Gas production equipment and gas production method

Abstract

Provided is gas production equipment capable of effectively utilizing heat of a product gas flowing out from a reverse water gas shift reactor. Gas production equipment (1A) comprises: a regeneration tower (7b) that heats an absorption liquid that has adsorbed CO2, thereby desorbing CO2 from the absorption liquid and regenerating the absorption liquid; and a reverse shift reactor (9) that generates a CO-containing product gas through a reverse water gas shift reaction using CO2 introduced from the regeneration tower (7b). The regeneration tower (7b) comprises a heating unit (7c) that heats the absorption liquid using heat possessed by the product gas generated in the reverse shift reactor (9).

Description

Gas production equipment and gas production method

[0001] The present disclosure relates to a gas production facility and a gas production method having a synthesis gas production apparatus that generates a product gas containing CO by a chemical reaction using, for example, CO2.

[0002] Patent Document 1 discloses a method for producing a gas used in a SAF (Sustainable Aviation Fuel) production process. In this document, for the purpose of reducing the heat (electric power) used in the reaction of a SOEC (Solid Oxide Electrolysis Cell), the waste heat of the product gas generated in a reverse water gas shift reactor (synthesis gas production apparatus) is used for heating the raw material gas (CO2, H2O) of the SOEC.

[0003] Japanese Patent Application Laid-Open No. 2024-500221

[0004] However, although Patent Document 1 discloses heat recovery from the product gas synthesized in the reverse water gas shift reactor to the raw material gas of the SOEC, other effective heat utilization has not been sufficiently studied.

[0005] The present disclosure has been made in view of such circumstances, and an object thereof is to provide a gas production facility and a gas production method capable of effectively utilizing the heat possessed by the product gas flowing out from a synthesis gas production apparatus that generates a product gas containing CO by a chemical reaction using CO2.

[0006] The gas production facility according to one aspect of the present disclosure includes an absorption liquid regeneration apparatus that regenerates by desorbing CO2 from an absorption liquid by heating the absorption liquid adsorbed with CO2, and a synthesis gas production apparatus that generates a product gas containing CO by a chemical reaction using the CO2 led from the absorption liquid regeneration apparatus. The absorption liquid regeneration apparatus includes a heating unit that heats the absorption liquid using the heat possessed by the product gas generated in the synthesis gas production apparatus.

[0007] A gas production method according to one aspect of the present disclosure comprises an absorbent liquid regeneration step of regenerating an absorbent liquid by heating an absorbent liquid on which CO2 has been adsorbed to remove CO2 from the absorbent liquid, and a synthesis gas production step of producing a product gas containing CO by a chemical reaction using the CO2 removed in the absorbent liquid regeneration step, wherein the absorbent liquid regeneration step includes a heating step of heating the absorbent liquid using the heat contained in the product gas produced in the synthesis gas production step.

[0008] The heat contained in the product gas flowing out of the reverse water-gas shift reactor can be effectively utilized.

[0009] This is a schematic diagram showing a gas manufacturing facility according to the first embodiment of this disclosure. This is a schematic diagram showing a gas manufacturing facility according to the second embodiment of this disclosure. This is a schematic diagram showing a gas manufacturing facility according to the third embodiment of this disclosure. This is a graph showing the state of heat exchange in the preheating section and heating section in the third embodiment. This is a reference example, a graph showing the state of heat exchange in the preheating section and heating section. This is a schematic diagram showing a gas manufacturing facility according to the fourth embodiment of this disclosure. This is a schematic diagram showing a gas manufacturing facility according to the fifth embodiment of this disclosure.

[0010] Embodiments of the present disclosure will be described below with reference to the drawings. [First Embodiment] The first embodiment of the present disclosure will be described below with reference to Figure 1. Figure 1 shows a gas production facility 1A according to this embodiment. The gas production facility 1A produces hydrocarbon fuels such as SAF (Sustainable Aviation Fuel).

[0011] The gas production facility 1A comprises a biomass boiler power generation device 3, a water electrolysis device 5, a CO2 recovery device 7, a reverse shift reactor (synthesis gas production device) 9, and an FT synthesis device (hydrocarbon fuel production device) 11.

[0012] In this embodiment and subsequent embodiments, the biomass boiler power generation system 3 will be described as an example, but this disclosure is not limited thereto. For example, other boiler power generation equipment using other fuels, such as waste-to-energy facilities or black liquor recovery boilers (for example, boilers used in paper mills), can be used. In addition, other synthesis gas production equipment can be applied instead of the reverse shift reactor 9. For example, a SOEC co-electrolytic device may be provided as the synthesis gas production equipment. In this case, the gas production equipment may be configured to supply H2O together with CO2 to the SOEC co-electrolytic device without providing a water electrolytic device 5.

[0013] The biomass boiler power generation system 3 includes a boiler that generates steam by burning biomass fuel such as wood, and a generator that uses the steam generated in the boiler to rotate a turbine and generate electricity. The electricity generated by the biomass boiler power generation system 3 is supplied to the water electrolysis device 5. The exhaust gas emitted after burning the biomass fuel in the boiler is led to the CO2 recovery device 7.

[0014] The water electrolysis device 5 is, for example, an SOEC (Solid Oxide Electrolysis Cell) and produces H2 (hydrogen) from H2O (steam or water). The electricity used for the water electrolysis device 5 is supplied from the biomass boiler power generation device 3. The H2 generated in the water electrolysis device 5 is supplied to the reverse shift reactor 9 via the hydrogen supply piping 13. Note that the electricity used for the water electrolysis device 5 is not limited to the electricity supplied from the biomass boiler power generation device 3; other renewable energy sources or purchased electricity can also be used.

[0015] The CO2 recovery device 7 recovers CO2 (carbon dioxide) from the exhaust gas supplied by the biomass boiler power generation device 3. The CO2 recovery device 7 uses a chemical absorption method, for example, by using an absorbent liquid that chemically absorbs CO2, such as an amine absorbent.

[0016] The CO2 recovery system 7 comprises an absorption tower 7a and a regeneration tower (absorption liquid regeneration device) 7b. In the absorption tower 7a, an amine absorption liquid is brought into contact with the exhaust gas to absorb CO2 from the exhaust gas. In the regeneration tower 7b, CO2 is desorbed from the absorption liquid that has absorbed CO2. The regeneration tower 7b is equipped with a heating section 7c.

[0017] The absorbent liquid is heated by the heating section 7c. The heating section 7c provides at least a portion of the heat required for the endothermic reaction that removes CO2. As the heated absorbent liquid flows through the regeneration tower 7b, CO2 is removed from the absorbent liquid. The CO2 removed from the absorbent liquid is discharged from the regeneration tower 7b via the CO2 supply pipe 15. The CO2 supply pipe 15 merges with the hydrogen supply pipe 13 to form a combined gas pipe 17. The combined gas pipe 17 is connected to the reverse shift reactor 9.

[0018] The heating section 7c is a heat exchanger, and the absorbent liquid is heated by the product gas introduced from the reverse shift reactor 9. The heating section 7c is equipped with an absorbent liquid supply pipe 7d that supplies the absorbent liquid from the regeneration tower 7b to the heating section 7c, and an absorbent liquid return pipe 7e that returns the absorbent liquid from the heating section 7c to the regeneration tower 7b. The heating temperature in the heating section 7c is, for example, 100°C to 200°C.

[0019] H2 and CO2 are introduced into the reverse shift reactor 9 via the confluence gas piping 17. The reverse shift reactor 9 uses a reverse water-gas shift reaction to produce CO (carbon monoxide) and H2O (water vapor) from H2 and CO2. The reaction temperature of the reverse shift reactor 9 is set to be between 400°C and 1100°C, and the temperature of the product gases (CO, H2O) generated in the reverse shift reactor 9 is set to be between approximately 400°C and 800°C.

[0020] The product gas generated in the reverse shift reactor 9 is guided to the heating section 7c through the upstream product gas piping (product gas flow path) 19. In the heating section 7c, the absorbent liquid is heated by the product gas. The temperature of the product gas in the heating section 7c is, for example, 120°C to 500°C (preferably 200°C or lower). Alternatively, an intermediate fluid such as water or steam may be heated by the heat of the product gas, and the absorbent liquid flowing through the heating section 7c may be heated via the intermediate fluid by guiding the intermediate fluid to the heating section 7c. Furthermore, steam generated in the biomass boiler power generation device 3 may be mixed with the intermediate fluid guided to the heating section 7c.

[0021] After heating the absorbent liquid in the heating section 7c, the generated gas flows through the generated gas downstream piping 21 and is led to the FT synthesis apparatus 11 via the first desuperheater 23, the generated gas downstream compressor 25, and the second desuperheater 27. The cooling medium for each desuperheater 23 and 27 is cooling water available in the gas production equipment 1A. The lower parts of each desuperheater 23 and 27 are designed to discharge condensed drain.

[0022] The FT synthesis unit 11 produces synthetic fuels such as SAF (Sustainable Aviation Fuel) from product gas (CO) using the Fischer-Tropsch process. Alternatively, other hydrocarbon fuel production equipment, such as a methanation unit for synthesizing methane, can be used instead of the FT synthesis unit 11.

[0023] Each of the above-mentioned devices is controlled by a control unit. The control unit consists of, for example, a CPU (Central Processing Unit), RAM (Random Access Memory), ROM (Read Only Memory), and a computer-readable storage medium. A series of processes for realizing various functions are stored in the storage medium in the form of a program, for example. The CPU reads this program into the RAM and performs information processing and calculations to realize the various functions. The program may be pre-installed on the ROM or other storage medium, provided in a state where it is stored on a computer-readable storage medium, or distributed via wired or wireless communication. Computer-readable storage media include magnetic disks, magneto-optical disks, CD-ROMs, DVD-ROMs, semiconductor memory, etc.

[0024] The effects of this embodiment described above are as follows. The reverse water-gas shift reaction is an endothermic reaction requiring high temperatures of 400°C to 1100°C, so the generated gas has a sensible heat of approximately 400°C to 800°C. On the other hand, the CO2 supplied to the reverse water-gas shift reaction is CO2 desorbed from an absorbent liquid on which CO2 has been adsorbed. In order to desorb CO2 from the absorbent liquid, it is necessary to heat the absorbent liquid to about 100°C to 200°C. Therefore, the absorbent liquid is heated in the heating section 7c using the generated gas produced by the reverse water-gas shift reaction. This makes it possible to effectively utilize the heat contained in the generated gas and improve the energy efficiency of the gas production equipment 1A.

[0025] In this embodiment, the generated gas is used exclusively as the heat supplied to the heating section 7c. However, in addition to this, extracted steam from the boiler, low-temperature waste heat, and the combustion heat of tail gas generated from the FT synthesis unit 11 may also be used.

[0026] [Second Embodiment] Next, a second embodiment of the present disclosure will be described with reference to Figure 2. This embodiment differs from the first embodiment in that it is provided with a preheating unit 30. Therefore, in the following, only the changes from the first embodiment will be described, and other similar components will be denoted by the same reference numerals and their descriptions will be omitted.

[0027] In this embodiment, the gas production equipment 1B is provided with a preheating section 30 between the upstream gas production piping 19 and the confluence gas piping 17. The preheating section 30 is a heat exchanger and preheats the upstream gas (H2, CO2) on the upstream side of the reverse shift reactor 9 with the production gas. After heating the upstream gas in the preheating section 30, the production gas heats the absorbent liquid in the heating section 7c.

[0028] The effects and advantages of this embodiment described above are as follows. The upstream gas is heated in the preheating section 30 by the generated gas, and then the absorbent liquid is heated in the heating section 7c. This allows for effective utilization of the sensible heat of the generated gas. Specifically, in order to heat the reverse shift reactor 9 to the high temperature required (400°C to 1100°C), the upstream gas on the upstream side of the reverse shift reactor 9 is heated with a generated gas at 400°C to 800°C. This reduces the amount of fuel required to heat the upstream gas, resulting in energy savings.

[0029] Furthermore, the gas preheated with the generated gas is not limited to the upstream gas flowing through the combined gas piping 17; the upstream gas flowing through the hydrogen supply piping 13 and / or the CO2 supply piping 15 may also be preheated.

[0030] [Third Embodiment] Next, a third embodiment of the present disclosure will be described with reference to Figure 3. This embodiment differs from the second embodiment in that a generated gas compressor 32 is provided. Therefore, in the following, only the changes from the second embodiment will be described, and other similar components will be denoted by the same reference numerals and their descriptions will be omitted.

[0031] The gas production equipment 1C according to this embodiment is equipped with a generated gas compressor 32 in the upstream generated gas piping 19. The generated gas compressor 32 is driven by, for example, an electric motor, and its rotational speed is controlled by a control unit. The generated gas compressor 32 increases the pressure of the generated gas supplied to the heating unit 7c. By increasing the pressure of the generated gas, the partial pressure of water vapor contained in the generated gas is increased, and the condensation temperature of the water vapor is increased. Specifically, the rotational speed of the generated gas compressor 32 is controlled by the control unit so that the condensation temperature of the water vapor corresponds to the target heating temperature in the heating unit 7c. For example, if it is desired to heat the absorbent liquid to 120°C in the heating unit 7c, the target heating temperature is set to 150°C.

[0032] Figure 4A shows a graph illustrating the heat exchange state between the preheating section 30 and the heating section 7c. In this figure, the horizontal axis represents the amount of heat exchanged, and the vertical axis represents the temperature.

[0033] As shown in the figure, while the generated gas, which is about 500°C, cools down to about 150°C in the preheating section 30, the upstream gas flowing through the confluence gas piping 17 is heated from about 100°C to about 450°C. Then, in the heating section 7c, the absorbent liquid is heated to 120°C by the water vapor in the generated gas, which has a condensation temperature of 150°C. In this way, the absorbent liquid is heated in the heating section 7c using the latent heat of condensation of the water vapor contained in the generated gas.

[0034] Figure 4B shows, as a reference example, the amount of heat exchanged when latent heat of condensation is not used (when the generated gas is not pressurized), as in Figure 4A. As can be seen from this figure, since latent heat of condensation cannot be used, the absorbent liquid can only be heated using sensible heat above the condensation temperature (60°C to 80°C), and the amount of heat exchanged cannot be made as large as in Figure 4A (this embodiment).

[0035] The effects of this embodiment described above are as follows: By compressing the generated gas with the generated gas compressor 32, the condensation temperature of the water vapor contained in the generated gas can be increased. As a result, when heating the absorbent liquid in the heating section 7c, the latent heat of condensation can be used at a temperature of 100°C or higher, and a larger amount of heat can be recovered from the generated gas.

[0036] The position of the generated gas compressor 32 may be between the preheating section 30 and the heating section 7c, as shown in Figure 3, or between the reverse shift reactor 9 and the preheating section 30.

[0037] [Fourth Embodiment] Next, a fourth embodiment of the present disclosure will be described with reference to Figure 5. This embodiment differs from the second embodiment in that an upstream gas compressor 34 is provided. Therefore, in the following, only the changes from the second embodiment will be described, and other similar components will be denoted by the same reference numerals and their descriptions will be omitted.

[0038] The gas production equipment 1D according to this embodiment is equipped with an upstream gas compressor 34 in the CO2 supply piping 15. The upstream gas compressor 34 is driven, for example, by an electric motor, and its rotational speed is controlled by a control unit. The upstream gas compressor 34 pressurizes the upstream gas supplied to the reverse shift reactor 9, and consequently increases the pressure of the product gas supplied to the heating unit 7c. By increasing the pressure of the product gas, the partial pressure of water vapor contained in the product gas is increased, thereby raising the condensation temperature of the water vapor. Specifically, the rotational speed of the upstream gas compressor 34 is controlled by the control unit to reach a water vapor condensation temperature corresponding to the target heating temperature in the heating unit 7c.

[0039] Furthermore, a water pump 36 is provided to pump water (liquid) to be supplied to the water electrolysis device 5. The water pump 36 increases the pressure of H2 produced in the water electrolysis device 5.

[0040] Alternatively, instead of the water pump 36, an upstream gas compressor 34 may be installed in the hydrogen supply piping 13. Alternatively, an upstream gas compressor 34 may be installed in the combined gas piping 17.

[0041] The effects of this embodiment described above are as follows: By compressing the upstream gas supplied to the reverse shift reactor 9 with the upstream gas compressor 34, the product gas flowing out of the reverse shift reactor 9 can be pressurized. As a result, when heating the absorbent liquid in the heating section 7c, the latent heat of condensation can be used at a temperature of 100°C or higher, and a larger amount of heat can be recovered from the product gas.

[0042] Since the upstream gas compressor 34 compresses the upstream gas, which is at a lower temperature than the product gas, there is an advantage that the temperature constraint is relaxed compared to the case of compressing the product gas like the product gas compressor 32 of the third embodiment, and the applicable range is wide.

[0043] [Fifth Embodiment] Next, the fifth embodiment of the present disclosure will be described with reference to FIG. 6. This embodiment is different from the second embodiment in that it includes a water separation device 38 using, for example, a water separation membrane or a desiccant. Therefore, hereinafter, only the matters changed from the second embodiment will be described, and the same components will be denoted by the same reference numerals and their description will be omitted.

[0044] The gas production facility 1E according to this embodiment includes a water separation device 38 downstream of the reverse shift reactor 9. The water separation device 38 separates water vapor from the product gas flowing out of the reverse shift reactor 9. The product gas from which water vapor has been separated by the water separation device 38 passes through the product gas upstream pipe 19, is preheated by the upstream gas in the preheating section 30, and then is guided to the FT synthesis device 11 via the first desuperheater 23.

[0045] The water vapor separated by the water separation device 38 is guided through the water vapor pipe 40 to the heating section 7c to heat the absorption liquid. Thereby, the absorption liquid is heated by the water vapor having the heat derived from the product gas.

[0046] A water vapor compressor 42 is provided in the water vapor pipe 40. The water vapor compressor 42 is driven by, for example, an electric motor, and its rotational speed is controlled by a control unit. The water vapor compressor 42 raises the pressure of the water vapor and raises the condensation temperature of the water vapor. Specifically, the rotational speed of the water vapor compressor 42 is controlled by the control unit so that the condensation temperature of the water vapor corresponds to the target heating temperature in the heating section 7c.

[0047] The effects of the present embodiment described above are as follows. The water separation device 38 separates water vapor from the product gas and guides the separated water vapor to the heating section 7c. Thereby, the heat possessed by the water vapor contained in the product gas can be effectively utilized.

[0048] Since the water vapor compressor 42 provided in the water vapor pipe 40 compresses water vapor, the flow rate of water vapor decreases compared to the case of compressing the generated gas before water separation as in the third embodiment, so the compressor power can be reduced. Also, the pipe diameter of the water vapor pipe 40 can be made smaller than the pipe diameter through which the generated gas that does not undergo water separation flows.

[0049] The gas production equipment and gas production method described in each of the embodiments described above can be understood as follows, for example.

[0050] The gas production equipment (1A) according to the first aspect of the present disclosure includes an absorption liquid regeneration device (7b) that regenerates by desorbing CO2 from the absorption liquid by heating the absorption liquid that has adsorbed CO2, and a synthesis gas production device (9) that produces a generated gas containing CO by a chemical reaction using the CO2 led from the absorption liquid regeneration device. The absorption liquid regeneration device includes a heating unit (7c) that heats the absorption liquid using the heat possessed by the generated gas generated by the synthesis gas production device.

[0051] The chemical reaction that produces a generated gas containing CO by a chemical reaction using CO2 is an endothermic reaction and requires a high temperature of 400°C or higher and 1100°C or lower. Therefore, the generated gas has sensible heat of about 400°C to 800°C. On the other hand, as the CO2 supplied to the reverse water gas shift reaction, the CO2 desorbed from the absorption liquid that has adsorbed CO2 is used. To desorb CO2 from the absorption liquid, it is necessary to heat the absorption liquid to about 100°C to 200°C. Therefore, the absorption liquid is heated using the heat possessed by the generated gas generated by the reverse water gas shift reaction. Thereby, the energy efficiency of the gas production equipment can be improved by effectively using the heat possessed by the generated gas.

[0052] The gas production equipment (1B) according to the second aspect of the present disclosure is the gas production equipment according to claim 1, wherein in the first aspect, a preheating unit (30) for preheating the upstream gas led to the synthesis gas production device with the generated gas is provided in the generated gas flow path (19) between the synthesis gas production device and the heating unit.

[0053] The system involves heating the upstream gas in the preheating section with the generated gas, and then heating the absorbent liquid in the heating section. This allows for effective utilization of the sensible heat contained in the generated gas. Specifically, to heat the synthesis gas production apparatus to the required high temperature (400°C to 1100°C), the upstream gas on the upstream side of the synthesis gas production apparatus is heated with the generated gas at 400°C to 800°C. This reduces the amount of fuel required to heat the upstream gas, resulting in energy savings.

[0054] A gas production apparatus (1C) according to a third aspect of this disclosure includes, in the first or second aspect, a product gas compressor (32) for pressurizing the product gas discharged from the synthesis gas production apparatus.

[0055] By compressing the generated gas with a generated gas compressor, the condensation temperature of the water vapor contained in the generated gas can be increased. This allows the latent heat of condensation to be used at a temperature of 100°C or higher when heating the absorbent liquid in the heating section, and more heat can be recovered from the generated gas. The generated gas compressor pressurizes the generated gas so that the heating temperature in the heating section corresponds to the pressure at which the water vapor condenses.

[0056] A gas production apparatus (1D) according to a fourth aspect of the present disclosure includes, in any of the first to third aspects, an upstream gas compressor (34) for pressurizing the upstream gas that is introduced into the synthesis gas production apparatus.

[0057] By compressing the upstream gas with an upstream gas compressor, the product gas flowing out of the synthesis gas production apparatus can be pressurized. This allows the latent heat of condensation to be used at a temperature of 100°C or higher when heating the absorbent liquid in the heating section, and more heat can be recovered from the product gas. The upstream gas compressor pressurizes the upstream gas so that the heating temperature in the heating section is equivalent to the condensation temperature of water vapor. Since the upstream gas compressor compresses the upstream gas, which is at a lower temperature than the product gas, it has the advantage of having less restriction on the operating temperature and a wider range of application compared to the case where the product gas is compressed, as in the product gas compressor of the third embodiment described above.

[0058] A gas production apparatus (1E) according to a fifth aspect of the present disclosure, in any of the first to fourth aspects, includes a water separator (38) for separating water vapor from the product gas discharged from the synthesis gas production apparatus, and the water vapor separated from the water separator is led to the heating section.

[0059] A water separator is used to separate water vapor from the generated gas, and the separated water vapor is guided to the heating section. This allows for effective utilization of the heat contained in the water vapor in the generated gas. Alternatively, a water vapor compressor may be provided to pressurize the water vapor separated by the water separator. This allows for the use of latent heat of condensation in the pressurization section. In this case, the flow rate of water vapor is reduced compared to the generated gas before water separation, thus reducing the compressor power. Furthermore, the diameter of the piping for the water vapor compressor can be made smaller compared to the diameter of the piping for the generated gas that has not undergone water separation. In addition, the generated gas from which water vapor has been separated by the water separator may be used to preheat the upstream gas in a preheating section.

[0060] A gas production facility (1A, 1B, 1C, 1D, 1E) according to a sixth aspect of the present disclosure includes a hydrocarbon fuel production facility (11) into which product gas discharged from the synthesis gas production facility is introduced to produce hydrocarbon fuel, in any of the first to fifth aspects.

[0061] Hydrocarbon fuels can be produced using CO contained in the generated gas. Examples of hydrocarbon fuel production equipment include SAF synthesis equipment that produces SAF using the Fischer-Tropsch process (FT process), and methanation equipment that synthesizes methane.

[0062] The gas production equipment according to the seventh aspect of this disclosure (1A, 1B, 1C, 1D, 1E) is, in any of the first to sixth aspects, an SOEC co-electrolytic apparatus that produces a product gas containing CO from H2O and CO2.

[0063] In the gas production equipment (1A, 1B, 1C, 1D, 1E) according to the eighth aspect of this disclosure, in any of the first to seventh aspects, the synthesis gas production apparatus is a reverse shift reactor, and the reverse shift reactor produces a product gas containing CO by a reverse water-gas shift reaction using CO2 introduced from the absorption liquid regeneration apparatus.

[0064] A gas production facility (1A, 1B, 1C, 1D, 1E) according to the ninth aspect of this disclosure, in any of the first to eighth aspects, includes a boiler power generation device that generates electricity using steam produced using combustion gas and a turbine, and the absorbent liquid absorbs CO2 from exhaust gas discharged from the boiler power generation device.

[0065] The gas production equipment (1A, 1B, 1C, 1D, 1E) according to the tenth aspect of the present disclosure includes, in the ninth aspect, a water electrolysis device that is supplied with electricity from the boiler power generation device to produce H2 from H2O, and the H2 obtained from the water electrolysis device is led to the reverse shift reactor.

[0066] As described above, since the absorbent liquid is heated using the heat contained in the generated gas, it is not necessary to use the steam produced by burning biomass fuel to generate electricity in the biomass boiler power generation device to heat the absorbent liquid, thus reducing the amount of biomass fuel used.

[0067] A gas production method according to a first aspect of this disclosure comprises an absorbent liquid regeneration step of regenerating an absorbent liquid by heating an absorbent liquid on which CO2 has been adsorbed to remove CO2 from the absorbent liquid, and a synthesis gas production step of producing a product gas containing CO by a chemical reaction using the CO2 removed in the absorbent liquid regeneration step, wherein the absorbent liquid regeneration step includes a heating step of heating the absorbent liquid using the heat contained in the product gas produced in the synthesis gas production step.

[0068] 1A, 1B, 1C, 1D, 1E Gas Production Equipment 3 Biomass Boiler Power Generation Equipment (Boiler Power Generation Equipment) 5 Water Electrolyzer 7 CO2 Recovery Equipment 7a Absorption Tower 7b Regeneration Tower (Absorbent Liquid Regeneration Equipment) 7c Heating Section 7d Absorbent Liquid Supply Piping 7e Absorbent Liquid Return Piping 9 Reverse Shift Reactor (Synthesis Gas Production Equipment) 11 FT Synthesis Equipment (Hydrogen Fuel Production Equipment) 13 Hydrogen Supply Piping 15 CO2 Supply Piping 17 Combined Gas Piping 19 Upstream Product Gas Piping (Product Gas Flow Path) 21 Downstream Product Gas Piping 23 First Desuperheater 25 Downstream Product Gas Compressor 27 Second Desuperheater 30 Preheating Section 32 Product Gas Compressor 34 Upstream Gas Compressor 36 Water Pump 38 Water Separator 40 Steam Piping 42 Steam Compressor

Claims

1. A gas production apparatus comprising: an absorbent liquid regeneration device that regenerates an absorbent liquid by heating the absorbent liquid to remove CO2; and a synthesis gas production device that produces a CO-containing product gas by a chemical reaction using CO2 introduced from the absorbent liquid regeneration device, wherein the absorbent liquid regeneration device is equipped with a heating section that heats the absorbent liquid using the heat contained in the product gas produced by the synthesis gas production device.

2. The gas production apparatus according to claim 1, wherein the generated gas flow path between the synthesis gas production apparatus and the heating unit is provided with a preheating unit that preheats the upstream gas introduced into the synthesis gas production apparatus with the generated gas.

3. The gas production apparatus according to claim 1 or 2, further comprising a product gas compressor for pressurizing the product gas discharged from the synthesis gas production apparatus.

4. The gas production apparatus according to claim 1 or 2, further comprising an upstream gas compressor for pressurizing the upstream gas that is introduced into the synthesis gas production apparatus.

5. The gas production apparatus according to claim 1 or 2, comprising a water separator for separating water vapor from the product gas discharged from the synthesis gas production apparatus, wherein the water vapor separated from the water separator is guided to the heating section.

6. The gas production apparatus according to claim 1 or 2, further comprising a hydrocarbon fuel production apparatus to which the generated gas discharged from the synthesis gas production apparatus is introduced for the production of hydrocarbon fuel.

7. The gas production apparatus according to claim 1 or 2, wherein the synthesis gas production apparatus is an SOEC co-electrolytic apparatus that produces a product gas containing CO from H2O and CO2.

8. The gas production apparatus according to claim 1 or 2, wherein the synthesis gas production apparatus is a reverse shift reactor, and the reverse shift reactor produces a product gas containing CO by a reverse water-gas shift reaction using CO2 introduced from the absorption liquid regeneration apparatus.

9. The gas production equipment according to claim 8, comprising a boiler power generation device that generates electricity using steam produced using combustion gas and a turbine, wherein the absorbent liquid absorbs CO2 from exhaust gas discharged from the boiler power generation device.

10. The gas production apparatus according to claim 9, comprising a water electrolysis apparatus that produces H2 from H2O using electricity supplied from the boiler power generation apparatus, wherein the H2 obtained from the water electrolysis apparatus is led to the reverse shift reactor.

11. A gas production method comprising: an absorbent liquid regeneration step of regenerating an absorbent liquid by heating an absorbent liquid that has adsorbed CO2 to remove CO2 from the absorbent liquid; and a synthesis gas production step of producing a product gas containing CO by a chemical reaction using the CO2 removed in the absorbent liquid regeneration step, wherein the absorbent liquid regeneration step includes a heating step of heating the absorbent liquid using the heat contained in the product gas produced in the synthesis gas production step.

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