E-fuel production system equipped with power generation facility

Abstract

This e-fuel production system 1a equipped with a power generation facility comprises: a synthesis gas production device 30 that is supplied with green hydrogen gas and DAC carbon dioxide gas recovered from the atmosphere by direct air capture, and produces a synthesis gas having a molar ratio of hydrogen gas to carbon monoxide gas of approximately 2:1; and an FT synthesis device 40 that generates FT crude oil through an FT synthesis reaction of the synthesis gas. The e-fuel production system 1a is equipped with a power generation facility 50 for driving a steam turbine generator 53 with superheated steam generated by burning, using a boiler 51, light diesel oil and residual oil produced through purification of the FT crude oil, and recovers carbon dioxide gas as recovered carbon dioxide gas from exhaust gas discharged from the power generation facility. The synthesis gas production device is supplied with mixed carbon dioxide gas obtained by mixing the recovered carbon dioxide gas and the DAC carbon dioxide gas, and green hydrogen gas in an amount required to produce the synthesis gas together with the mixed carbon dioxide gas, produces the synthesis gas, and sends the synthesis gas to the FT synthesis device. This makes it possible to produce e-fuel in a carbon-neutral manner, at low cost, and with low energy consumption.

Description

E-fuel production system with power generation facilities

[0001] The present invention relates to an e-fuel production system that produces synthesis gas from direct air capture (DAC) carbon dioxide gas captured from the atmosphere by DAC and green hydrogen gas generated by electrolyzing water using electricity derived from renewable energy, and then subjects the synthesis gas to an FT synthesis reaction to produce FT crude oil.

[0002] Global warming is becoming increasingly serious, and measures to limit the rise in global average temperature by the end of the 21st century to below 2°C, or at least 1.5°C, above pre-industrial levels are becoming an urgent issue. At the G7 summit held in the UK in June 2021, the goal of achieving net carbon neutrality by 2050 was announced. In July of the same year, the European Commission announced a policy to limit passenger cars sold in Europe from 2035 to electric vehicles. However, in March 2023, in order to protect the automotive industry in Germany, Italy, and other countries, the European Commission and the German government agreed to allow the sale of new engine vehicles after 2035 only if they use carbon-neutral synthetic fuel, "e-fuel." E-fuel is a synthetic fuel produced by synthesizing DAC carbon dioxide and green hydrogen gas. DAC carbon dioxide and green hydrogen gas are synthesized using FT synthesis to produce FT crude oil, which is then refined to produce LPG, naphtha, kerosene, diesel, and residual oil.

[0003] E-fuel production requires DAC carbon dioxide, but the concentration of carbon dioxide in the atmosphere is very low at approximately 400 ppm, meaning that approximately 4,000 times the amount of air required must be processed. DAC plants that directly recover carbon dioxide from the atmosphere are costly and energy-intensive, resulting in an extremely high unit price for DAC carbon dioxide. Furthermore, DAC plants and e-fuel production plants require large amounts of electricity, which must be carbon-neutral. Patent Document 1 describes a technology that generates green electricity through biomass power generation, produces carbon-neutral methane gas from the carbon dioxide and low-carbon hydrogen gas produced by the biomass power generation, produces synthesis gas from the carbon-neutral methane gas, synthesizes the synthesis gas into FT crude oil, and utilizes the waste heat generated during the synthesis to recover carbon dioxide.

[0004] Patent No. 7136523

[0005] Patent Document 1 describes a technology for generating synthesis gas from carbon dioxide gas and low-carbon hydrogen gas produced by biomass power generation, and for producing FT crude oil from the synthesis gas, but does not describe the low-cost, low-energy production of e-fuel from DAC carbon dioxide gas and green hydrogen gas.

[0006] The object of the present invention is to provide an e-fuel production system equipped with a power generation facility that drives a steam turbine generator with superheated steam produced by burning in a boiler the diesel and residual oil produced by refining the FT crude oil, in an e-fuel production system that includes a synthesis gas production unit that produces synthesis gas from DAC carbon dioxide gas and green hydrogen gas, and an FT synthesis unit that produces FT crude oil by subjecting the synthesis gas to an FT synthesis reaction.The system is capable of producing carbon-neutral e-fuel at low cost and with low energy consumption.

[0007] The present invention provides an e-fuel production system that includes a synthesis gas production unit that receives DAC carbon dioxide gas recovered from the atmosphere by direct air capture (DAC) and green hydrogen gas generated by electrolyzing water using electricity derived from renewable energy, and produces synthesis gas with a molar ratio of hydrogen gas to carbon monoxide gas of approximately 2:1, and an FT synthesis unit that generates FT crude oil by subjecting the synthesis gas supplied from the synthesis gas production unit to an FT synthesis reaction using a catalyst under a predetermined temperature and pressure environment. The system also includes a power generation facility that receives diesel and residual oil produced by refining the FT crude oil in a refinery as fuel, a boiler that generates superheated steam by burning the fuel, and a steam turbine generator that is driven by the superheated steam. and a carbon dioxide recovery device including an absorption tower to which exhaust gas generated by the combustion of the fuel is supplied from the power generation facility and which generates a CO2-containing absorption liquid by absorbing carbon dioxide contained in the exhaust gas into an absorption liquid, and a regeneration tower to which the CO2-containing absorption liquid is supplied from the absorption tower and which heats the CO2-containing absorption liquid with exhaust heat supplied from the FT synthesis device to release and recover the carbon dioxide as recovered carbon dioxide, and a carbon dioxide mixing device that mixes the recovered carbon dioxide with the DAC carbon dioxide and supplies the resulting mixed carbon dioxide to the synthesis gas production device, wherein the synthesis gas production device is supplied with the mixed carbon dioxide and the amount of green hydrogen gas necessary to produce the synthesis gas from the mixed carbon dioxide.

[0008] According to the present invention, carbon-neutral electricity can be produced by burning diesel and residual oil produced by refining FT crude oil, which is produced from DAC carbon dioxide and green hydrogen gas, in a boiler to generate heated steam, which drives a steam turbine generator. Carbon dioxide is recovered from the exhaust gas discharged from the boiler using the waste heat emitted from the FT synthesis unit, and mixed with DAC carbon dioxide before being supplied to the synthesis gas production unit, thereby reducing the amount of expensive DAC carbon dioxide used. In this way, by organically combining carbon-neutral technologies, e-fuel and carbon-neutral electricity can be produced carbon-neutral in every process of the system, at low cost, and with low energy consumption.

[0009] Fig. 1 is a block diagram showing the overall configuration of an e-fuel production system with an attached power generation facility according to a first embodiment. Fig. 2 is a block diagram showing the overall configuration of an e-fuel production system with an attached power generation facility according to a second embodiment. Fig. 3 is a diagram showing the mass-energy balance of an e-fuel production system with an attached power generation facility according to a second embodiment.

[0010] 1. Configuration of the First Embodiment As shown in FIG. 1 , the e-fuel production system 1a with power generation equipment according to the first embodiment includes a DAC carbon dioxide supply device 10, a green hydrogen supply device 20, a synthesis gas production device 30, an FT synthesis device 40, a power generation facility 50, a heat exchanger 60, a carbon dioxide recovery device 70, and a carbon dioxide mixing device 80.

[0011] The DAC plant 11 is well known and directly recovers carbon dioxide contained in the atmosphere as DAC carbon dioxide using direct air recovery technology. The DAC carbon dioxide supply device 10 supplies the DAC carbon dioxide recovered in the DAC plant 11 at a set flow rate to the synthesis gas production device 30 via a carbon dioxide mixer 80. The green hydrogen production device 21 is well known and produces green hydrogen gas by electrolyzing water using electricity derived from renewable energy. The green hydrogen supply device 20 supplies the green hydrogen gas produced in the green hydrogen production device 21 to the synthesis gas production device 30 at a set flow rate.

[0012] The synthesis gas production apparatus 30 is well known and, as an example, includes a reverse water gas shift reactor 31 filled with a reverse water gas shift catalyst and a mixer 32. The reverse water gas shift reactor 31 receives DAC carbon dioxide from the DAC carbon dioxide supply device 10 and green hydrogen from the green hydrogen supply device 20 at flow rates such that the molar ratio of carbon dioxide to hydrogen is 1:1, and performs a reverse water gas shift reaction according to reaction formula (1) to produce carbon monoxide and water vapor. The mixer 32 receives carbon monoxide, obtained by removing water vapor from the product produced in the reactor 31, and green hydrogen from the green hydrogen supply device 20, and mixes the two gases to deliver synthesis gas with a carbon monoxide to hydrogen molar ratio of 1:2. When only DAC carbon dioxide is supplied from the DAC carbon dioxide supply device 10 to the synthesis gas production apparatus 30, the green hydrogen supply device 20 supplies the synthesis gas production apparatus 30 with the amount of green hydrogen gas required to produce synthesis gas from the DAC carbon dioxide and green hydrogen gas. CO ２ +H ２ =CO+H ２ O (endothermic reaction 439 kcal / Nm ３ -CO ２ ) (1)

[0013] The synthesis gas production device 30 may include a methanation reactor filled with a methanation catalyst, a methane dry reforming reactor filled with a methane dry reforming catalyst, and a mixer. The methanation reactor receives DAC carbon dioxide from the DAC carbon dioxide supply device 10 and green hydrogen from the green hydrogen supply device 20 at flow rates such that the molar ratio of carbon dioxide to hydrogen is 1:4, and undergoes a methanation reaction according to reaction formula (2) to produce methane gas and water vapor. ２ +4H ２ =CH ４ +2H ２In the methane dry reforming reactor, methane gas obtained by removing water vapor from the product produced in the methanation reactor is supplied with DAC carbon dioxide gas from the DAC carbon dioxide gas supply device 10 at a flow rate such that the molar ratio of methane gas to carbon dioxide gas is 1:1, and the methane dry reforming reaction is carried out according to reaction formula (3), producing a mixed gas of carbon monoxide gas and hydrogen gas in a molar ratio of 1:1. ４ +CO ２ = 2CO + 2H ２ (3) The mixer is supplied with mixed gas from the methane dry reforming reactor and green hydrogen gas from the green hydrogen supply device 20 at a volumetric flow rate half that of the mixed gas, and mixes the two gases to deliver synthesis gas with a carbon monoxide to hydrogen molar ratio of 1:2.

[0014] The FT synthesis unit 40 comprises a reactor 41 filled with a catalyst and a cooling pipe 42 arranged within the reactor 41. Synthesis gas is supplied to the reactor 41 from the synthesis gas production unit 30, and the synthesis gas is reacted with the catalyst under a predetermined temperature and pressure environment to synthesize FT crude oil. A heat transfer medium circulation circuit 43 is connected to the cooling pipe 42, through which the heat transfer medium is circulated. The reaction heat generated when the synthesis gas is synthesized into FT crude oil in the FT synthesis unit 40 is transferred to the heat transfer medium in the cooling pipe 42 to maintain the interior of the reactor 41 at a predetermined temperature, and is transported to the heat exchanger 60 and the carbon dioxide recovery unit 70 by the heat transfer medium circulating through the heat transfer medium circulation circuit 43 as exhaust heat discharged from the FT synthesis unit 40.

[0015] The refining unit 45 is well known and receives FT crude oil from the FT synthesis unit 40, distills the FT crude oil into LPG, gasoline, kerosene, diesel, and residual oil components in an atmospheric distillation unit, and then performs the necessary processing to produce final products such as various fuels.

[0016] The power generation facility 50 includes a boiler 51 and a steam turbine generator 53. The boiler 51 burns diesel fuel and residual oil produced by refining FT crude oil in the refining unit 45 as fuel in a combustion chamber 52, and generates superheated steam by heating supplied high-temperature water with the combustion heat. It is preferable to mix a portion of the diesel fuel with the residual oil to generate fuel. The steam turbine generator 53 generates electricity by rotating a condensing turbine 54 with the superheated steam supplied from the boiler 51, which drives a generator 55. A portion of the generated electricity is used as on-site power in the power generation facility-attached e-fuel production system 1a, and surplus electricity is sold to a power grid 59, which is connected to the grid to allow reverse power flow.

[0017] The low-pressure steam, the pressure of which is reduced by rotating the condensing turbine 54, is cooled in the condenser 56 and becomes condensed water. A cooling tower 58 is connected to the cooling pipes 57 of the condenser 56, and cooling water is circulated between the two. The low-pressure steam discharged from the condensing turbine 54 and flowing into the condenser 56 transfers condensation heat to the cooling water flowing through the cooling pipes 57 and becomes condensed water, and the cooling water to which the condensation heat has been transferred releases its condensation heat in the cooling tower 58, is cooled, and is returned to the cooling pipes 57.

[0018] The condensed water sent out from the condenser 56 flows into the heat exchanger 60, where it is heated and returned to the boiler 51. The heat transfer pipes 61 of the heat exchanger 60 are connected to the cooling pipes 42 of the FT synthesis apparatus 40 via the heat medium circulation circuit 43. The reaction heat generated in the FT synthesis apparatus 40 is transferred to the heat transfer pipes 61 by the heat medium circulating through the heat medium circulation circuit 43 as waste heat discharged from the FT synthesis apparatus 40, and the condensed water that flows into the heat exchanger 60 is heated to become high-temperature water.

[0019] The carbon dioxide recovery system 70 receives exhaust gas generated by the combustion of diesel and residual oil from a boiler 51 and recovers carbon dioxide contained in the exhaust gas as recovered carbon dioxide. The carbon dioxide recovery system 70 is well known, as described in, for example, Japanese Patent No. 4956519, and includes an absorption tower 71 that absorbs carbon dioxide contained in the exhaust gas into a regenerated absorbing liquid to produce a CO2-containing absorbing liquid, a regeneration tower 72 that separates carbon dioxide from the CO2-containing absorbing liquid to produce a regenerated absorbing liquid, and a reboiler 73 that heats a portion of the regenerated absorbing liquid to produce high-temperature steam. The absorption tower 71 receives exhaust gas from the combustion chamber 52 of the boiler 51 at its bottom, and receives regenerated absorbing liquid that has been cooled on its way back from the regeneration tower 72 and is supplied from its top. The descending regenerated absorbing liquid absorbs the carbon dioxide contained in the exhaust gas to produce a CO2-containing absorbing liquid, and the exhaust gas from which the carbon dioxide has been recovered is released from its top. The regenerator 72 is supplied from above with the CO2-containing absorbing liquid that has been heated on its way from the absorption tower 71 to the regenerator 72, and the descending CO2-containing absorbing liquid is heated with steam supplied from below to release carbon dioxide, thereby forming a regenerated absorbing liquid. The regenerated absorbing liquid that remains at the bottom of the regenerator 72 is returned to the absorption tower 71. The heat transfer tube 74 of the reboiler 73 is connected to the cooling tube 42 of the FT synthesis unit 40 via the heat medium circulation circuit 43. A portion of the regenerated absorbing liquid supplied from the bottom of the regenerator 72 to the reboiler 73 is heated by exhaust heat from the FT synthesis unit 40 that has been transferred to the heat transfer tube 74 by the heat medium circulating through the heat medium circulation circuit 43, and part of the moisture is converted into steam, which is returned to the regenerator 72.

[0020] The carbon dioxide mixing device 80 is supplied with DAC carbon dioxide from the DAC carbon dioxide supply device 10 and with recovered carbon dioxide from the carbon dioxide recovery device 70, mixes the recovered carbon dioxide with the DAC carbon dioxide, and supplies the resulting mixed carbon dioxide to the synthesis gas production device 30. When mixed carbon dioxide is supplied to the synthesis gas production device 30, the green hydrogen supply device 20 supplies the synthesis gas production device 30 with an amount of green hydrogen gas necessary to produce synthesis gas from the mixed carbon dioxide and green hydrogen gas.

[0021] 2. Operation of the First Embodiment The synthesis gas production apparatus 30 is supplied with mixed carbon dioxide gas from the mixer 80, and is supplied with an amount of green hydrogen gas from the green hydrogen supply apparatus 20 that is necessary to produce synthesis gas from the supplied mixed carbon dioxide gas and green hydrogen gas. The synthesis gas production apparatus 30 produces synthesis gas with a molar ratio of hydrogen gas to carbon monoxide gas of approximately 2:1 and delivers it to the FT synthesis apparatus 40.

[0022] In the FT synthesis unit 40, synthesis gas is supplied from the synthesis gas production unit 30 to a reactor 41 filled with a catalyst, and the synthesis gas is reacted by the catalyst under a predetermined temperature and pressure environment to produce FT crude oil. The reaction heat generated by the catalytic reaction is transferred to a heat medium circulating through a cooling pipe 42, maintaining the inside of the reactor 41 at a predetermined temperature.

[0023] The FT crude oil is supplied to a refinery 45, where it is distilled into LPG, gasoline, kerosene, diesel, and residual oil in an atmospheric distillation unit, and then subjected to the necessary processing to produce the final product. In the first embodiment, a portion of the diesel oil is mixed with the residual oil and supplied as fuel to a boiler 51 of a power generation facility 50. The boiler 51 burns the diesel oil and residual oil supplied from the refinery 45 in a combustion chamber 52, heating high-temperature water supplied from a heat exchanger 60 to generate superheated steam. A condensing turbine 54 driven by the superheated steam operates a generator 55. A portion of the electricity output from the generator 55 is used as on-site power in the power generation facility-attached e-fuel production system 1a, and surplus electricity is sold to a power grid 59. The steam, whose pressure is reduced by rotating the condensing turbine 54, is discharged to a condenser 56, where it transfers latent heat to the cooling water circulating between a cooling pipe 57 and a cooling tower 58, becoming condensed water, which is then sent to a heat exchanger 60. The condensed water that has flowed into the heat exchanger 60 is heated to high temperature water by the exhaust heat from the FT synthesis device 40 that has been transferred to the heat transfer tube 61 via the heat medium circulation circuit 43 , and is returned to the boiler 51 .

[0024] In the carbon dioxide recovery device 70, exhaust gas discharged from the combustion chamber 52 of the boiler 51 is supplied to the absorption tower 71, and the regenerated absorbing liquid absorbs carbon dioxide contained in the exhaust gas to become a CO2-containing absorbing liquid. The CO2-containing absorbing liquid sent to the regenerator 72 is heated by the exhaust heat from the FT synthesis device 40, which is transferred to the heat transfer tube 74 of the reboiler 73 by the heat medium circulating in the heat medium circulation circuit 43, and releases carbon dioxide to become a regenerated absorbing liquid, which is returned to the absorption tower 71. The released carbon dioxide is supplied to the carbon dioxide mixing device 80 as recovered carbon dioxide.

[0025] The carbon dioxide gas mixer 80 mixes recovered carbon dioxide gas supplied from the carbon dioxide gas recovery device 70 with DAC carbon dioxide gas supplied from the DAC carbon dioxide gas supply device 10 , and supplies the resulting mixed carbon dioxide gas to the synthesis gas production device 30 .

[0026] 3. Effects of the First Embodiment According to the first embodiment, in an e-fuel production system that produces carbon-neutral FT crude oil from DAC carbon dioxide gas and green hydrogen gas, diesel and residual oil produced by refining the FT crude oil are combusted in a combustion chamber 52 of a boiler 51 of a power generation facility 50 to generate superheated steam, which can then be used to operate a steam turbine generator 53 to generate green electricity. The reaction heat generated by the FT reaction in the FT synthesis device 40 is transferred as exhaust heat from the FT synthesis device 40 through the heat medium circulation circuit 43 to the heat transfer tubes 61 of the heat exchanger 60, where it heats the condensed water that flows into the heat exchanger 60 from the condenser 57 of the power generation facility 50 to generate high-temperature water, thereby improving thermal efficiency. Furthermore, the exhaust heat emitted from the FT synthesis unit 40 is used to recover carbon dioxide from the exhaust gas discharged from the combustion chamber 52 of the boiler 51 as recovered carbon dioxide, which is then mixed with DAC carbon dioxide and supplied to the synthesis gas production unit, thereby reducing the amount of expensive DAC carbon dioxide used. The recovered carbon dioxide is carbon-neutral because it is generated in the e-fuel production facility 1a attached to the power generation facility, where the only externally supplied raw materials are green hydrogen gas and DAC carbon dioxide. By organically combining carbon-neutral technologies in this way, e-fuel and carbon-neutral electricity can be produced carbon-neutral in every process of the system, at low cost, and with low energy consumption.

[0027] 4. Configuration of the Second Embodiment The e-fuel production system 1b with attached power generation facility according to the second embodiment is the same as the first embodiment except that the exhaust heat emitted from the FT synthesis device 40 in the first embodiment is utilized by the binary power generation facility 90. Therefore, only the differences will be described, and the same components as those in the first embodiment will be assigned the same reference numbers and will not be described again.

[0028] The binary power generation facility 90 generates electricity by driving a generator with a medium turbine rotated by medium vapor. The medium vapor that rotates the medium turbine is condensed in a condenser 91 and then evaporated in an evaporator 93 to become medium vapor. Cooling water is circulated between a cooling pipe 92 of the condenser 91 and a cooling tower 58. A heat transfer pipe 94 of the evaporator 93 is connected to the cooling pipe 42 of the FT synthesis unit 40 via a heat medium circulation circuit 43.

[0029] 5. Operation and Effects of Second Embodiment The reaction heat generated in the FT synthesis apparatus 40 is transferred to the heat transfer tube 94 of the evaporator 93 as exhaust heat discharged from the FT synthesis apparatus 40 by the heat medium circulating through the heat medium circulation circuit 43, and is condensed in the condenser 91 to heat the medium that flows into the evaporator 93 and become medium vapor. The medium vapor rotates a medium turbine to drive a generator and generate carbon-neutral electricity. The medium vapor that rotates the medium turbine flows into the condenser 91, transfers latent heat to the cooling water circulating through the cooling tube 92, and is condensed and sent to the evaporator 93.

[0030] In the second embodiment, the exhaust heat emitted from the FT synthesis device 40 is used to operate the binary power generation equipment 90 to generate electricity, so in addition to the effects of the first embodiment, more carbon-neutral electricity can be produced with low energy consumption.

[0031] In the above embodiment, the steam turbine of the steam turbine generator 53 is the condensing turbine 54, but it may be a back-pressure turbine. If a back-pressure turbine is used, the condenser 57 becomes unnecessary, and the condensed water sent out from the condenser 57 does not need to be heated to high-temperature water by the exhaust heat discharged from the FT synthesis device 40.

[0032] Next, an example of the mass-energy balance study of the second embodiment shown in Figure 3 will be described. A. Assumed conditions 1. The synthesis gas production method is the reverse water-gas shift reaction method, and the efficiency is 100%. 2. The carbon dioxide recovery rate in the carbon dioxide recovery unit 70 is 100%. 3. The power generation efficiency of the condensing steam turbine generator 53 is 35%, and the power generation efficiency of the binary power generation facility 90 is 8%. 4. The carbon dioxide emission coefficient of the residual oil is 1.5 Nm ３ -CO2 / kg-residual oil. 5. The endothermic reaction heat in the synthesis gas production unit 30 is 439 kcal / Nm ３ -CO ２ The exothermic reaction heat in the FT synthesis apparatus 40 is 1789 kcal / Nm ３ -CO. B. Effects of e-fuel production system with power generation facility When DAC carbon dioxide gas is supplied to the carbon dioxide gas mixer 80 at a flow rate of 20,625 Nm3 / h and recovered carbon dioxide gas is supplied to the carbon dioxide gas mixer 80 at a flow rate of 9.375 Nm3 / h, and green hydrogen is supplied to the synthesis gas production unit 30 at a flow rate of 90,000 Nm3 / h, the flow rates of the products sent from each unit are as shown in Figure 3, and the products of the e-fuel production system with power generation facility are as follows. 1. e-fuel yield is 345 kL / day 2. Carbon-neutral electricity is approximately 36,000 kW

[0033] 1a-1b: e-fuel production system with attached power generation facility, 10: DAC carbon dioxide supply device, 11: DAC plant, 20: green hydrogen supply device, 21: green hydrogen production device, 30: synthesis gas production device, 40: FT synthesis device, 42: cooling pipe, 43: heat medium circulation circuit, 45: purification device, 50: power generation device, 51: boiler, 52: heat transfer tube, 53: steam turbine generator, 54: condensing turbine, 55: generator, 56: condenser, 57: cooling pipe, 58: cooling tower, 60: heat exchanger, 61: heat transfer tube, 70: carbon dioxide recovery device, 71: absorption tower, 72: regeneration tower, 73: reboiler, 80: carbon dioxide mixing device, 90: binary power generation facility, 91: condenser, 92: cooling pipe, 93: evaporator, 94: heat transfer tube.

Claims

1. An e-fuel production system comprising a synthesis gas production unit which receives DAC carbon dioxide gas captured from the atmosphere by direct air capture (DAC) and green hydrogen gas produced by electrolyzing water using electricity derived from renewable energy sources, and produces synthesis gas with a molar ratio of hydrogen gas to carbon monoxide gas of approximately 2:1, and an FT synthesis unit which produces FT crude oil by subjecting the synthesis gas supplied from the synthesis gas production unit to an FT synthesis reaction using a catalyst under a predetermined temperature and pressure environment, the system comprising: a power generation facility which receives diesel and residual oil produced by refining the FT crude oil in a refining unit as fuel, a boiler which produces superheated steam by burning the fuel, and a steam turbine generator which is driven by the superheated steam; an absorption tower to which exhaust gas generated by combustion of the fuel from the boiler is supplied, and carbon dioxide gas contained in the exhaust gas is absorbed into an absorption liquid to produce a CO2-containing absorption liquid, and a regeneration tower to which the CO2-containing absorption liquid is supplied from the absorption tower, and which heats the CO2-containing absorption liquid with exhaust heat supplied from the FT synthesis apparatus, releases the carbon dioxide gas, and recovers it as recovered carbon dioxide gas; and a carbon dioxide mixing device that mixes the recovered carbon dioxide gas with the DAC carbon dioxide gas, and supplies the mixed carbon dioxide gas to the synthesis gas production apparatus, wherein the synthesis gas production apparatus is supplied with the mixed carbon dioxide gas and the green hydrogen gas in an amount necessary for producing the synthesis gas from the mixed carbon dioxide gas.

2. The e-fuel production system with power generation facility described in claim 1, wherein the steam turbine of the steam turbine generator is a condensing turbine, low-pressure steam discharged from the condensing turbine is condensed into condensed water in a condenser, and the condensed water is heated by exhaust heat discharged from the FT synthesis device and then supplied to the boiler to generate the superheated steam.

3. The e-fuel production system with power generation facility according to claim 1 or 2, wherein exhaust heat discharged from the FT synthesis device is utilized in a binary power generation facility.

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