Hydrocarbon production facility

Abstract

For the efficient production of a hydrocarbon, a hydrocarbon production facility (100) comprises: a first reactor (110) containing a first catalyst (220) for promoting a reaction of hydrogen and carbon dioxide to form a hydrocarbon, and to which hydrogen and carbon dioxide are supplied; a second reactor (120) containing a second catalyst (240) having an activation temperature different from that of the first catalyst (220) for promoting the reaction of hydrogen and carbon dioxide to form a hydrocarbon, and to which a production gas discharged from the first reactor (110) is supplied; and a temperature control device (140) that makes the temperature of the first reactor (110) different from the temperature of the second reactor (120).

Description

Technical field

[0001] The present disclosure relates to a hydrocarbon production plant. The present application claims priority based on Japanese patent application No. 2024-175743, filed on October 7, 2024, the contents of which are incorporated herein. State of the art

[0002] Fossil fuels, such as coal, heavy oil, and superheated oil, are burned in facilities like thermal power plants, steel mills, and boilers. This process releases exhaust gases containing carbon dioxide, a byproduct of fossil fuel combustion, into the atmosphere. Carbon dioxide is considered a cause of global warming, and therefore, technologies for capturing carbon dioxide from the air have been developed.

[0003] Furthermore, as a technology for the effective use of the collected carbon dioxide, for example in patent literature 1, a technology of producing methane is disclosed by supplying carbon dioxide and hydrogen to a reaction device which houses a catalyst which promotes a methanization reaction and causing the carbon dioxide and hydrogen to react with each other in the reaction device. Citation list for patent literature

[0004] Patent literature 1: WO 2021 / 220930 A1 Brief description of the invention: Technical problem

[0005] In the technology of producing hydrocarbons, such as methane, by causing carbon dioxide and hydrogen to react with each other, as described above in patent literature 1, it is desirable to develop a technology for the efficient production of hydrocarbons.

[0006] The present disclosure was made in consideration of the aforementioned problem and has the objective of providing a hydrocarbon production facility capable of efficiently producing a hydrocarbon. Solution to the problem

[0007] To solve the aforementioned problem, according to one aspect of the present disclosure, a hydrocarbon production apparatus is provided, comprising: a first reactor containing a first catalyst for promoting a reaction of hydrogen and carbon dioxide to form hydrocarbons, and to which hydrogen and carbon dioxide are supplied; a second reactor containing a second catalyst, having an activation temperature different from that of the first catalyst, for promoting the reaction of hydrogen and carbon dioxide to form hydrocarbons, and to which a production gas discharged from the first reactor is supplied; and a temperature control device that makes the temperature of the first reactor different from the temperature of the second reactor.

[0008] The activation temperature of the first catalyst can be higher than the activation temperature of the second catalyst, and the temperature control device can cause the temperature of the first reactor to be higher than the temperature of the second reactor.

[0009] The temperature control device can cause the temperature difference between the first reactor and the second reactor to be 100 °C or more and 150 °C or less.

[0010] The aforementioned hydrocarbon production facility may further comprise: a cooling device that cools the production gas discharged from the first reactor; and a gas-liquid separator that separates water from the production gas cooled by the cooling device, and the production gas, from which the water has been removed by the gas-liquid separator, may be fed to the second reactor. Effects

[0011] According to the present disclosure, the hydrocarbon can be produced efficiently. Brief description of drawings Fig. Figure 1 is a schematic diagram of a hydrocarbon production facility according to at least one embodiment of the present disclosure. Fig. Figure 2 is a schematic diagram illustrating an example of a first reactor and a second reactor in at least one embodiment. Fig. Figure 3 is a diagram illustrating an effect achieved by providing a first cooling device and a first gas-liquid separator. Description of embodiments

[0012] With reference to the attached drawings, at least one embodiment of the present disclosure will now be described in detail. The dimensions, materials, and other specific numerical values ​​shown in the at least one embodiment are merely examples used to facilitate understanding of the disclosure and do not limit the present disclosure unless otherwise specifically stated. Components having essentially the same functions and designs herein and in the drawings are designated by the same reference numerals to avoid repetitive descriptions. Furthermore, a representation of components not directly related to the present disclosure has been omitted. [1. Overview of a hydrocarbon production facility]

[0013] First, with reference to Fig. 1 a description of an overview of a hydrocarbon production facility 100 according to at least one embodiment of the present disclosure is provided. Fig. Figure 1 is a schematic diagram of the hydrocarbon production plant 100 according to at least one embodiment of the present disclosure.

[0014] As in Fig. As shown in Figure 1, the hydrocarbon production plant 100 according to at least one embodiment comprises a first reactor 110, a second reactor 120, a raw gas supply device 130 and a temperature control device 140. Fig. 1. The arrows at the solid lines indicate flows of hydrogen (gas), carbon dioxide (gas), hydrocarbons (gas), and water (gas and liquid). Furthermore, in Fig. 1. The arrows at the broken lines indicate flows of heating media.

[0015] The first reactor 110 and the second reactor 120 cause hydrogen and carbon dioxide to react with each other to produce hydrocarbons. A synthesis reaction between hydrogen and carbon dioxide takes place in the first reactor 110 and the second reactor 120, resulting in the production of hydrocarbons. The synthesis reaction between hydrogen and carbon dioxide is an exothermic reaction. For example, the synthesis reaction between hydrogen and carbon dioxide is a reaction that can be described by at least one of formulas (1) to (4). 4H2+CO2→CH4+2H2O Formula (1) 6H2+2CO2→C2H4+4H2O Formula (2) 9H2+3CO2→C3H6+6H2O Formula (3) mH2+nCO2→hydrocarbon+2nH2O Formula (4)

[0016] Methane is produced by the reaction described by formula (1). Ethylene (olefin) is produced by the reaction described by formula (2). Propylene (olefin) is produced by the reaction described by formula (3). Hydrocarbon is produced by the Fischer-Tropsch (FT) synthesis reaction described by formula (4). In at least one embodiment, a case is described by way of example in which the reaction described by formula (1) takes place in the first reactor 110 and the second reactor 120 to produce methane.

[0017] The first reactor 110 stores a first catalyst 220 to promote a reaction of hydrogen and carbon dioxide to form hydrocarbons. Hydrogen and carbon dioxide are supplied to the first reactor 110 from, for example, the raw gas supply device 130, which will be described later.

[0018] The second reactor 120 contains a second catalyst 240 for promoting the reaction of hydrogen and carbon dioxide to form hydrocarbons and differs from the first catalyst 220 in its activation temperature. For example, the thermal resistance temperature of the second catalyst 240 is lower than that of the first catalyst 220. The production gas discharged from the first reactor 110 is fed into the second reactor 120.

[0019] Fig. Figure 2 is a schematic view illustrating an example of the first reactor 110 and the second reactor 120 in at least one embodiment. Fig. For the sake of simplicity, a heat exchanger 180, a first cooling device 172 and a first gas-liquid separator 174 are not shown.

[0020] As in Fig. As shown in Figure 2, the first reactor 110 and the second reactor 120 are, for example, a multi-tube reactor and a heat exchanger reactor, respectively. The first reactor 110 comprises a heating medium reservoir 210 and a plurality of reaction tubes 212. The heating medium is supplied to the heating medium reservoir 210 by the temperature control device 140, which will be described later.

[0021] The numerous reaction tubes 212 are provided in the heating medium container 210. The first catalyst 220 is housed in the reaction tubes 212. The first catalyst 220 comprises, for example, nickel oxide (NiO) and silica (SiO2).

[0022] For example, the temperature in the reaction tubes 212 (temperature of the catalyst) is adjusted to 300 °C or higher and 350 °C or lower by using the heating medium supplied to the heating medium reservoir 210 by the temperature control device 140, and is appropriately adjusted to 320 °C or higher and 350 °C or lower.

[0023] The second reactor 120 is connected to the first reactor 110 by means of, for example, a first delivery tube 170. That is, the first reactor 110 and the second reactor 120 are connected in series via the first delivery tube 170. A first production gas, generated in the first reactor 110, is supplied to the second reactor 120 via the first delivery tube 170. The first production gas comprises at least methane, which is a reaction product, and hydrogen and carbon dioxide, which have not reacted.

[0024] The second reactor 120 comprises a heating medium container 230 and a plurality of reaction tubes 232, as in the first reactor 110. The heating medium is supplied to the heating medium container 230 by the temperature control device 140.

[0025] The multiple reaction tubes 232 are provided in the heating medium container 230. The second catalyst 240 is housed in the reaction tubes 232. The activation temperature of the second catalyst 240 differs from the activation temperature of the first catalyst 220. For example, the activation temperature of the second catalyst 240 is lower than that of the first catalyst 220. In other words, the activation temperature of the first catalyst 220 is higher than that of the second catalyst 240. The second catalyst 240 comprises, for example, nickel (Ni), platinum (Pt), and / or ruthenium (Ru) as an active metal. Furthermore, the second catalyst 240 comprises aluminum oxide (Al₂O₃), silica (SiO₂), magnesium oxide (MgO), and / or titanium oxide (TiO₂) as a support.

[0026] A temperature in the reaction tubes 232 (temperature of the catalyst) is adjusted to, for example, 200 °C or higher and 300 °C or lower, appropriately 200 °C or higher and 275 °C or lower, by means of the heating medium which is supplied to the heating medium container 230 by the temperature control device 140.

[0027] Again with reference to Fig. 1 The raw gas supply device 130 supplies hydrogen and carbon dioxide to the first reactor 110. The raw gas supply device 130 comprises, for example, a supply source 130a for a first raw gas, a first supply device 132, a supply source 130b for a second raw gas, and a second supply device 134.

[0028] The first feed device 132 supplies the first raw gas to the first reactor 110. The first raw gas contains at least hydrogen. The first raw gas consists, for example, of hydrogen and unavoidable impurities.

[0029] The first feed device 132 comprises, for example, a first feed tube 132a and a flow rate control mechanism 132b. The first feed tube 132a is a tube that connects the supply source 130a of the first raw gas and the reaction tubes 212 of the first reactor 110. The flow rate control mechanism 132b is provided at the first feed tube 132a. The flow rate control mechanism 132b adjusts a flow rate of the first raw gas flowing through the first feed tube 132a. The flow rate control mechanism 132b is, for example, designed as a mass flow control system.

[0030] The second feed device 134 supplies the second raw gas to the first reactor 110. The second raw gas comprises at least carbon dioxide. The second raw gas consists, for example, of carbon dioxide and unavoidable impurities. The second feed device 134 comprises, for example, a second feed tube 134a and a flow rate control mechanism 134b. The second feed tube 134a is a tube that connects the supply source 130b of the second raw gas and the first feed tube 132a. In at least one embodiment, the second feed device 134 supplies the second raw gas to the first reactor 110 by means of the second feed tube 134a and the first feed tube 132a. More precisely, the second feed tube 134a connects the supply source 130b of the second raw gas and a section between the flow rate control mechanism 132b and the heat exchanger 180, which will be described later, at the first feed tube 132a.The flow rate control mechanism 134b is provided at the second feed tube 134a. The flow rate control mechanism 134b adjusts the flow rate of the second raw gas flowing through the second feed tube 134a. The flow rate control mechanism 134b is, for example, designed as a mass flow control system.

[0031] Furthermore, the heat exchanger 180 can be provided at the first feed tube 132a. The heat exchanger 180 is located between the flow rate control mechanism 132b and the first reactor 110. The heat exchanger 180 performs a heat exchange between a mixed gas formed from the first raw gas and the second raw gas, which flows through the first feed tube 132a, and the first production gas, which flows through the first discharge tube 170. As described above, the first production gas is the gas produced in the first reactor 110 and comprises hydrogen, carbon dioxide, methane, and steam. In at least one embodiment, the heat exchanger 180 transfers heat from the first production gas to the mixed gas.

[0032] Furthermore, the heat exchanger 180, the first cooling device 172 and the first gas-liquid separator 174 can be provided at the first delivery tube 170 in the specified order.

[0033] The first cooling device 172 cools the first production gas discharged from the first reactor 110 in order to condense the vapor contained within the first production gas. The first cooling device 172 is, for example, a condenser. The first gas-liquid separator 174 separates water (the liquid) from the first production gas cooled by the first cooling device 172.

[0034] The first production gas, from which the water has been removed by the first gas-liquid separator, is supplied to the reaction tubes 232 of the second reactor 120 by means of the first delivery tube 170.

[0035] The second delivery tube 190 is a tube that allows the second reactor 120 and a feed destination 102 to be interconnected. If the hydrocarbon production unit 100 produces methane as one of the hydrocarbons, the feed destination 102 could be, for example, a vehicle that uses methane as a fuel, a combustion device that uses methane as a fuel, a boiler that includes a combustion device that uses methane as a fuel, or an electric power generator that includes a combustion device that uses methane as a fuel. The second delivery tube 190 includes a second cooling device 192, a second gas-liquid separator 194, and a backpressure valve 196 in the order shown.

[0036] The second cooling device 192 cools a second production gas discharged from the second reactor 120, thereby condensing the steam contained within the second production gas. The second production gas is a gas generated in the second reactor 120 and includes at least methane and steam. The second cooling device 192 is, for example, a condenser. The second gas-liquid separator 194 separates the water (the liquid) from the second production gas cooled by the second cooling device 192. The second production gas, from which the water has been removed by the second gas-liquid separator 194, is fed to the feed point 102 via the second discharge tube 190. The backpressure valve 196 maintains the pressure of the second reactor 120 at a predetermined pressure.

[0037] The temperature control device 140 differentiates the temperature of the first reactor 110 from the temperature of the second reactor 120. As described above, the activation temperature of the first catalyst 220, located in the first reactor 110, is higher than the activation temperature of the second catalyst 240, located in the second reactor 120. Therefore, the temperature control device 140 appropriately causes the temperature of the first reactor 110 to be higher than the temperature of the second reactor 120. Furthermore, the temperature difference between the activation temperature of the first catalyst 220 and the activation temperature of the second catalyst 240 must be 100 °C or more and 150 °C or less. Thus, the temperature control device 140 appropriately causes the temperature difference between the first reactor 110 and the second reactor 120 to be 100 °C or more and 150 °C or less.

[0038] In at least one embodiment, for example, the temperature control device 140 causes the heating medium to circulate through the heating medium container 210 of the first reactor 110 and the heating medium container 230 of the second reactor 120 in order to adjust the temperature of the first reactor 110 and the temperature of the second reactor 120.

[0039] The temperature control device 140 comprises, for example, a first temperature control device 142 and a second temperature control device 144.

[0040] The first temperature control device 142 comprises a circulation path 142a, a pump 142b, a flow rate control mechanism 142c and a heating and cooling device 142d.

[0041] Circulation path 142a is a flow path through which the heating medium circulates. Circulation path 142a includes pump 142b, flow rate control mechanism 142c, the heating medium reservoir 210 of the first reactor 110, and the heating and cooling device 142d in the specified order. A suction side of pump 142b is connected to the heating and cooling device 142d. A discharge side of pump 142b is connected to the flow rate control mechanism 142c. When pump 142b is operating, the heating medium circulates through circulation path 142a. The flow rate control mechanism 142c adjusts the flow rate of the heating medium flowing through circulation path 142a. The heating and cooling device 142d heats or cools the heating medium.

[0042] The second temperature control device 144 comprises a circulation path 144a, a pump 144b, a flow rate control mechanism 144c and a heating and cooling device 144d.

[0043] Circulation path 144a is a flow path through which the heating medium circulates. Circulation path 144a includes pump 144b, flow rate control mechanism 144c, the heating medium reservoir 230 of the second reactor 120, and the heating and cooling device 144d in the specified order. A suction side of pump 144b is connected to the heating and cooling device 144d. A discharge side of pump 144b is connected to the flow rate control mechanism 144c. When pump 144b is operating, the heating medium circulates through circulation path 144a. The flow rate control mechanism 144c adjusts the flow rate of the heating medium flowing through circulation path 144a. The heating and cooling device 144d heats or cools the heating medium. [2. Conclusion]

[0044] As described above, the hydrocarbon production facility 100 according to at least one embodiment comprises: the first reactor 110, which stores the first catalyst 220 for promoting the reaction of hydrogen and carbon dioxide to hydrocarbon and to which hydrogen and carbon dioxide are supplied; the second reactor 120, which stores the second catalyst 240, which has an activation temperature different from that of the first catalyst 220, for promoting the reaction of hydrogen and carbon dioxide to hydrocarbon and to which a production gas released from the first reactor 110 is supplied; and the temperature control device 140, which makes the temperature of the first reactor 110 different from the temperature of the second reactor 120.

[0045] The activation temperature of the first catalyst 220 can be higher than the activation temperature of the second catalyst 240, and the temperature control device 140 can cause the temperature of the first reactor 110 to be higher than the temperature of the second reactor 120.

[0046] As described above, the synthesis reaction of hydrocarbons from hydrogen and carbon dioxide is an exothermic reaction. Therefore, when hydrogen and carbon dioxide are supplied to the first reactor 110, its temperature increases. Similarly, when hydrogen and carbon dioxide are supplied to the second reactor 120, its temperature increases. Hydrogen and carbon dioxide are supplied to the first reactor 110 from the raw gas supply device 130. Hydrogen and carbon dioxide that did not react in the first reactor 110, and methane produced in the first reactor 110, are supplied to the second reactor 120. Thus, the amount of hydrogen and carbon dioxide supplied to the second reactor 120 is less than the amount supplied to the first reactor 110.This means that the amount of hydrogen and carbon dioxide contributing to the synthesis reaction is greater in the first reactor 110 than in the second reactor 120. Therefore, the reaction quantity is greater in the first reactor 110 than in the second reactor 120, and consequently, the temperature of the first reactor 110 is higher than the temperature of the second reactor 120. Furthermore, if the temperature of a reaction chamber is equal to or higher than the reaction start temperature, the conversion rate of the synthesis reaction producing hydrocarbons from hydrogen and carbon dioxide will increase as the temperature decreases, due to an equilibrium of the exothermic reaction, and decrease as the temperature increases.Thus, as described above, by placing the first catalyst 220, which has a higher thermal resistance temperature than the second catalyst 240, in the first reactor 110, which reaches a relatively higher temperature, the hydrocarbon production device 100, according to at least one embodiment, can achieve both an increase in the conversion rate per unit time and a suppression of catalyst decomposition at high temperatures, due to an increase in the reaction rate by the first catalyst 220. As a result, the hydrocarbon production device 100, according to at least one embodiment, can prevent a decrease in the conversion rate of the synthesis reaction in the first reactor 110.Furthermore, the conversion rate in the first reactor 110 can be reduced, and thus, according to at least one embodiment, the hydrocarbon production device 100 can avoid a situation in which the amount of unreacted hydrogen and carbon dioxide to be supplied to the second reactor 120 increases. Therefore, according to at least one embodiment, the hydrocarbon production device 100 can suppress a temperature increase in the second reactor 120 due to the progress of the synthesis reaction, and thus the conversion rate in the second reactor 120 can be increased. As a result, according to at least one embodiment, the hydrocarbon production device 100 can produce the hydrocarbon efficiently.

[0047] Furthermore, according to at least one embodiment, the hydrocarbon production device 100 can increase the conversion rate in the second reactor 120 and thus increase the concentration of the hydrocarbon contained in the second production gas discharged from the second reactor 120. Therefore, according to at least one embodiment, the hydrocarbon production device 100 can simplify or eliminate the need for a purification device to remove impurities (for example, hydrogen, carbon dioxide, and water) from the second production gas.

[0048] The temperature control device 140 can cause the temperature difference between the first reactor 110 and the second reactor 120 to be 100 °C or more and 150 °C or less.

[0049] In a case where the temperature difference between the first reactor 110 and the second reactor 120 is 100 °C or more, compared to a case where the temperature difference is less than 100 °C, it is possible to increase the conversion rate in both reactors. Furthermore, in a case where the temperature difference between the first reactor 110 and the second reactor 120 is less than 150 °C, compared to a case where the temperature difference is 150 °C or more, it is possible to increase the conversion rates in both reactors. The temperature control device 140 in at least one embodiment causes the temperature difference between the first reactor 110 and the second reactor 120 to be 100 °C or more and 150 °C or less, so that an even higher conversion rate can be achieved in both the first reactor 110 and the second reactor 120.Thus, the hydrocarbon production facility 100 can produce the hydrocarbon even more efficiently according to at least one embodiment.

[0050] The hydrocarbon production facility 100 according to at least one embodiment may comprise: the cooling device (first cooling device 172) that cools the production gas supplied by the first reactor 110; and the gas-liquid separator (first gas-liquid separator 174) that separates the water from the production gas cooled by the cooling device (first cooling device 172), and the production gas from which the water has been removed by the gas-liquid separator (first gas-liquid separator 174) may be supplied to the second reactor 120.

[0051] The concentration of methane included in the second production gas was simulated in the case where the first cooling device 172 and the first gas-liquid separator 174 were provided at the first delivery tube 170, which allows the first reactor 110 and the second reactor 120 to be connected to each other, and in the case where the first cooling device 172 and the first gas-liquid separator 174 were not provided at the first delivery tube 170. Fig. Figure 3 is a diagram illustrating an effect achieved by providing the first cooling device 172 and the first gas-liquid separator 174. Fig. Figure 3 shows the vertical axis representing the concentration of methane contained in the second production gas, and the horizontal axis represents the temperature [°C] of the second reactor 120. When the concentration of methane from Fig. 3 is shown as a normalized value. Furthermore, in Fig. 3 The solid line represents a course of the methane concentration in the case where the first cooling device 172 and the first gas-liquid separator 174 were provided. In Fig. Figure 3 shows the dashed line representing the concentration profile of methane in the case where the first cooling device 172 and the first gas-liquid separator 174 were not provided.

[0052] As in Fig.As shown in Figure 3, it was confirmed that in the case where the first cooling device 172 and the first gas-liquid separator 174 were provided, the concentration of methane contained in the second production gas was higher than in the case where the first cooling device 172 and the first gas-liquid separator 174 were not provided, regardless of the temperature of the second reactor 120. That is to say, it was confirmed that in the case where the first production gas, from which the water had been removed, was fed to the second reactor 120, the concentration of methane contained in the second production gas was higher than in the case where the first production gas, from which the water had not been removed, was fed to the second reactor 120, regardless of the temperature of the second reactor 120.

[0053] The hydrocarbon production plant 100 according to at least one embodiment comprises the first cooling device 172 and the first gas-liquid separator 174, so that the conversion rate in the second reactor 120 can be increased. Thus, the hydrocarbon production plant 100 according to at least one embodiment can produce the hydrocarbon more efficiently.

[0054] The at least one embodiment has been described above with reference to the attached drawings, but it is needless to say that the present disclosure is not limited to the at least one embodiment. It is evident that those skilled in the art may arrive at various modifications and variations within the attached claims, and these examples are interpreted as naturally falling within the technical scope of the present disclosure.

[0055] For example, in at least one embodiment, the case was described by way of example in which the hydrocarbon production unit 100 comprises the first reactor 110 and the second reactor 120. However, the hydrocarbon production unit 100 can comprise one or a plurality of reactors at the stage preceding the first reactor 110, at the stage following the second reactor 120, or between the first reactor 110 and the second reactor 120. In any case, it is sufficient that the production gas discharged from the first reactor 110 is fed to the second reactor 120.

[0056] Furthermore, in at least one embodiment, the case was described by way of example in which the second reactor 120 is a multi-tube reactor of the heat exchanger type. However, the second reactor 120 can also be an adiabatic reactor. As a result, the costs of the second reactor 120 can be reduced.

[0057] Furthermore, in at least one embodiment, the case was described by way of example in which the raw gas supply device 130 supplies hydrogen and carbon dioxide only to the first reactor 110. However, the raw gas supply device 130 can also supply hydrogen and / or carbon dioxide to the second reactor 120 in addition to the first reactor 110. For example, the raw gas supply device 130 can supply hydrogen and / or carbon dioxide to both the first reactor 110 and the second reactor 120 such that the temperature of the first reactor 110 is lower than a decomposition temperature of the first catalyst 220 and the temperature of the second reactor 120 is lower than a decomposition temperature of the second catalyst 240.Furthermore, the raw gas supply device 130 can supply hydrogen and / or carbon dioxide to the first reactor 110 and the second reactor 120, thus reducing the length of the reaction field of the first reactor 110 and reducing the length of the reaction field of the second reactor 120.

[0058] Furthermore, in at least one embodiment, the case was described by way of example in which the activation temperature of the first catalyst 220 is higher than the activation temperature of the second catalyst 240. However, it is sufficient that the activation temperature of the first catalyst 220 and the activation temperature of the second catalyst 240 differ from each other. For example, the activation temperature of the first catalyst 220 can be lower than the activation temperature of the second catalyst 240. In this case, hydrogen and carbon dioxide are freshly supplied to the second reactor 120 in addition to the first production gas.

[0059] The present disclosure may, for example, contribute to Goal 7 “Ensure access to affordable, reliable, sustainable and modern energy for all” and Goal 13 “Take urgent action to combat climate change and its impacts” of the Sustainable Development Goals (SDGs). Reference symbol list 100 hydrocarbon production facilities 110 first reactor 120 second reactor 140 Temperature control device 172 first cooling device (cooling device) 174 first gas-liquid separator (gas-liquid separator) 220 first catalyst 240 second catalyst QUOTES INCLUDED IN THE DESCRIPTION

[0000] This list of documents cited by the applicant was automatically generated and is included solely for the reader's convenience. The list is not part of the German patent or utility model application. The DPMA accepts no liability for any errors or omissions. Cited patent literature

[0000] JP 2024 - 175743

[0001] WO 2021 / 220930 A1

[0004]

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