Hydrocarbon production system and hydrocarbon production method

Abstract

A hydrocarbon production system (1) comprises: a carbon dioxide recovery device (10) that recovers carbon dioxide and water from air in the atmosphere; a hydrogen production device (30) that produces hydrogen from the water recovered by the carbon dioxide recovery device (10); and a hydrocarbon production device (40) that produces a reaction product containing hydrocarbons from a starting material containing the carbon dioxide recovered by the carbon dioxide recovery device (10) and the hydrogen produced by the hydrogen production device (30).

Description

Hydrocarbon Production System and Hydrocarbon Production Method

[0001] The present disclosure relates to a hydrocarbon production system and a hydrocarbon production method.

[0002] Carbon dioxide is regarded as a cause of global warming, and efforts to suppress the increase in carbon dioxide concentration are spreading worldwide. As one method of reducing the carbon dioxide concentration in the atmosphere, a technique called direct air capture (DAC) has been proposed. DAC is a technique for directly capturing carbon dioxide in the air and has attracted attention as a measure to reduce carbon dioxide emissions into the atmosphere.

[0003] Patent Document 1 discloses a synthesis gas production apparatus that produces synthesis gas from a raw material containing DAC carbon dioxide gas recovered from the atmosphere and hydrogen gas generated by electrolyzing water, and a FT synthesis apparatus that generates FT crude oil from the above synthesis gas. An e-fuel production system is disclosed.

[0004] Japanese Patent No. 7474013

[0005] However, in regions such as desert areas, although it is easy to obtain renewable energy such as sunlight, there is a possibility that it is not easy to secure water. In such regions, it may not be possible to obtain a sufficient amount of hydrogen by electrolysis, and there is a possibility that a sufficient amount of hydrocarbons cannot be produced.

[0006] Therefore, an object of the present disclosure is to provide a hydrocarbon production system and a hydrocarbon production method capable of securing water and producing hydrocarbons even in regions where it is difficult to secure water such as desert areas.

[0007] The hydrocarbon production system according to the present disclosure includes a carbon dioxide recovery device that recovers carbon dioxide and water from air in the atmosphere, and a hydrogen production device that produces hydrogen from the water recovered by the carbon dioxide recovery device. The hydrocarbon production system includes a hydrocarbon production device that produces a reaction product containing hydrocarbons from a raw material containing carbon dioxide recovered by the carbon dioxide recovery device and hydrogen produced by the hydrogen production device.

[0008] A carbon dioxide recovery device may produce a desorbed gas by desorbing carbon dioxide and water. A hydrocarbon production system may include a first gas-liquid separator that cools the desorbed gas and separates it into a first gas containing carbon dioxide and a first liquid containing water. A hydrogen production device may produce hydrogen from the water contained in the first liquid.

[0009] The reaction product may contain water vapor. The hydrocarbon production system may include a second gas-liquid separator for cooling the reaction product and separating it into a second gas containing hydrocarbons and water vapor, and a second liquid containing water. The hydrocarbon production system may also include a steam production device for producing water vapor from the water contained in the second liquid to be supplied to a carbon dioxide recovery device.

[0010] The reaction product may contain water vapor. The hydrocarbon production system may include a second gas-liquid separator for cooling the reaction product and separating it into a second gas containing hydrocarbons and water vapor and a second liquid containing water. The hydrocarbon production system may also include a third gas-liquid separator for cooling the second gas and separating it into a third gas containing hydrocarbons and a third liquid containing water. The hydrogen production apparatus may produce hydrogen from the water contained in the third liquid.

[0011] The hydrogen production device may produce hydrogen and oxygen from water. The hydrocarbon production system may include a combustion device that burns a portion of the hydrocarbons produced in the hydrocarbon production device with an oxidizing gas containing oxygen produced in the hydrogen production device, generating steam from the heat of combustion. The steam generated in the combustion device may be supplied to a carbon dioxide recovery device.

[0012] The hydrocarbon production system may include a combustion device that burns a portion of the hydrocarbons produced in the hydrocarbon production device with an oxidizing gas containing oxygen produced in the hydrogen production device. The heat of combustion generated in the combustion device may be supplied to the hydrocarbon production device.

[0013] The hydrocarbon production system may include a combustion device that burns a portion of the hydrocarbons produced in the hydrocarbon production device with an oxidizing gas containing oxygen produced in the hydrogen production device. The carbon dioxide recovery device may recover the carbon dioxide generated by the combustion of hydrocarbons in the combustion device.

[0014] The hydrocarbon production method described herein involves recovering carbon dioxide and water from atmospheric air in a first apparatus. The hydrocarbon production method involves producing hydrogen from the water recovered in the first apparatus in a second apparatus. The hydrocarbon production method involves producing a reaction product containing hydrocarbons from raw materials including carbon dioxide recovered in the first apparatus and hydrogen produced in the second apparatus.

[0015] According to this disclosure, it is possible to provide a hydrocarbon production system and hydrocarbon production method that enable the production of hydrocarbons even in areas where it is difficult to secure water, such as desert regions.

[0016] Figure 1 is a schematic diagram showing a hydrocarbon production system according to one embodiment.

[0017] Several exemplary embodiments will be described below with reference to the drawings. Note that the dimensional ratios in the drawings are exaggerated for illustrative purposes and may differ from the actual ratios.

[0018] As shown in Figure 1, the hydrocarbon production system 1 according to this embodiment includes a carbon dioxide recovery device 10, a steam production device 14, a first gas-liquid separator 15, a hydrogen production device 30, a hydrocarbon production device 40, a second gas-liquid separator 50, a third gas-liquid separator 60, and a combustion device 80.

[0019] The carbon dioxide recovery device 10 recovers carbon dioxide and water from the air in the atmosphere. Specifically, the carbon dioxide recovery device 10 adsorbs carbon dioxide from the air using an adsorbent 12. The carbon dioxide recovery device 10 also adsorbs water from moisture in the air using an adsorbent 12. Then, the carbon dioxide recovery device 10 desorbs the carbon dioxide and water adsorbed on the adsorbent 12 to generate a desorbed gas. The desorbed gas contains carbon dioxide and water. The carbon dioxide recovery device 10 can recover carbon dioxide and water by adsorption and desorption of carbon dioxide and water. The carbon dioxide recovery device 10 includes a tank 11, an adsorbent 12, and a heating device 13.

[0020] The tank 11 has an air supply port 11a, an air outlet 11b, a water vapor supply port 11c, and a desorption gas outlet 11d. The air supply port 11a supplies air into the tank 11. The air outlet 11b discharges the air supplied into the tank 11 from the air supply port 11a to the atmosphere outside the tank 11. The air outlet 11b is connected to an air discharge channel 11e, and air is discharged from inside the tank 11 through the air outlet 11b to the air discharge channel 11e. A damper 11f is provided in the air discharge channel 11e. The damper 11f can be opened and closed within the air discharge channel 11e, and is configured so that when the air discharge channel 11e is open, air is discharged from inside the tank 11, and when the air discharge channel 11e is closed, air is not discharged from inside the tank 11.

[0021] The steam supply port 11c supplies steam to the adsorbent 12 in the tank 11. By supplying steam to the adsorbent 12, the desorption of carbon dioxide from the adsorbent 12 can be promoted. A first flow path L1 is connected to the steam supply port 11c. A steam production device 14 is connected to the first flow path L1. An on-off valve 14d is also provided in the first flow path L1. The on-off valve 14d is configured such that when the valve is open, steam is supplied from the steam production device 14 to the carbon dioxide recovery device 10, and when the valve is closed, steam does not flow through the first flow path L1.

[0022] The steam generating apparatus 14 produces steam to be supplied to the carbon dioxide recovery apparatus 10. The steam generating apparatus 14 includes a storage section 14a for storing water, a heater 14b for heating the steam generated from the water in the storage section 14a, and an AC power supply 14c electrically connected to the heater 14b. In this embodiment, the storage section 14a is a tank. The heater 14b generates heat when electricity flows from the AC power supply 14c. The AC power supply 14c may also be a DC power supply. The steam heated by the heater 14b is supplied into the tank 11 via the steam supply port 11c. By supplying steam into the tank 11, the adsorbent 12 is heated from the inside and the partial pressure of carbon dioxide can be lowered, thereby promoting the desorption of carbon dioxide adsorbed on the adsorbent 12. The carbon dioxide recovery apparatus 10 can also promote desorption by heating with a heating device 13, which will be described later.

[0023] The desorption gas outlet 11d discharges the desorption gas that has passed through the tank 11. The desorption gas outlet 11d is connected to the first gas-liquid separator 15, and the desorption gas, which contains carbon dioxide and water desorbed from the adsorbent 12, is discharged from the tank 11 through the desorption gas outlet 11d. A second flow path L2 is connected to the desorption gas outlet 11d, and the desorption gas discharged from the tank 11 is supplied to the first gas-liquid separator 15.

[0024] The adsorbent 12 adsorbs carbon dioxide and water from the air in the atmosphere. The adsorbent 12 may contain at least one selected from the group consisting of porous materials, alkali metals, and alkaline earth metals. These materials can efficiently adsorb carbon dioxide. The porous material may contain at least one selected from the group consisting of zeolite, alumina, silica, resin, clay, and activated carbon. The adsorbent 12 containing alkali metals may contain at least one of alkali metal carbonates and lithium transition metal composite oxides. The adsorbent 12 containing alkaline earth metals may contain alkaline earth metal oxides, etc. The adsorbent 12 may contain at least one of a porous material on which a basic substance is supported on the surface, and a porous material on which the surface is modified with a base. Such materials have a large specific surface area and high reactivity of the base to carbon dioxide, making it possible to adsorb a large amount of carbon dioxide. The porous material may be one of those described above. The basic substance may also contain at least one amine compound selected from the group consisting of primary amine compounds, secondary amine compounds, and tertiary amine compounds. Furthermore, the base used to modify the surface of the porous material may be an amino group. These materials can be obtained by immersing the porous material in the aforementioned amine compound, drying it, and then supporting or modifying the surface of the porous material with a basic substance. Alternatively, these materials can be obtained by modifying the porous material with a basic substance using a chemical reaction such as the de-alcoholization reaction between the porous material surface and the amine compound.

[0025] The heating device 13 heats the adsorbent 12. Heating the adsorbent 12 can promote the desorption of carbon dioxide adsorbed on the adsorbent 12. The heating device 13 includes a heater 13a and an AC power supply 13b electrically connected to the heater 13a. The heater 13a generates heat when electricity flows from the AC power supply 13b. The heater 13a may be provided so as to surround the adsorbent 12, or it may be embedded inside the adsorbent 12. The heating device 13 may include at least one selected from the group consisting of a band heater, film heater, plate heater, sheath heater, tube heater, hose heater, plug heater, and flange heater. The heating device 13 may also heat the adsorbent 12 by at least one selected from the group consisting of induction heating, resistance heating, microwave heating, millimeter-wave heating, and heat exchanger. In the case of a heat exchanger, piping may be placed around the adsorbent 12 and hot water or steam may be supplied into the piping. Note that the AC power supply 13b may be a DC power supply.

[0026] The first gas-liquid separator 15 cools the desorbed gas and separates it into a first gas GAS1 containing carbon dioxide and a first liquid LIQ1 containing water. The first gas-liquid separator 15 includes a cooler 15a and a first gas-liquid separator 15b. A second flow path L2 is connected to the carbon dioxide recovery device 10, and the second flow path is configured to allow the desorbed gas to flow through it. The second flow path L2 is provided with a cooler 15a, an on-off valve 15c, and a first gas-liquid separator 15b. The cooler 15a cools the desorbed gas. The first gas-liquid separator 15b separates the desorbed gas cooled by the cooler 15a into a first liquid LIQ1 containing water and a first gas GAS1 containing carbon dioxide. The on / off valve 15c is configured such that when the valve is open, the desorbed gas is supplied from the carbon dioxide recovery device 10 to the first gas-liquid separator 15b, and when the valve is closed, the desorbed gas does not flow through the second flow path L2. A third flow path L3 is connected to the first gas-liquid separator 15b. The third flow path L3 is configured so that the first gas GAS1 flows through it.

[0027] The third flow path L3 connects the first gas-liquid separator 15 and the mixer 35. The third flow path L3 is equipped with an on-off valve 16, a vacuum pump 17, an on-off valve 18, a compressor 19, a first gas tank 20, and an on-off valve 21. A fourth flow path L4 is connected between the vacuum pump 17 and the on-off valve 18 in the third flow path L3. An on-off valve 22 is provided in the fourth flow path L4. The mixer 35 is connected to the third flow path L3, the fifth flow path L5, and the sixth flow path L6.

[0028] The on-off valve 16 is configured such that when the valve is open, the first gas GAS1 is supplied from the first gas-liquid separator 15b to the vacuum pump 17, and when the valve is closed, the first gas GAS1 does not flow through the third flow path L3. The vacuum pump 17 reduces the pressure inside the tank 11 of the carbon dioxide recovery device 10, promoting the desorption of carbon dioxide and water. The on-off valve 18 is configured such that when the valve is open, the first gas GAS1 is supplied from the vacuum pump 17 to the first gas tank 20, and when the valve is closed, the first gas GAS1 does not flow through the third flow path L3. The compressor 19 compresses the first gas GAS1 separated in the first gas-liquid separator 15 and sends it to the first gas tank 20. The first gas tank 20 stores the first gas GAS1 separated in the first gas-liquid separator 15. The on-off valve 21 is configured such that when the valve is open, the first gas GAS1 is supplied from the first gas tank 20 to the mixer 35, and when the valve is closed, the first gas GAS1 does not flow from the first gas tank 20 to the mixer 35. The on-off valve 22 is configured such that when the valve is open, the first gas GAS1 is released into the atmosphere from the first gas-liquid separator 15, and when the valve is closed, the first gas GAS1 does not flow through the fourth flow path L4. In the fourth flow path L4, gas with a relatively low concentration of carbon dioxide, such as in the initial stages of operation, flows and is released into the atmosphere. Note that the gas released from the fourth flow path L4, with a carbon dioxide concentration of, for example, 2000 ppm to 4000 ppm, may be diluted to 800 ppm to 1000 ppm or so and used as a carbon dioxide source supplied in greenhouse horticulture.

[0029] The hydrogen production apparatus 30 produces hydrogen from water recovered by the carbon dioxide recovery apparatus 10. The hydrogen production apparatus 30 may also produce hydrogen and oxygen from water. The hydrogen production apparatus 30 includes a pure water device 31, an electrolytic device 32, and a hydrogen tank 33. The pure water device 31, the electrolytic device 32, and the hydrogen tank 33 are located in the fifth flow path L5. A shut-off valve 34 is also provided in the fifth flow path L5.

[0030] The pure water system 31 produces pure water. The pure water system 31 may include at least one of a distilled water production system, an ion exchange resin pure water production system, and an RO water production system. The distilled water production system produces distilled water by distilling water. The ion exchange resin pure water production system produces pure water by passing water through an ion exchange resin layer. The RO water production system includes an RO (reverse osmosis) membrane and produces RO water by passing water through the RO membrane. The resistivity of pure water at 25°C may be 0.1 MΩ·cm or more and 18.24 MΩ·cm or less, and may be 1 MΩ·cm to 10 MΩ·cm.

[0031] The electrolytic device 32 electrolyzes water to produce hydrogen and oxygen from it. The electrolytic device 32 may be at least one type of electrolytic device selected from the group consisting of alkaline water electrolytic devices, polymer electrolyte water electrolytic devices, and solid oxide water electrolytic devices. The electrolytic device 32 may also use renewable energy such as solar, wind, and hydroelectric power to electrolyze water. This reduces carbon dioxide emissions for the hydrocarbon production system 1 as a whole.

[0032] The hydrogen tank 33 stores the hydrogen produced by the electrolytic device 32. The shut-off valve 34 is configured such that when the valve is open, hydrogen is supplied from the hydrogen tank 33 to the hydrocarbon production device 40, and when the valve is closed, hydrogen does not flow through the fifth flow path L5.

[0033] Mixer 35 mixes carbon dioxide recovered by carbon dioxide recovery device 10 with hydrogen produced by hydrogen production device 30. The raw material containing carbon dioxide and hydrogen mixed in mixer 35 is supplied to hydrocarbon production device 40. The molar ratio of hydrogen to carbon dioxide supplied to hydrocarbon production device 40 can be set as appropriate, but may be 1 or more, 2 or more, 3 or more, 3.5 or more, or 4 or more. Also, the molar ratio of hydrogen to carbon dioxide supplied to hydrocarbon production device 40 may be less than 8, less than 6, less than 5, or less than 4.5. The raw material containing carbon dioxide and hydrogen mixed in mixer 35 is heated in heat exchanger 51 and supplied to hydrocarbon production device 40.

[0034] The hydrocarbon production apparatus 40 produces reaction products containing hydrocarbons from raw materials including carbon dioxide recovered by the carbon dioxide recovery apparatus 10 and hydrogen produced by the hydrogen production apparatus 30. The reaction products may contain water vapor. By producing hydrocarbons in the hydrocarbon production apparatus 40, carbon dioxide emissions can be suppressed, and carbon dioxide can be utilized effectively.

[0035] The hydrocarbons produced in the hydrocarbon production apparatus 40 may contain at least one of alkanes and alkenes. These hydrocarbons can be produced by a methanation reaction or an FT (Fischer-Tropsch) reaction. The hydrocarbons produced in the hydrocarbon production apparatus 40 may be used as sustainable aviation fuel (SAF). At least one of the alkanes and alkenes may contain at least one hydrocarbon having 1 to 100 carbon atoms. At least one of the alkanes and alkenes may contain at least one hydrocarbon having 1 to 4 carbon atoms. For example, the alkanes may include at least one selected from the group consisting of methane, ethane, propane, and butane. For example, the alkenes may include at least one selected from the group consisting of ethylene, propylene, 1-butene, 2-butene, isobutene, and 1,3-butadiene. Methane, ethane, and propane can be used as fuel for city gas. In addition, alkenes with 2 to 4 carbon atoms are useful as raw materials for plastics. The reaction products generated in the hydrocarbon production apparatus 40 may also contain compounds other than those mentioned above.

[0036] The hydrocarbon production apparatus 40 includes a reactor 41, a heat transfer medium tank 42, a heat transfer medium pump 43, and a cooler 44. The reactor 41, the heat transfer medium tank 42, and the heat transfer medium pump 43 are located in a seventh flow path L7. In this embodiment, the seventh flow path L7 is a circulation flow path.

[0037] Reactor 41 is connected to a sixth flow path L6, and a heat exchanger 51 is provided in the sixth flow path L6. The raw materials, including carbon dioxide and hydrogen mixed in mixer 35, are heated in the heat exchanger 51 and supplied to reactor 41. Reactor 41 may include a fixed-bed reactor. Fixed-bed reactors have a relatively simple structure and can be configured simply. The fixed-bed reactor may be a single-tube reactor or a multi-tube reactor such as a shell-and-tube reactor. The fixed-bed reactor may include reaction tubes and a shell that houses the reaction tubes. By passing a heat transfer medium as a cooling medium outside the reaction tubes inside the shell, the reaction heat generated by hydrocarbon production in reactor 41 can be removed.

[0038] A catalyst may be placed inside the reactor 41. Contact between the raw materials and the catalyst can promote the reaction between carbon dioxide and hydrogen contained in the raw materials. The catalyst may include at least one selected from the group consisting of, for example, nickel catalysts, ruthenium catalysts, iron catalysts, and cobalt catalysts. The catalyst can be selected from the viewpoint of the type of hydrocarbon produced. Nickel catalysts or ruthenium catalysts can be used in methanation reactions to produce methane. Iron catalysts and cobalt catalysts can be used in FT reactions. Iron catalysts can mainly produce light hydrocarbons, and cobalt catalysts can mainly produce heavy hydrocarbons containing wax. Furthermore, iron catalysts can mainly produce alkenes and alkanes, and cobalt catalysts can mainly produce alkanes. Note that a nickel catalyst is a catalyst containing nickel as an active ingredient. A ruthenium catalyst is a catalyst containing ruthenium as an active ingredient. An iron catalyst is a catalyst containing iron as an active ingredient. A cobalt catalyst is a catalyst containing cobalt as an active ingredient. The content of the active ingredient may be 20% by mass or more of the total catalyst.

[0039] In addition, reactor 41 may include reactors other than fixed-bed reactors, either in addition to or in place of fixed-bed reactors. Reactor 41 may include at least one reactor selected from the group consisting of fixed-bed reactors, slurry-bed reactors, and fluidized-bed reactors. The reaction conditions in reactor 41 are not particularly limited, but for example, the reaction temperature may be 200°C to 500°C and the pressure may be 0.3 MPaG to 3 MPaG.

[0040] The heat transfer medium tank 42 stores the heat transfer medium. The heat transfer medium may be a known heat transfer medium such as steam or oil. The heat transfer medium pump 43 supplies the heat transfer medium stored in the heat transfer medium tank 42 to the reactor 41 and circulates the heat transfer medium in the seventh flow channel L7. Since the reaction in the reactor 41 is an exothermic reaction, cooling the reactor 41 with the heat transfer medium improves the reaction efficiency of the reactor 41 and allows the temperature inside the reactor 41 to be kept constant. To maintain the temperature of the heat transfer medium appropriately, a cooler 44 may be installed in the seventh flow channel L7.

[0041] The second gas-liquid separator 50 cools the reaction products and separates them into a second gas GAS2 containing hydrocarbons and water vapor, and a second liquid LIQ2 containing water. The second gas-liquid separator 50 includes a heat exchanger 51 and a gas-liquid separator 52. The heat exchanger 51 and the gas-liquid separator 52 are located in the eighth flow path L8. The reactor 41 is connected to the eighth flow path L8.

[0042] The heat exchanger 51 exchanges heat between the raw materials supplied to the hydrocarbon production apparatus 40 and the reaction products produced in the hydrocarbon production apparatus 40. Specifically, the heat exchanger 51 heats the raw materials supplied to the hydrocarbon production apparatus 40 and cools the reaction products produced in the hydrocarbon production apparatus 40. Since the reaction in the hydrocarbon production apparatus 40 is an exothermic reaction, the energy efficiency of the hydrocarbon production system 1 can be improved by exchanging the heat between the raw materials and the reaction products. The heat exchanger 51 also cools the reaction products produced in the hydrocarbon production apparatus 40. Therefore, by cooling the reaction products in the heat exchanger 51, the water contained in the reaction products can be condensed.

[0043] The gas-liquid separator 52 separates the reaction product cooled by the heat exchanger 51 into a second gas GAS2 containing hydrocarbons and water vapor and a second liquid LIQ2 containing water. A ninth flow path L9 through which the second liquid LIQ2 flows and a tenth flow path L10 through which the second gas GAS2 flows are connected to the gas-liquid separator 52.

[0044] The ninth flow path L9 is connected to the water vapor production device 14, and the second liquid LIQ2 separated by the second gas-liquid separation device 50 is supplied to the water vapor production device 14. An on-off valve 36 is provided in the ninth flow path L9. When the valve is open, the second liquid LIQ2 is supplied from the second gas-liquid separation device 50 to the water vapor production device 14, and when the valve is closed, the second liquid LIQ2 is configured not to flow in the ninth flow path L9.

[0045] The water vapor production device 14 may produce water vapor to be supplied to the carbon dioxide recovery device 10 from the water contained in the second liquid LIQ2. Then, the carbon dioxide adsorbed by the adsorbent 12 may be desorbed by the water vapor produced by the water vapor production device 14. With such a configuration, water vapor can be produced from the water recovered from the reaction product. Therefore, the water produced as a by-product in the hydrocarbon production device 40 can be effectively utilized.

[0046] The third gas-liquid separation device 60 cools the second gas GAS2 and separates it into a third gas GAS3 containing hydrocarbons and a third liquid LIQ3 containing water. The third gas-liquid separation device 60 includes a cooler 61 and a gas-liquid separator 62. The cooler 61 and the gas-liquid separator 62 are provided in the tenth flow path L10.

[0047] The cooler 61 cools the second gas GAS2 separated by the second gas-liquid separator 50. The second gas GAS2 contains water that remained unseparated in the second gas-liquid separator 50. Therefore, by cooling the second gas GAS2 with the cooler 61, the water contained in the second gas GAS2 can be condensed. The cooling temperature in the cooler 61 may be lower than the cooling temperature in the heat exchanger 51. Thereby, the condensation of the water contained in the second gas GAS2 can be promoted. In the present embodiment, the cooler 61 is a heat exchanger that exchanges the heat of the second gas GAS2 separated by the second gas-liquid separator 50 and the heat of the cooling water of the cooling tower 63.

[0048] The cooler 61 is connected to the eleventh flow path L11. In the present embodiment, the eleventh flow path L11 is a circulation flow path. The eleventh flow path L11 is provided with a cooling tower 63, a cooling water pump 64, an on-off valve 65, and an on-off valve 66. The cooling tower 63 cools the water supplied to the cooler 61. The cooling tower 63 stores the water supplied to the cooler 61 and cools the stored water with a fan or the like. The cooling water pump 64 supplies the cooling water in the cooling tower 63 to the cooler 61. The on-off valve 65 is configured such that when the valve is open, the cooling water is supplied from the cooling tower 63 to the cooler 61, and when the valve is closed, the cooling water does not flow in the eleventh flow path L11. The on-off valve 66 is configured such that when the valve is open, the cooling water is supplied from the cooler 61 to the cooling tower 63, and when the valve is closed, the cooling water does not flow in the eleventh flow path L11.

[0049] The gas-liquid separator 62 separates the second gas GAS2 cooled by the cooler 61 into a third gas GAS3 containing hydrocarbons and a third liquid LIQ3 containing water. The gas-liquid separator 62 is connected to a twelfth flow path L12 through which the third liquid LIQ3 flows and a thirteenth flow path L13 through which the third gas GAS3 flows. The third liquid LIQ3 is supplied to the cooling water tank 67 through the twelfth flow path L12. The third gas GAS3 is supplied to the third gas tank 72 and the combustion device 80 through the thirteenth flow path L13.

[0050] The 12th flow path L12 is connected to the cooling water tank 67, and the third liquid LIQ3 separated by the third gas-liquid separator 60 is supplied to the cooling water tank 67 through the 12th flow path L12. The 12th flow path L12 is also provided with an on-off valve 68. The on-off valve 68 is configured such that when the valve is open, the third liquid LIQ3 is supplied from the third gas-liquid separator 60 to the cooling water tank 67, and when the valve is closed, the third liquid LIQ3 does not flow through the 12th flow path L12.

[0051] The cooling water tank 67 and the first gas-liquid separator 15b of the first gas-liquid separator 15 are connected by a 14th flow path L14. An on-off valve 69 is provided in the 14th flow path L14. The on-off valve 69 is configured such that when the valve is open, the first liquid LIQ1 is supplied from the first gas-liquid separator 15b to the cooling water tank 67, and when the valve is closed, the first liquid LIQ1 does not flow through the 14th flow path L14. The cooling water tank 67 is also connected to a 15th flow path L15. A pump 70 is provided in the 15th flow path L15. The water contained in the first liquid LIQ1 and the third liquid LIQ3 stored in the cooling water tank 67 is supplied to the pure water device 31 by the pump 70.

[0052] The hydrogen production apparatus 30 may produce hydrogen from water contained in at least one of the first liquid LIQ1 and the third liquid LIQ3. That is, the hydrogen production apparatus 30 may produce hydrogen from water contained in the first liquid LIQ1. Alternatively, the hydrogen production apparatus 30 may produce hydrogen from water contained in the third liquid LIQ3. By producing hydrogen from water contained in the first liquid LIQ1, the water recovered by the carbon dioxide recovery apparatus 10 can be effectively utilized. Furthermore, by producing hydrogen from water contained in the third liquid LIQ3, the water produced as a by-product in the hydrocarbon production apparatus 40 can be effectively utilized.

[0053] A fifth flow path L5 is connected between the pump 70 and the pure water system 31 in the 15th flow path L15. The 15th flow path L15 is also connected to the cooling tower 63. An on-off valve 71 is provided in the 15th flow path L15. The on-off valve 71 is configured such that when the valve is open, liquid containing water is supplied from the cooling water tank 67 to the cooling tower 63, and when the valve is closed, liquid containing water does not flow through the 15th flow path L15.

[0054] The cooler 61 may cool the second gas GAS2 using water contained in at least one of the first liquid LIQ1 and the third liquid LIQ3. That is, the cooler 61 may cool the second gas GAS2 using water contained in the first liquid LIQ1. Alternatively, the cooler 61 may cool the second gas GAS2 using water contained in the third liquid LIQ3. By cooling the second gas GAS2 using water contained in the first liquid LIQ1, the water recovered in the carbon dioxide recovery device 10 can be effectively utilized. Furthermore, by cooling the second gas GAS2 using water contained in the third liquid LIQ3, the water produced as a by-product in the hydrocarbon production device 40 can be effectively utilized.

[0055] The third gas tank 72 is connected to the 13th flow path L13. The third gas tank 72 stores the third gas GAS3, which contains hydrocarbons, separated by the third gas-liquid separator 60. The 13th flow path L13 is also provided with an on-off valve 73. When the valve 73 is open, the third gas GAS3 is supplied from the third gas-liquid separator 60 to the third gas tank 72, and when the valve is closed, water is prevented from flowing through the 13th flow path L13. The 16th flow path L16 is connected between the gas-liquid separator 62 of the 13th flow path L13 and the third gas tank 72. The 16th flow path L16 is also connected to the combustion device 80. The 16th flow path L16 is provided with an on-off valve 74. The on / off valve 74 is configured such that when the valve is open, the third gas GAS3 is supplied from the third gas-liquid separator 60 to the combustion device 80, and when the valve is closed, the third gas GAS3 does not flow through the 16th flow path L16. In the initial stages of operation, a gas with a relatively low concentration of hydrocarbons may flow through the 16th flow path L16 and be supplied to the combustion device 80.

[0056] The combustion device 80 burns a portion of the hydrocarbons produced in the hydrocarbon production device 40 with an oxidizing gas containing oxygen produced in the hydrogen production device 30. In this embodiment, the combustion device 80 is a boiler, and it burns a portion of the hydrocarbons produced in the hydrocarbon production device 40 with an oxidizing gas containing oxygen produced in the hydrogen production device 30, generating steam from the heat of combustion. The combustion device 80 is connected to the hydrogen production device 30 via the 17th flow path L17. The oxygen produced in the hydrogen production device 30 is supplied to the combustion device 80 through the 17th flow path L17. The oxidizing gas used for combustion in the combustion device 80 may include air from the atmosphere in addition to the oxygen produced in the hydrogen production device 30.

[0057] The steam generated in the combustion device 80 may be supplied to the carbon dioxide recovery device 10. This configuration allows for a reduction in the amount of steam produced by the steam production device 14. As a result, the overall energy efficiency of the hydrocarbon production system 1 can be reduced.

[0058] The combustion heat generated in the combustion device 80 may be supplied to the hydrocarbon production device 40. This configuration reduces the amount of energy supplied to the hydrocarbon production device 40. As a result, the overall energy efficiency of the hydrocarbon production system 1 can be improved.

[0059] The carbon dioxide recovery device 10 may recover carbon dioxide generated by the combustion of hydrocarbons in the combustion device 80. This configuration can reduce the amount of carbon dioxide released into the atmosphere. Furthermore, hydrocarbons can be produced from the carbon dioxide recovered by the carbon dioxide recovery device 10. Therefore, the carbon dioxide recovery efficiency of the hydrocarbon production system 1 can be improved.

[0060] The combustion device 80 is connected to the 18th flow path L18. The 18th flow path L18 is connected to the carbon dioxide recovery device 10. The combustion gas produced by the combustion device 80 is supplied to the carbon dioxide recovery device 10 through the 18th flow path L18. The 18th flow path L18 is equipped with an air blower 81 and a damper 82. The air blower 81 supplies the combustion gas, which contains carbon dioxide produced in the combustion device 80, to the carbon dioxide recovery device 10. The damper 82 is configured so that when the flow path is open, the combustion gas is supplied from the combustion device 80 to the carbon dioxide recovery device 10, and when the flow path is closed, the combustion gas does not flow through the 18th flow path L18.

[0061] A 19th flow path L19 is connected between the air blower 81 and the damper 82 in the 18th flow path L18. The 19th flow path L19 is provided with an air intake port 83 and a damper 84. The air intake port 83 takes in air from the atmosphere into the 19th flow path L19 and supplies the air from the atmosphere to the carbon dioxide recovery device 10. The damper 84 is configured so that when the flow path is open, air from the atmosphere is supplied to the carbon dioxide recovery device 10, and when the flow path is closed, air from the atmosphere does not flow through the 19th flow path L19. The proportion of air from the atmosphere in the air supplied to the carbon dioxide recovery device 10 may be, for example, 99% by volume or more. Also, the proportion of combustion gas supplied from the combustion device 80 in the air supplied to the carbon dioxide recovery device 10 may be, for example, 1% by volume or less.

[0062] In this embodiment, an example was described in which the hydrogen production apparatus 30 produces hydrogen from water contained in the first liquid LIQ1 and the third liquid LIQ3. Furthermore, an example was described in which the cooler 61 cools the second gas GAS2 using water contained in at least one of the first liquid LIQ1 and the third liquid LIQ3. However, the second liquid LIQ2 may also be used as the water source. Additionally, water contained in at least one selected from the group consisting of the first liquid LIQ1, the second liquid LIQ2, and the third liquid LIQ3 may be used as drinking water or other domestic water, or as cooling water for each device.

[0063] Next, the operation and effects of the hydrocarbon production system 1 and hydrocarbon production method according to this embodiment will be described.

[0064] As described above, the hydrocarbon production system 1 includes a carbon dioxide recovery device 10 that recovers carbon dioxide and water from the air in the atmosphere, and a hydrogen production device 30 that produces hydrogen from the water recovered by the carbon dioxide recovery device 10. The hydrocarbon production system 1 also includes a hydrocarbon production device 40 that produces a reaction product containing hydrocarbons from raw materials containing carbon dioxide recovered by the carbon dioxide recovery device 10 and hydrogen produced by the hydrogen production device 30.

[0065] Furthermore, the hydrocarbon production method involves recovering carbon dioxide and water from the air using a carbon dioxide recovery device 10 (first device). The hydrocarbon production method involves producing hydrogen from the water recovered by the carbon dioxide recovery device 10 using a hydrogen production device 30 (second device). The hydrocarbon production method involves producing a reaction product containing hydrocarbons from raw materials containing carbon dioxide recovered by the carbon dioxide recovery device 10 and hydrogen produced by the hydrogen production device 30.

[0066] The carbon dioxide capture device 10 captures water in addition to carbon dioxide from the air. The hydrogen production device 30 then produces hydrogen from the water captured by the carbon dioxide capture device 10. Furthermore, the hydrocarbon production device 40 produces reaction products containing hydrocarbons from raw materials that include the carbon dioxide captured by the carbon dioxide capture device 10 and the hydrogen produced by the hydrogen production device 30. Therefore, the hydrocarbon production system 1 and hydrocarbon production method according to this embodiment can produce hydrocarbons from carbon dioxide and water in the air. Consequently, hydrocarbons can be produced even in areas where it is difficult to secure water, such as desert areas, by securing water.

[0067] The carbon dioxide recovery device 10 may desorb carbon dioxide and water to produce a desorbed gas. The hydrocarbon production system 1 may include a first gas-liquid separator 15 that cools the desorbed gas and separates it into a first gas GAS1 containing carbon dioxide and a first liquid LIQ1 containing water. The hydrogen production device 30 may produce hydrogen from the water contained in the first liquid LIQ1.

[0068] This configuration allows for efficient recovery of water from the air. Furthermore, by producing hydrogen from the water contained in the first liquid LIQ1, the water recovered by the carbon dioxide recovery device 10 can be effectively utilized.

[0069] The reaction product may contain water vapor. The hydrocarbon production system 1 may include a second gas-liquid separator 50 that cools the reaction product and separates it into a second gas GAS2 containing hydrocarbons and water vapor, and a second liquid LIQ2 containing water. The hydrocarbon production system 1 may also include a steam production device 14 that produces water vapor from the water contained in the second liquid LIQ2 to be supplied to the carbon dioxide recovery device 10.

[0070] With this configuration, steam can be produced from water recovered from the reaction products. Therefore, water generated as a by-product in the hydrocarbon production apparatus 40 can be effectively utilized. Furthermore, since the water contained in the second liquid LIQ2 is at a higher temperature and pressure than the water contained in the third liquid LIQ3, steam can be easily generated by releasing or reducing the pressure to atmospheric pressure.

[0071] The reaction product may contain water vapor. The hydrocarbon production system 1 may include a second gas-liquid separator 50 that cools the reaction product and separates it into a second gas GAS2 containing hydrocarbons and water vapor and a second liquid LIQ2 containing water. The hydrocarbon production system 1 may also include a third gas-liquid separator 60 that cools the second gas GAS2 and separates it into a third gas GAS3 containing hydrocarbons and a third liquid LIQ3 containing water. The hydrogen production apparatus 30 may produce hydrogen from the water contained in the third liquid LIQ3.

[0072] With this configuration, hydrogen can be produced from water recovered from the reaction product, and the reaction product can be produced from raw materials containing this hydrogen. Therefore, water generated as a by-product in the hydrocarbon production apparatus 40 can be effectively utilized.

[0073] The hydrogen production apparatus 30 may produce hydrogen and oxygen from water. The hydrocarbon production system 1 may include a combustion apparatus 80 that burns a portion of the hydrocarbons produced in the hydrocarbon production apparatus 40 with an oxidizing gas containing oxygen produced in the hydrogen production apparatus 30, and generates steam from the heat of combustion. The steam generated in the combustion apparatus 80 may be supplied to the carbon dioxide recovery apparatus 10.

[0074] This configuration allows for a reduction in the amount of steam produced by the steam production device 14. As a result, the overall energy efficiency of the hydrocarbon production system 1 can be reduced.

[0075] The hydrocarbon production system 1 may include a combustion device 80 that burns a portion of the hydrocarbons produced in the hydrocarbon production apparatus 40 with an oxidizing gas containing oxygen produced in the hydrogen production apparatus 30. The heat of combustion generated in the combustion device 80 may be supplied to the hydrocarbon production apparatus 40.

[0076] This configuration allows for a reduction in the amount of energy supplied to the hydrocarbon production apparatus 40. As a result, the overall energy efficiency of the hydrocarbon production system 1 can be reduced.

[0077] The hydrocarbon production system 1 may include a combustion device 80 that burns a portion of the hydrocarbons produced in the hydrocarbon production apparatus 40 with an oxidizing gas containing oxygen produced in the hydrogen production apparatus 30. The carbon dioxide recovery device 10 may recover the carbon dioxide generated by the combustion of hydrocarbons in the combustion device 80.

[0078] This configuration reduces the amount of carbon dioxide released into the atmosphere. Furthermore, hydrocarbons can be produced from the carbon dioxide recovered by the carbon dioxide recovery device 10. Therefore, the carbon dioxide recovery efficiency of the hydrocarbon production system 1 can be improved.

[0079] The entire contents of Japanese Patent Application No. 2024-174867 (Filing Date: October 4, 2024) are incorporated herein by reference.

[0080] Although several embodiments have been described, it is possible to modify or transform the embodiments based on the above disclosure. All components of the above embodiments, and all features described in the claims, may be taken individually and combined, provided that they do not conflict with each other.

[0081] This disclosure can contribute, for example, to United Nations-led Sustainable Development Goals (SDGs) Goal 6, "Ensure availability and sustainable management of water and sanitation for all," 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."

[0082] 1. Hydrocarbon Production System 10. Carbon Dioxide Recovery Unit (Unit 1) 14. Steam Production Unit 15. First Gas-Liquid Separator 30. Hydrogen Production Unit (Unit 2) 40. Hydrocarbon Production Unit 50. Second Gas-Liquid Separator 60. Third Gas-Liquid Separator 80. Combustion Unit GAS1: First Gas GAS2: Second Gas GAS3: Third Gas LIQ1: First Liquid LIQ2: Second Liquid LIQ3: Third Liquid

Claims

1. A hydrocarbon production system comprising: a carbon dioxide recovery device for recovering carbon dioxide and water from atmospheric air; a hydrogen production device for producing hydrogen from water recovered by the carbon dioxide recovery device; and a hydrocarbon production device for producing a reaction product containing hydrocarbons from raw materials including carbon dioxide recovered by the carbon dioxide recovery device and hydrogen produced by the hydrogen production device.

2. The hydrocarbon production system according to claim 1, wherein the carbon dioxide recovery device desorbs carbon dioxide and water to produce a desorbed gas, the hydrocarbon production system includes a first gas-liquid separation device that cools the desorbed gas and separates it into a first gas containing carbon dioxide and a first liquid containing water, and the hydrogen production device produces hydrogen from the water contained in the first liquid.

3. The hydrocarbon production system according to claim 1 or 2, wherein the reaction product includes water vapor, and the hydrocarbon production system comprises: a second gas-liquid separator for cooling the reaction product and separating it into a second gas containing hydrocarbons and water vapor and a second liquid containing water; and a water vapor production apparatus for producing water vapor from the water contained in the second liquid to be supplied to the carbon dioxide recovery apparatus.

4. The hydrocarbon production system according to any one of claims 1 to 3, wherein the reaction product contains water vapor, the hydrocarbon production system comprises a second gas-liquid separator for cooling the reaction product and separating it into a second gas containing hydrocarbons and water vapor and a second liquid containing water, and a third gas-liquid separator for cooling the second gas and separating it into a third gas containing hydrocarbons and a third liquid containing water, and the hydrogen production apparatus produces hydrogen from the water contained in the third liquid.

5. The hydrocarbon production system according to any one of claims 1 to 4, wherein the hydrogen production apparatus produces hydrogen and oxygen from water, the hydrocarbon production system comprises a combustion apparatus that burns a portion of the hydrocarbon produced in the hydrocarbon production apparatus with an oxidizing gas containing oxygen produced in the hydrogen production apparatus, and generates steam with the heat of combustion, and the steam generated in the combustion apparatus is supplied to the carbon dioxide recovery apparatus.

6. The hydrocarbon production system according to any one of claims 1 to 5, wherein the hydrocarbon production system comprises a combustion device that burns a portion of the hydrocarbon produced in the hydrocarbon production apparatus with an oxidizing gas containing oxygen produced in the hydrogen production apparatus, and the heat of combustion generated in the combustion device is supplied to the hydrocarbon production apparatus.

7. The hydrocarbon production system according to any one of claims 1 to 6, wherein the hydrocarbon production system comprises a combustion device that burns a portion of the hydrocarbons produced in the hydrocarbon production apparatus with an oxidizing gas containing oxygen produced in the hydrogen production apparatus, and the carbon dioxide recovery device recovers the carbon dioxide generated by the combustion of hydrocarbons in the combustion device.

8. A method for producing hydrocarbons, comprising: recovering carbon dioxide and water from atmospheric air in a first apparatus; producing hydrogen from the water recovered in the first apparatus in a second apparatus; and producing a reaction product containing hydrocarbons from raw materials including the carbon dioxide recovered in the first apparatus and the hydrogen produced in the second apparatus.

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