption) 600 through which another part of the heat-exchanged hydrogen flows into the solid-phase heat exchanger 300,
Blue-green hydrogen production system.
According to claim 1,
Further comprising a carbon storage tank 500 into which solid-phase carbon that has been heat-exchanged flows into the solid-phase heat exchanger 300,
Blue-green hydrogen production system.
According to claim 1,
As heat storage occurs in the other reactor, water vapor and nitrogen are generated, and the generated water vapor and nitrogen flow into the preheater 200 to provide heat.
Blue-green hydrogen production system.
According to claim 4,
Further comprising a Heat Recovery Steam Generator (HRSG) 700 in which water vapor and nitrogen provided as heat from the preheater 200 are introduced and heat is recovered,
Blue-green hydrogen production system.
According to claim 1,
The heat storage material included in the reactors (410, 420) includes solid carbon generated in one of the reactors,
Blue-green hydrogen production system.
According to claim 2,
The heated methane discharged from the solid-phase heat exchanger 300 flows to one of the reactors 410 and 420 by the first valve V1,
Hydrogen generated in one of the reactors (410, 420) flows into one pipe through the second valve (V2) and then flows into the solid-phase heat exchanger (300),
The solid carbon generated in one of the reactors (410, 420) is introduced into one pipe by the third valve (V3) and then introduced into the solid-phase heat exchanger (300).
Blue-green hydrogen production system.
According to claim 7,
The heat-exchanged hydrogen discharged from the solid-gas heat exchanger 300 is divided into the part and the other part by the fourth valve V4, and the part of the hydrogen flows to another one of the reactors 410 and 420. It is reacted for heat storage, and the other part of the hydrogen flows to the hydrogen turbine or PSA (600),
Some of the hydrogen flows only to the other one of the reactors (410, 420) by the fifth valve (V5),
Blue-green hydrogen production system.
According to claim 7,
Water vapor and nitrogen generated in another one of the reactors (410, 420) are introduced into one pipe by the sixth valve (V6) and then flow to the preheater (200).
Blue-green hydrogen production system.
According to claim 1,
Each of the reactors (410, 420) is equipped with sensors (S1, S2) that measure the internal temperature,
If the temperature measured by a sensor provided in any of the reactors (410, 420) in which direct methane thermal decomposition is performed is on a decreasing trend for a predetermined period of time, one of the reactors is switched to a reactor in which heat storage is performed. and the other reactor is switched to a reactor in which direct methane pyrolysis is performed,
Blue-green hydrogen production system.
According to claim 7,
A sensor (S3) for measuring the internal temperature is provided in the pipe connecting the second valve (V2) and the solid-gas heat exchanger (300),
If the temperature measured by the sensor S3 for a predetermined time is decreasing, one of the reactors is switched to a reactor in which heat storage is performed and the other reactor is switched to a reactor in which methane direct pyrolysis is performed,
Blue-green hydrogen production system.

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