Turquoise hydrogen production system using thermal storage methane pyrolysis

Abstract

The present invention comprises two or more pyrolysis reactors (100) for pyrolyzing incoming methane into hydrogen and solid carbon; two or more heat storage reactors (200) to which a portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100) is introduced, which store heat generated by burning the introduced hydrogen, and which are configured to be paired with any one of the pyrolysis reactors (100); a heat exchanger (300) to preheat methane introduced into the pyrolysis reactors (100) by receiving heat from the exhaust gas discharged from the two or more heat storage reactors (200); and a hydrogen storage tank (400) in which another portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100) is stored. When any one of the pyrolysis reactors (100) operates to perform the pyrolysis of methane, the heat storage reactor (200) paired with any one of the pyrolysis reactors (100) operates, and the two or more A cyanoacrylate hydrogen production system is provided in which a pyrolysis reactor (100) is operated alternately and is equipped with two or more reactors, and the time required for the pyrolysis reaction in the pyrolysis reactor (100) and the time required for heat accumulation in the heat accumulation reactor (200) are operated equally.

Description

Technology Field

[0001] The present invention relates to the thermal decomposition of methane, and more specifically, to a blue-green hydrogen production system capable of operating under optimal operating conditions according to a target hydrogen production volume and target methane conversion rate by applying a thermal storage type methane thermal decomposition. Background Technology

[0003] Depending on the production method, hydrogen is classified into grey hydrogen produced from fossil fuels, green hydrogen produced using water electrolysis, and turquoise hydrogen generated through the direct pyrolysis of methane.

[0004] Blue-green hydrogen has the advantage of theoretically not emitting greenhouse gases (CO2) during the hydrogen acquisition process, as it is produced by a direct pyrolysis reaction in which CH4 is decomposed into two H2 and C(s). Blue-green hydrogen is a recently researched concept, and a production system for it has not yet been established; however, it is reported that theoretically, significant energy is required to raise the reactor to about 1200 degrees Celsius for the production of blue-green hydrogen through the direct pyrolysis of methane.

[0006] Therefore, it is important to reliably secure a significant amount of energy to reach about 1200 degrees Celsius for the production of blue-green hydrogen. Technologies for this purpose have been proposed, one of which is to efficiently supply the heat required for the pyrolysis reaction by burning some of the hydrogen produced by the methane pyrolysis reaction and storing the heat generated during the hydrogen combustion in a thermal storage reactor.

[0007] Various heat storage methods are utilized, one of which involves transferring a portion of the hydrogen produced after pyrolysis in a methane pyrolysis reactor to a tank and burning the remaining portion. However, if both methane pyrolysis and heat storage occur within a single reactor in this manner, continuous production is impossible. In other words, because the heat storage and pyrolysis reactions are performed alternately within a single reactor, there is a limitation in that hydrogen cannot be produced continuously. This leads to a decrease in the hydrogen production rate.

[0008] A method has also been proposed to separately provide a methane pyrolysis reactor and a hydrogen combustion reactor for heat storage. Even in this case, considering the relatively short hydrogen combustion time, there is inevitably a dead time for either the methane pyrolysis reactor or the hydrogen combustion reactor. If the methane pyrolysis reactor stops operating, the hydrogen production rate decreases, and if the hydrogen combustion reactor stops operating, the energy reduction effect is reduced because it is not possible to preheat the methane or provide the heat required for pyrolysis.

[0009] Therefore, it is necessary to develop a blue-green hydrogen production system capable of continuous hydrogen production and efficiently supplying the thermal energy required for the thermal decomposition reaction of methane by adopting a thermal storage method, as well as to develop an appropriate control method for this purpose.

[0010] Review related patent literature.

[0011] Korean Registered Patent No. 10-2526186 relates to a hydrogen and carbon production reactor and a combination reactor including the same, which improves energy efficiency by storing combustion heat generated during the process of pure oxygen combustion of carbon in a heat storage unit and utilizing it for the thermal decomposition of methane; however, there is a limitation in that continuous production of hydrogen is impossible because the pure oxygen combustion of carbon and the thermal decomposition of methane are performed alternately.

[0012] Japanese Patent No. 7208172 relates to a decomposition furnace system comprising a plurality of convection banks configured to receive and preheat hydrocarbon feedstocks and a radiating unit configured to heat so that a pyrolysis reaction takes place. Since the convection banks preheat the hydrocarbons using boiler coils, there is a limit to stably supplying the thermal energy required for the pyrolysis reaction. Prior art literature

[0014] Korean Registered Patent No. 10-2526186, Japanese Registered Patent No. 7208172, Japanese Published Patent No. 2011-111388 The problem to be solved

[0015] The present invention was devised to solve the above-mentioned problems.

[0016] The purpose is to provide a blue-green hydrogen production system utilizing a thermal storage multi-stage pyrolysis reactor, and to provide a system that efficiently achieves continuous hydrogen production and target hydrogen production volume by operating the multi-stage thermal storage reactor and pyrolysis reactor under optimal operating conditions.

[0017] To efficiently secure the thermal energy required for the pyrolysis of methane, we aim to provide a blue-green hydrogen production system that stores the combustion heat of hydrogen in a thermal storage reactor and utilizes it for the pyrolysis of methane.

[0018] In addition, we aim to provide a system capable of efficiently achieving target hydrogen production volume and target methane conversion rate by controlling the operating conditions (operating time, operating temperature range, methane input amount, hydrogen fuel amount, etc.) of the thermal storage reactor and the pyrolysis reactor. means of solving the problem

[0020] An embodiment of the present invention for solving the above-mentioned problem comprises: two or more pyrolysis reactors (100) that pyrolyze incoming methane into hydrogen and solid carbon; two or more heat storage reactors (200) to which a portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100) is introduced, which store heat generated by burning the introduced hydrogen, and which are configured to be paired with any one of the pyrolysis reactors (100); a heat exchanger (300) that receives heat from the exhaust gas discharged from the two or more heat storage reactors (200) to preheat the methane introduced into the pyrolysis reactors (100); and a hydrogen storage tank (400) in which another portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100) is stored. When any one of the pyrolysis reactors (100) operates to perform the pyrolysis of methane, the heat storage reactor paired with any one of the pyrolysis reactors (100) A blue-green hydrogen production system is provided in which a reactor (200) is operated, and two or more pyrolysis reactors (100) are operated alternately, and two or more are provided, and the time required for the pyrolysis reaction of the pyrolysis reactor (100) and the time required for heat accumulation in the heat accumulation reactor (200) are operated equally.

[0021] Additionally, the above-described blue-green hydrogen production system further includes a control unit (500), and the control unit (500) preferably includes an input module (510) into which a target hydrogen production amount (A) and a target methane conversion rate (B) are input, a pyrolysis reactor dynamic characteristic analysis module (520) that analyzes the dynamic characteristics of the pyrolysis reactor (100) according to the information input to the input module (510), a thermal storage reactor dynamic characteristic analysis module (530) that analyzes the dynamic characteristics of the thermal storage reactor (200) according to the information input to the input module (510), and an optimal control calculation module (540) that receives the information analyzed by the pyrolysis reactor dynamic characteristic analysis module (520) and the thermal storage reactor dynamic characteristic analysis module (530) and controls the pyrolysis reaction time of the pyrolysis reactor (100) and the thermal storage time of the thermal storage reactor (200) to be the same.

[0022] Additionally, the pyrolysis reactor dynamic characteristic analysis module (520) preferably further includes a pyrolysis start temperature calculation module (521) that calculates a pyrolysis start temperature (C) using a target methane conversion rate (B) input to the input module (510), a methane input amount calculation module (522) that calculates an initial methane input amount (D) using the target hydrogen production amount (A) and the target methane conversion rate (B), and a pyrolysis end temperature calculation module (523) that calculates a pyrolysis end temperature (E) using the target hydrogen production amount (A), the target methane conversion rate (B), the pyrolysis start temperature (C), and the methane input amount (D).

[0023] Additionally, the thermal storage reactor dynamic characteristic analysis module (530) includes a hydrogen fuel amount calculation module (531) that determines the hydrogen fuel amount (F) using the pyrolysis start temperature (C) and the pyrolysis end temperature (E), and it is preferable that the thermal storage reactor dynamic characteristic analysis module (530) analyzes the dynamic characteristics of the thermal storage reactor (200) using the hydrogen fuel amount (F).

[0024] Additionally, the methane input amount calculation module (522) calculates the required methane input amount (D') using the amount of hydrogen pyrolyzed in the pyrolysis reactor (100) and the target methane conversion rate (B), and the optimal control calculation module (540) calculates the required hydrogen fuel amount (F) so that the pyrolysis reaction time of the pyrolysis reactor (100) and the heat storage time of the heat storage reactor (200) are the same.

[0025] Additionally, it is preferable to further include a methane supply line (2000) connecting the heat exchanger (300) and the pyrolysis reactor (100), and a methane supply control valve (V1) configured to control the supply of methane at a point on the methane supply line (2000).

[0026] Additionally, it is preferable to further include a hydrogen production line (2100) configured to allow hydrogen pyrolyzed in the pyrolysis reactor (100) to flow, with one end connected to the pyrolysis reactor (100) and the other end connected to the hydrogen storage tank (400), and a hydrogen production valve (V2) installed at one point of the hydrogen production line (2100) to control the flow of hydrogen.

[0027] Additionally, it is preferable to further include a hydrogen supply line (2200) in which one end is connected to another point (P) located in front of the one point of the hydrogen production line (2100) and the other end is connected to the heat storage reactor (200), and a hydrogen supply control valve (V3) installed on the hydrogen supply line (2200) and configured to control the flow of hydrogen.

[0028] In addition, it is preferable that the methane supply control valve (V1), the hydrogen production valve (V2), and the hydrogen supply control valve (V3) are controlled to be opened or closed by the optimal control calculation module (540). Effects of the invention

[0030] According to the present invention described above, continuous production of blue-green hydrogen is possible by applying a multi-stage thermal decomposition reactor of the thermal storage type, and the target hydrogen production volume can be efficiently achieved by operating the blue-green hydrogen production system under optimal operating conditions.

[0031] By controlling the operating conditions (operating time, operating temperature range, methane input, hydrogen fuel amount, etc.) of the thermal storage reactor and the pyrolysis reactor, it is possible to operate a system capable of efficiently achieving target hydrogen production and target methane conversion rates.

[0032] In addition, when a pyrolysis reaction occurs in one pyrolysis reactor, the heat of hydrogen combustion is stored in one heat storage reactor, and continuous production of blue-green hydrogen is possible by having the pyrolysis reactor and the heat storage reactor form a pair to carry out the reaction.

[0033] Furthermore, by pyrolyzing methane to separate it into hydrogen and carbon and utilizing the heat generated from burning the hydrogen produced during the pyrolysis process, the high-temperature thermal energy required for methane pyrolysis can be efficiently obtained. Specifically, efficient heat utilization is possible by storing the combustion heat of hydrogen in a thermal storage reactor and preheating the methane using the latent heat of the flue gas generated during hydrogen combustion. Brief explanation of the drawing

[0035] FIG. 1 is a drawing illustrating an embodiment of a blue-green hydrogen production system according to the present invention. FIG. 2 is a drawing for explaining the configuration of a control unit according to the present invention. FIG. 3 is a diagram illustrating the operation process of a control unit according to the present invention. Figure 4 is a graph showing the reactor temperature, total hydrogen production, and methane conversion rate of a pyrolysis reactor and a thermal storage reactor according to one embodiment of the present invention. Specific details for implementing the invention

[0036] The above-mentioned objectives, features, and other advantages of the present invention will become more apparent by describing preferred embodiments of the invention in detail with reference to the accompanying drawings. In this process, the thickness of lines or the size of components depicted in the drawings may be exaggerated for clarity and convenience of explanation. Furthermore, the terms described below are defined considering their functions in the present invention, and these may vary depending on the intention or convention of the user or operator. Therefore, the definitions of these terms should be described based on the content throughout this specification.

[0037] Furthermore, the described embodiments are provided as examples for the purpose of explaining the invention and do not limit the technical scope of the invention.

[0039] The present invention will be described in detail below with reference to the drawings.

[0040] FIG. 1 is a schematic diagram illustrating an optimal blue-green hydrogen production system applying regenerative methane pyrolysis according to the present invention. The blue-green hydrogen production system according to the present invention includes a pyrolysis reactor (100), a regenerative reactor (200), a heat exchanger (300), a hydrogen storage tank (400), and a control unit (500).

[0042] A pyrolysis reactor (100) pyrolyzes incoming methane into hydrogen and solid carbon. In one embodiment according to the present invention, at least two pyrolysis reactors (100) are provided, and pyrolysis of methane is performed independently in each pyrolysis reactor (100). A portion of the hydrogen decomposed in the pyrolysis reactor (100) is introduced into a heat storage reactor (200), and another portion is stored in a separate hydrogen storage tank (400). Various downstream processes are required to form hydrogen for use in other industrial fields, but a detailed description is omitted here. There may also be residual methane that is not decomposed in the pyrolysis reactor (100). This is explained by the methane conversion rate described later. The residual methane may be combusted, or it may be reintroduced into the pyrolysis reactor (100) through a separate fuel source and pyrolyzed again.

[0044] A heat storage reactor (200) receives a portion of the hydrogen that is pyrolyzed in the pyrolysis reactor (100) and stores the heat generated by burning the introduced hydrogen. One heat storage reactor (200) is configured to be paired with one pyrolysis reactor (100). That is, a pair of pyrolysis reactors (100) and heat storage reactors (200) are provided in multiple quantities, configured to perform a pyrolysis reaction and a heat storage reaction, respectively, and the number of each is the same.

[0046] The heat exchanger (300) receives heat from the exhaust gas discharged from the plurality of heat storage reactors (200) and preheats the methane flowing into the plurality of pyrolysis reactors (100). That is, heat is exchanged between the exhaust gas discharged from the combustion of hydrogen in the heat storage reactor (200) and the methane, and after the methane reaches a temperature within a certain range, it is fed into the pyrolysis reactor (100) and pyrolyzed. In other words, efficient heat utilization is possible by storing the combustion heat of hydrogen in the heat storage reactor (200) and preheating the methane using the latent heat of the exhaust gas generated during hydrogen combustion. Any method of heat exchange is acceptable.

[0048] The hydrogen storage tank (400) stores another portion of the hydrogen pyrolyzed in each of the plurality of pyrolysis reactors (100). As previously mentioned, the description of the subsequent process is omitted.

[0050] Hereinafter, with reference to FIGS. 2 and FIGS. 3, the control unit (500) of the blue-green hydrogen production system according to the present invention will be described in detail. The drawings are merely schematic representations, and the following description should be prioritized.

[0052] The control unit (500) includes an input module (510), a pyrolysis reactor dynamic characteristic analysis module (520), a thermal storage reactor dynamic characteristic analysis module (530), and an optimal control calculation module (540), and controls the operating conditions of the pyrolysis reactor (100) and the thermal storage reactor (200) according to the target hydrogen production amount (A) and the target methane conversion rate (B).

[0054] The input module (510) receives a target hydrogen production amount (A) and a target methane conversion rate (B). The target hydrogen production amount (A) refers to the amount of hydrogen to be produced, and the target methane conversion rate (B) refers to the amount of hydrogen produced relative to the input methane. The information on the received target hydrogen production amount (A) and target methane conversion rate (B) is transmitted to the pyrolysis reactor dynamic characteristics analysis module (520), the thermal storage reactor dynamic characteristics analysis module (530), and the optimal control calculation module (540).

[0056] The pyrolysis reactor dynamic characteristics analysis module (520) analyzes the operating conditions of the pyrolysis reactor (100) that change according to the target hydrogen production amount (A) and target methane conversion rate (B) input to the input module (510). That is, the pyrolysis reactor dynamic characteristics analysis module (520) analyzes the dynamic characteristics of the pyrolysis reactor (100) according to the input of the input module (510). The pyrolysis reactor dynamic characteristics analysis module (520) includes a pyrolysis start temperature calculation module (521), a methane input amount calculation module (522), and a pyrolysis end temperature calculation module (523).

[0058] The pyrolysis start temperature calculation module (521) calculates the pyrolysis start temperature (C) using the target methane conversion rate (B). If the pyrolysis start temperature is high, the methane conversion rate can be increased, and more hydrogen can be produced. That is, when the target methane conversion rate (B) is input through the input module (510), the pyrolysis start temperature (C) is determined in proportion to it. Accordingly, the methane is preheated to the determined pyrolysis start temperature (C) and fed into the pyrolysis reactor (100).

[0060] The methane input amount calculation module (522) calculates the initial methane input amount (D) using the target hydrogen production amount (A) and the target methane conversion rate (B). Ideally, when 1 mole of methane is pyrolyzed, 2 moles of hydrogen molecules (gaseous hydrogen) are produced. In the pyrolysis reactor (100) according to the present invention, the target methane conversion rate (B) considering unreacted methane can be measured by experiment, and the required methane input amount (D) is calculated using this.

[0062] The pyrolysis end temperature calculation module (523) calculates the pyrolysis end temperature (E) using the target hydrogen production volume (A), target methane conversion rate (B), pyrolysis start temperature (C), and methane input amount (D). The dynamic characteristics of methane pyrolysis can be analyzed by considering the unique characteristic variables of the pyrolysis reactor (100) according to the present invention together and using the target hydrogen production volume (A), target methane conversion rate (B), pyrolysis start temperature (C), and methane input amount (D). Considering the analyzed dynamic characteristics, an appropriate pyrolysis end temperature (E) is calculated for methane pyrolysis in the pyrolysis reactor (100).

[0064] As described above, when both the pyrolysis start temperature (C) and the pyrolysis end temperature (E) are calculated, the reaction characteristics of the thermal storage reactor (200) for operation can be determined. The hydrogen fuel amount calculation module (531) considers the unique characteristic variables of the thermal storage reactor (200) according to the present invention and determines the amount of hydrogen fuel (F) to be supplied to the thermal storage reactor (200) to achieve the pyrolysis start temperature (C) calculated by the pyrolysis start temperature calculation module (521) and the pyrolysis end temperature (E) calculated by the pyrolysis end temperature calculation module (523).

[0066] Subsequently, the amount of hydrogen to be decomposed from the pyrolysis reactor (100) is calculated as the sum of the hydrogen production amount and the hydrogen fuel amount (F). The methane input amount calculation module (522) calculates the methane input amount (D') to be input through mass balance by considering the amount of hydrogen decomposed from the pyrolysis reactor (100) and the target methane conversion rate (B) together in order to achieve the target hydrogen production amount (A).

[0068] Using the information calculated so far (target hydrogen production volume (A), target methane conversion rate (B), pyrolysis start temperature (C), methane input amount (D), pyrolysis end temperature (E), hydrogen fuel amount (F), methane input amount (D')), the dynamic characteristics of the pyrolysis reactor (100) are re-analyzed, and simultaneously, since the characteristic variables of the thermal storage reactor (200) and the hydrogen fuel amount (F) have been identified, the dynamic characteristics of the thermal storage reactor can also be analyzed. The dynamic characteristics analysis of the thermal storage reactor (200) is performed in the thermal storage reactor dynamic characteristics analysis module (530), and the operating conditions of the thermal storage reactor (200) that change according to the hydrogen fuel amount (F) supplied to the thermal storage reactor (200) are analyzed.

[0070] Subsequently, the optimal control calculation module (540) can calculate the pyrolysis reaction time of the pyrolysis reactor (100) and the heat storage reaction time of the heat storage reactor (200) by synthesizing the analyzed information. If, as a result of the calculation, the reaction time of the pyrolysis reactor (100) is greater than the reaction time of the heat storage reactor (200), it means that more hydrogen fuel than necessary has been supplied, so a setting to lower the amount of hydrogen fuel (F) is made, and the dynamic characteristics are analyzed again. If, the reaction time of the pyrolysis reactor (100) is smaller than the reaction time of the heat storage reactor (200), it means that less hydrogen fuel has been supplied, so a setting to increase the amount of hydrogen fuel (F) is made, and the dynamic characteristics are analyzed again. By repeating the above process, the methane pyrolysis time of the pyrolysis reactor (100) and the heat storage time of the heat storage reactor (200) paired with it can be set to be equal. If the corresponding times are set equally, the pyrolysis reactor (100) and the heat storage reactor (200) will each operate alternately without dead time, and each reactor will operate continuously, thereby increasing thermal efficiency and maximizing hydrogen production.

[0071] Accordingly, the blue-green hydrogen production system according to the present invention can efficiently achieve a target hydrogen production amount (A) by operating with a methane input amount (D') and a hydrogen fuel amount (F) for optimal control.

[0073] One end of the methane supply line (2000) is connected to a heat exchanger (300), and the other end is connected to a pyrolysis reactor (100). A methane supply control valve (V1) is provided on the methane supply line (2000) to control the supply of methane so that methane preheated in the heat exchanger (300) is supplied to the pyrolysis reactor (100).

[0074] One end of the hydrogen production line (2100) is connected to a pyrolysis reactor (100), and the other end is connected to a hydrogen storage tank (400), configured to allow the flow of hydrogen pyrolyzed in the pyrolysis reactor (100). A hydrogen production valve (V2) is installed at one point of the hydrogen production line (2100) to control the flow of hydrogen to the hydrogen storage tank (400).

[0075] One end of the hydrogen supply line (2200) is connected to another point (P) located in front of one point of the hydrogen production line (2100), and the other end is connected to a thermal storage reactor (200). A hydrogen supply control valve (V3) is installed on the hydrogen supply line (2200) to control the flow of hydrogen so that hydrogen produced in the pyrolysis reactor (100) flows into the thermal storage reactor (200).

[0076] The methane supply control valve (V1), hydrogen production valve (V2), and hydrogen supply control valve (V3) receive a control signal from the optimal control calculation module (540) and are controlled to open or close, thereby allowing the blue-green hydrogen production system to be optimally controlled.

[0078] FIG. 4 is a graph showing the reactor temperature, total hydrogen production amount, and methane conversion rate of a pyrolysis reactor (100) and a heat storage reactor (200) according to one embodiment of the present invention.

[0079] It can be confirmed that hydrogen can be continuously produced by applying a multi-stage thermal storage type pyrolysis reactor, and the target hydrogen production amount (A) can be efficiently achieved by repeatedly calculating the required amount of hydrogen fuel (F) in the optimal control calculation module (540) so that the pyrolysis reaction time and the thermal storage time are the same. Explanation of the symbols

[0082] 100: Pyrolysis reactor 200: Thermal storage reactor 300: Heat exchanger 400: Hydrogen storage tank 500: Control unit 510: Input Module 520: Pyrolysis Reactor Dynamics Analysis Module 521: Pyrolysis Start Temperature Calculation Module 522: Methane Input Calculation Module 523: Pyrolysis Termination Temperature Calculation Module 530: Thermal Storage Reactor Dynamics Analysis Module 531: Hydrogen Fuel Quantity Calculation Module 540: Optimal Control Calculation Module 2000: Methane supply line 2100: Hydrogen production line 2200: Hydrogen supply line V1: Methane supply control valve V2: Hydrogen production valve V3: Hydrogen supply control valve

Claims

Claim 1 Two or more pyrolysis reactors (100) that pyrolyze incoming methane into hydrogen and solid carbon; two or more heat storage reactors (200) that receive a portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100), store heat generated by burning the introduced hydrogen, and are configured to be paired with any one of the pyrolysis reactors (100); a heat exchanger (300) that receives heat from the exhaust gas discharged from the two or more heat storage reactors (200) to preheat the methane introduced into the pyrolysis reactors (100); and a hydrogen storage tank (400) that stores another portion of the hydrogen pyrolyzed in each of the two or more pyrolysis reactors (100). The apparatus includes a control unit (500), and when any one of the pyrolysis reactors (100) operates to perform pyrolysis of methane, a heat storage reactor (200) paired with any one of the pyrolysis reactors (100) operates, and two or more of the pyrolysis reactors (100) operate alternately, and two or more are provided, and the time required for the pyrolysis reaction of the pyrolysis reactor (100) and the time required for heat storage in the heat storage reactor (200) are operated identically, and the control unit (500) includes an input module (510) into which a target hydrogen production amount (A) and a target methane conversion rate (B) are input; a pyrolysis reactor dynamic characteristic analysis module (520) that analyzes the dynamic characteristics of the pyrolysis reactor (100) according to the information input to the input module (510); and a heat storage reactor dynamic characteristic analysis module that analyzes the dynamic characteristics of the heat storage reactor (200) according to the information input to the input module (510). Module (530); and an optimal control calculation module (540) that receives information analyzed by the pyrolysis reactor dynamic characteristics analysis module (520) and the heat storage reactor dynamic characteristics analysis module (530) and controls the pyrolysis reaction time of the pyrolysis reactor (100) and the heat storage time of the heat storage reactor (200) to be the same.A blue-green hydrogen production system comprising: a pyrolysis reactor dynamic characteristic analysis module (520) further comprising: a pyrolysis start temperature calculation module (521) that calculates a pyrolysis start temperature (C) using a target methane conversion rate (B) input to the input module (510); a methane input amount calculation module (522) that calculates an initial methane input amount (D) using the target hydrogen production amount (A) and the target methane conversion rate (B); and a pyrolysis end temperature calculation module (523) that calculates a pyrolysis end temperature (E) using the target hydrogen production amount (A), the target methane conversion rate (B), the pyrolysis start temperature (C), and the methane input amount (D). Claim 2 delete Claim 3 delete Claim 4 In claim 1, the thermal storage reactor dynamic characteristic analysis module (530) includes a hydrogen fuel amount calculation module (531) that determines the hydrogen fuel amount (F) using the pyrolysis start temperature (C) and the pyrolysis end temperature (E), and the thermal storage reactor dynamic characteristic analysis module (530) analyzes the dynamic characteristics of the thermal storage reactor (200) using the hydrogen fuel amount (F), a blue-green hydrogen production system. Claim 5 In claim 4, the methane input amount calculation module (522) calculates the required methane input amount (D') using the amount of hydrogen pyrolyzed in the pyrolysis reactor (100) and the target methane conversion rate (B), and the optimal control calculation module (540) calculates the required amount of hydrogen fuel (F) so that the pyrolysis reaction time of the pyrolysis reactor (100) and the heat storage time of the heat storage reactor (200) are the same, in a blue-green hydrogen production system. Claim 6 A blue-green hydrogen production system further comprising, in claim 5, a methane supply line (2000) connecting the heat exchanger (300) and the pyrolysis reactor (100); and a methane supply control valve (V1) configured to control the supply of methane at a point of the methane supply line (2000). Claim 7 A cyan hydrogen production system according to claim 6, further comprising: a hydrogen production line (2100) configured to flow hydrogen pyrolyzed in the pyrolysis reactor (100), with one end connected to the pyrolysis reactor (100) and the other end connected to the hydrogen storage tank (400); and a hydrogen production valve (V2) installed at one point of the hydrogen production line (2100) and configured to control the flow of hydrogen. Claim 8 A cyan hydrogen production system according to claim 7, further comprising: a hydrogen supply line (2200) having one end connected to another point (P) located in front of the one point of the hydrogen production line (2100) and the other end connected to the heat storage reactor (200); and a hydrogen supply control valve (V3) installed on the hydrogen supply line (2200) and configured to control the flow of hydrogen. Claim 9 In claim 8, the methane supply control valve (V1), the hydrogen production valve (V2), and the hydrogen supply control valve (V3) are controlled to be opened and closed by the optimal control calculation module (540), in a blue-green hydrogen production system.

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