Fuel manufacturing apparatus and fuel manufacturing method

Abstract

This fuel production apparatus 1 is provided with: a synthetic gas production unit for producing a synthetic gas comprising carbon monoxide and hydrogen using carbon dioxide and hydrogen; a hydrocarbon production unit for producing a hydrocarbon using the synthetic gas; a first distillation separation unit 28 for separating at least a first fraction and a second fraction that is lighter than the first fraction from a product flowing away from the hydrocarbon production unit; a hydrocracking unit 32 for subjecting a portion of the first fraction to a hydrocracking treatment; and a catalytic cracking unit 34 for subjecting another portion of the first fraction to a catalytic cracking treatment.

Description

[Technical Field]

[0001] The present invention relates to a fuel production apparatus and a fuel production method. [Background technology]

[0002] A technology for producing liquid fuels using GTL (Gas to Liquid) is known (see Patent Document 1). This technology includes, as an example, a step of producing hydrogen and carbon monoxide from natural gas, and a step of producing high-energy-density liquid hydrocarbons by a Fischer-Tropsch reaction (hereinafter referred to as "FT reaction") using synthesis gas containing hydrogen and carbon monoxide as raw materials. [Prior art documents] [Patent Documents]

[0003] [Patent Document 1] Japanese Patent Publication No. 2008-248179 [Overview of the project] [Problems that the invention aims to solve]

[0004] As a result of diligent research, the inventors have come up with a new technology for producing various fuels from the products of the FT reaction.

[0005] This invention has been made in view of these circumstances, and one of its objectives is to provide a technology for producing various fuels from the products of the FT reaction. [Means for solving the problem]

[0006] One aspect of the present invention is a fuel production apparatus. This apparatus comprises a synthesis gas production unit that produces synthesis gas containing carbon monoxide and hydrogen using carbon dioxide and hydrogen; a hydrocarbon production unit that produces hydrocarbons using the synthesis gas; a first distillation separation unit that separates at least a first fraction and a second fraction that is lighter than the first fraction from the effluent from the hydrocarbon production unit; a hydrocracking unit that subjects a portion of the first fraction to hydrocracking treatment; and a catalytic cracking unit that subjects another portion of the first fraction to catalytic cracking treatment.

[0007] Another aspect of the present invention is a fuel production method. This method includes a synthesis gas production step of producing synthesis gas containing carbon monoxide and hydrogen using carbon dioxide and hydrogen; a hydrocarbon production step of producing hydrocarbons using synthesis gas; a first distillation separation step of separating at least a first fraction and a second fraction lighter than the first fraction from the effluent from the hydrocarbon production step; a hydrocracking step of subjecting a portion of the first fraction to hydrocracking treatment; and a catalytic cracking step of subjecting the other portion of the first fraction to catalytic cracking treatment.

[0008] Any combination of the above components, as well as any conversion of the expressions of this disclosure between methods, apparatus, systems, etc., are also valid forms of this disclosure. [Effects of the Invention]

[0009] According to the present invention, various fuels can be produced from the products of the FT reaction. [Brief explanation of the drawing]

[0010] [Figure 1] This is a schematic diagram of a fuel manufacturing apparatus according to an embodiment. [Figure 2] This is a schematic diagram of a fuel manufacturing apparatus according to an embodiment. [Figure 3] Figures 3(A), 3(B), and 3(C) show examples of reactions occurring in the hydrogenation purification section. Figure 3(D) shows an example of a reaction occurring in the hydrocracking section. Figures 3(E), 3(F), and 3(G) show examples of reactions occurring in the catalytic cracking section. [Figure 4]This is a schematic diagram of a fuel manufacturing apparatus according to the first modified example. [Figure 5] This is a schematic diagram of a fuel manufacturing apparatus according to modified example 2. [Figure 6] This is a schematic diagram of a fuel manufacturing apparatus relating to the third modified example. [Figure 7] This is a schematic diagram of a fuel manufacturing apparatus relating to Modification 4. [Modes for carrying out the invention]

[0011] The present invention will be described below with reference to the drawings, based on preferred embodiments. The embodiments are illustrative and not limit the technical scope of the present invention, and not all features or combinations thereof described in the embodiments are necessarily essential to the invention. Therefore, the content of the embodiments can be modified in many ways, such as changing, adding, or deleting components, as long as it does not depart from the spirit of the invention as defined in the claims. A new embodiment with modified designs will have the combined effects of both the embodiments and the variations. In the embodiments, such modifications are emphasized with notations such as "of this embodiment" or "in this embodiment," but modifications are also permitted for content without such notations. Any combination of components described in the embodiments is also valid as an aspect of the present invention. The same or equivalent components, members, and processes shown in each drawing are denoted by the same reference numerals, and redundant explanations are omitted as appropriate. Furthermore, the scale and shape of each part shown in each drawing are set for convenience to facilitate explanation and are not to be interpreted restrictively unless specifically mentioned. Furthermore, where terms such as "first," "second," etc., are used in this specification or claims, these terms do not indicate any order or importance, but are used to distinguish one configuration from another. In addition, some components that are not important for describing the embodiments are omitted from the drawings.

[0012] FIG. 1 and FIG. 2 are schematic diagrams of a fuel production apparatus 1 according to an embodiment. The fuel production apparatus 1 includes a synthesis gas production unit 2, a hydrocarbon production unit 4, a first separation unit 6, a second separation unit 8, a third separation unit 20, a fifth separation unit 22, a reforming unit 14, a first distillation separation unit 28, a hydrogenation purification unit 30, a hydrocracking unit 32, a catalytic cracking unit 34, a second distillation separation unit 36, and a third distillation separation unit 38.

[0013] The synthesis gas production unit 2 is disposed upstream of the hydrocarbon production unit 4. A second separation unit 8 is disposed between the synthesis gas production unit 2 and the hydrocarbon production unit 4. A first separation unit 6 is disposed downstream of the hydrocarbon production unit 4. A third separation unit 20, a fifth separation unit 22, and a reforming unit 14 are disposed between the first separation unit 6 and the synthesis gas production unit 2. Further, the third separation unit 20 is connected to the hydrocarbon production unit 4, and the fifth separation unit 22 is connected to the second separation unit 8.

[0014] A first distillation separation unit 28 is disposed downstream of the first separation unit 6 with an oil-water separator 24 interposed therebetween. A hydrogenation purification unit 30, a hydrocracking unit 32, and a catalytic cracking unit 34 are connected to the first distillation separation unit 28. The hydrogenation purification unit 30, the hydrocracking unit 32, and the catalytic cracking unit 34 are connected to the first distillation separation unit 28 in parallel with each other. Further, the hydrogenation purification unit 30 and the hydrocracking unit 32 are connected to the second distillation separation unit 36. The catalytic cracking unit 34 is connected to the third distillation separation unit 38. Note that the physical arrangement of each unit can be set as appropriate. For example, the first separation unit 6 and the hydrocarbon production unit 4 may be disposed in the same housing. Further, for example, "a second separation unit 8 is disposed between the synthesis gas production unit 2 and the hydrocarbon production unit 4" does not mean that the second separation unit 8 is disposed in the space sandwiched between the synthesis gas production unit 2 and the hydrocarbon production unit 4, but means that the second separation unit 8 is present in the middle of the flow of substances from the synthesis gas production unit 2 to the hydrocarbon production unit 4. Of course, the second separation unit 8 may be disposed in the space sandwiched between the synthesis gas production unit 2 and the hydrocarbon production unit 4.

[0015] The synthesis gas production unit 2 receives supplies of carbon dioxide and hydrogen as raw materials gases. Then, using the carbon dioxide and hydrogen, it produces synthesis gas containing carbon monoxide and hydrogen. The synthesis gas production unit 2 receives a supply of hydrogen from the water electrolysis module 12 as an example. Note that the water electrolysis module 12 may be provided as an external device with respect to the fuel production apparatus 1, or may be incorporated inside the fuel production apparatus 1.

[0016] The water electrolysis module 12 is an electrolytic cell that generates hydrogen and oxygen by electrolyzing water. As an example, the water electrolysis module 12 has a structure in which an oxygen generation electrode having a catalyst such as iridium or platinum and a hydrogen generation electrode having a catalyst such as platinum are separated by a proton-conductive diaphragm. That is, the water electrolysis module 12 is a solid polymer type water electrolysis module. Note that other examples of the water electrolysis module 12 include an alkaline type water electrolysis module and a solid oxide type water electrolysis module. The reactions during the electrolysis of water in the solid polymer type water electrolysis module are as shown in the following formulas (1) and (2). Reaction occurring at the oxygen generation electrode: 2H2O → O2 + 4H + 4e - (1) Reaction occurring at the hydrogen generation electrode: 4H + + 4e - → 2H2 (2)

[0017] The water electrolysis module 12 receives a supply of the power necessary for water electrolysis from a power supply device not shown. Examples of the power supply device include power generation devices that generate electricity using renewable energy, such as wind power generation devices and solar power generation devices. Thereby, it is possible to reduce the amount of carbon dioxide emissions associated with the production of hydrogen, and thus the production of various fuels that are the target products. Note that the power supply device is not limited to a power generation device that uses renewable energy, and may be a grid power supply, or may be a power storage device that stores power from a renewable energy power generation device or a grid power supply, or the like. Also, combinations of two or more of these may be used.

[0018] The carbon dioxide supplied to the synthesis gas production unit 2 can, for example, be carbon dioxide recovered directly from the atmosphere by air capture (DAC). Alternatively, carbon dioxide can be separated and recovered from combustion exhaust gases emitted from thermal power plants, chemical plants, etc., by methods such as chemical absorption or physical absorption. This is expected to reduce carbon dioxide in the atmosphere and reduce the consumption of fossil fuels.

[0019] In the synthesis gas production unit 2, the reverse shift reaction shown in equation (3) below occurs, producing synthesis gas containing at least carbon monoxide and hydrogen. Therefore, the synthesis gas production unit 2 can also be considered as a reverse shift reaction unit. The heat required for the reverse shift reaction is supplied, for example, from an external source. In addition, as shown in equation (4) below, some carbon monoxide may react with hydrogen to produce methane and water. Therefore, in addition to hydrogen and carbon monoxide, the synthesis gas may also contain methane. Furthermore, the synthesis gas may also contain unreacted carbon dioxide. CO2 + H2 ⇔ CO + H2O (3) CO + 3H2 ⇔ CH4 + H2O (4)

[0020] The synthesis gas discharged from the synthesis gas production unit 2 is sent to the second separation unit 8. The water discharged from the synthesis gas production unit 2 may be separated from the synthesis gas and supplied to, for example, a water electrolysis module 12. The second separation unit 8 separates carbon dioxide from the synthesis gas. A known carbon dioxide separator can be used in the second separation unit 8. The carbon dioxide separated in the second separation unit 8 is supplied to the synthesis gas production unit 2. The synthesis gas production unit 2 receives the carbon dioxide separated by the second separation unit 8 and uses this carbon dioxide in the production of synthesis gas. This improves the utilization rate of carbon dioxide. Therefore, the efficiency of fuel production can be improved.

[0021] The synthesis gas from which carbon dioxide has been separated in the second separation unit 8 is sent to the hydrocarbon production unit 4. The H2 / CO ratio of the synthesis gas supplied to the hydrocarbon production unit 4 is, for example, 1.80 to 2.30, preferably 1.90 to 2.20, and more preferably 2.00 to 2.10. The hydrocarbon production unit 4 uses the supplied synthesis gas to produce hydrocarbons having 5 or more carbon atoms (hereinafter referred to as "C5+ components" as appropriate). The C5+ components are, for example, normal paraffins having 5 or more carbon atoms. The hydrocarbon production unit 4 can also produce olefins, alcohols, and the like.

[0022] The hydrocarbon production unit 4 of this embodiment is composed of a known FT reactor. As the FT reactor, a tubular fixed-bed reactor, a slurry-bed reactor, etc., can be used. In the hydrocarbon production unit 4, the FT reaction shown in the following formula (5) occurs, and C5+ components are produced by carbon-carbon chain growth. As the catalyst for the FT reaction, a cobalt catalyst, a precipitated iron catalyst, a ruthenium catalyst, etc., can be used. The reaction temperature of the hydrocarbon production unit 4 is, for example, 200°C to 250°C. The rate at which a reaction intermediate with n carbon atoms is degraded into a reaction intermediate with n+1 carbon atoms by carbon-carbon chain growth is expressed by the chain growth probability α. A higher α means that a higher molecular weight hydrocarbon can be obtained. α varies depending on the type of catalyst and reaction conditions, and is preferably 0.75 to 0.95, and more preferably 0.85 to 0.95. In formula (5), for example, when α is 0.95, n of the C5+ components contained in 0.1 mol% or more is, for example, an integer from 5 to 60. In addition, the hydrocarbon production unit 4 also produces by-products such as methane, ethane, propane, and butane, which are gaseous at room temperature and pressure and have four or fewer carbon atoms (hereinafter referred to as "C4-components" as appropriate). nCO + (2n+1)H2 → C n H 2n+2 +nH2O (5)

[0023] The effluent from the hydrocarbon production unit 4 is sent to the first separation unit 6. This effluent may contain not only C5+ and C4- components, but also other by-products such as water, as well as unreacted hydrogen, carbon monoxide, and carbon dioxide. The first separation unit 6 can be configured with a known gas-liquid separator and separates the effluent into liquid and gaseous components. The liquid component contains C5+ components and water. The gaseous component contains hydrogen, carbon monoxide, carbon dioxide, and C4- components. Note that the gaseous component may also contain gaseous C5+ components. The liquid component is separated of water by a known oil-water separator 24. The liquid component from which water has been separated by the oil-water separator 24 is sent to the first distillation separation unit 28. The separated water may be supplied to, for example, a water electrolysis module 12. The flow from the first distillation separation unit 28 onward will be described in detail later.

[0024] The gaseous component is used as recycled gas. In this embodiment, a portion of the recycled gas is returned directly from the first separation unit 6 to the hydrocarbon production unit 4. The hydrocarbon production unit 4 receives a portion of the recycled gas from the first separation unit 6 and uses this recycled gas in the production of the C5+ component. The carbon monoxide conversion rate for one reaction in the hydrocarbon production unit 4, that is, when synthesis gas is passed through the hydrocarbon production unit 4 once, is approximately 50-60% as an example. By returning a portion of the recycled gas from the first separation unit 6 to the hydrocarbon production unit 4, this conversion rate can be increased to, for example, approximately 80-99%, 85-97%, or 90-95%. Furthermore, by returning a portion of the recycled gas directly from the first separation unit 6 to the hydrocarbon production unit 4, the load on the third separation unit 20 and the fifth separation unit 22 can be reduced, thereby suppressing an increase in the equipment size of these separation units. In addition, an increase in the equipment size of the synthesis gas production unit 2, the second separation unit 8, the reforming unit 14, etc., to which the separated recycled gas is supplied can be suppressed. Therefore, the process efficiency in the fuel production apparatus 1 can be improved.

[0025] The remaining recycled gas flowing out of the first separation unit 6 is sent to the third separation unit 20, which is located between the first separation unit 6 and the synthesis gas production unit 2. The third separation unit 20 separates carbon monoxide from the recycled gas. The third separation unit 20 can use a known separator that separates carbon monoxide, for example, by the pressure fluctuation adsorption (PSA) method. The carbon monoxide separated in the third separation unit 20 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this carbon monoxide in the production of C5+ components. This improves the utilization rate of carbon monoxide and improves the production efficiency of C5+ components. Furthermore, the separation of carbon monoxide in the third separation unit 20 reduces the load on the fifth separation unit 22, thereby suppressing an increase in the equipment size of the fifth separation unit 22. In addition, it is possible to suppress an increase in the equipment size of the synthesis gas production unit 2, the second separation unit 8, the reforming unit 14, etc., to which the separated recycled gas is supplied. Thus, the process efficiency of the fuel production apparatus 1 can be improved.

[0026] The recycled gas from which carbon monoxide has been separated in the third separation unit 20 is sent to the fifth separation unit 22, which is located between the third separation unit 20 and the synthesis gas production unit 2. The fifth separation unit 22 separates hydrogen and carbon dioxide from the recycled gas supplied from the third separation unit 20. The fifth separation unit 22 can use a known separator that separates hydrogen and carbon dioxide, for example, by membrane separation. As an example, the fifth separation unit 22 has at least one of a polyimide membrane, a carbon membrane obtained by carbonizing the polyimide membrane, and a metal membrane containing Pd. The hydrogen and carbon dioxide separated in the fifth separation unit 22 are supplied to the second separation unit 8. This improves the utilization rate of hydrogen and carbon dioxide and improves the production efficiency of the C5+ component. In addition, the separation of hydrogen and carbon dioxide in the fifth separation unit 22 reduces the load on the reforming unit 14 and suppresses an increase in the size of the equipment. Therefore, the process efficiency of the fuel production apparatus 1 can be improved.

[0027] The second separation unit 8 separates the hydrogen and carbon dioxide supplied from the fifth separation unit 22 into hydrogen and carbon dioxide. The hydrogen separated by the second separation unit 8 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses the hydrogen in the production of C5+ components. Thereby, the utilization rate of hydrogen is improved, and the production efficiency of C5+ components is improved. The carbon dioxide separated by the second separation unit 8 is supplied to the synthesis gas production unit 2. The synthesis gas production unit 2 also uses the carbon dioxide in the production of synthesis gas. Thereby, the utilization rate of carbon dioxide is improved, and the production efficiency of C5+ components is improved.

[0028] The recycled gas from which hydrogen and carbon dioxide have been separated by the fifth separation unit 22 is sent to the reforming unit 14 provided between the fifth separation unit 22 and the synthesis gas production unit 2. For the reforming unit 14, a known reformer capable of reforming C4- components into methane can be used. For example, a steam reformer can be used for the reforming unit 14. The water required for the reaction in the reforming unit 14 is supplied from the outside, for example. Also, the water generated in the synthesis gas production unit 2 or the hydrocarbon production unit 4 may be recycled and supplied to the reforming unit 14. The reaction temperature of the reforming unit 14 is, for example, 450°C to 600°C, preferably 450°C to 500°C. By treating the C4- components at 450°C to 600°C, the precipitation of carbon (coke) can be suppressed. Thereby, the possibility of catalyst deterioration and blockage of the reaction apparatus in the reforming unit 14 can be reduced.

[0029] In the reforming unit 14, the reactions shown in the following formulas (6), (7) and (8) occur, and the C4- components (denoted as C n H m in formula (6)) contained in the recycled gas are reformed into methane, hydrogen, carbon monoxide and carbon dioxide. In formula (6), n is an integer from 1 to 4, and m is an integer from 4 to 10. By providing the reforming unit 14, the possibility of catalyst deterioration and blockage of the reaction apparatus in the synthesis gas production unit 2 can be reduced. C n H m +nH2O→nCO+(n+m / 2)H2(6) CO+3H2⇔CH4+H2O (7) CO + H2O ⇔ CO2 + H2 (8)

[0030] The recycled gas containing methane, hydrogen, carbon monoxide, and carbon dioxide produced in the reforming unit 14 is sent to the synthesis gas production unit 2. The synthesis gas production unit 2 receives this recycled gas and uses the methane, hydrogen, carbon monoxide, and carbon dioxide contained in the recycled gas to produce synthesis gas. This improves the utilization rate of the C4- component and the production efficiency of the C5+ component. Furthermore, when the reaction temperature of the synthesis gas production unit 2 is set to 700°C or higher, preferably 800°C or higher, and more preferably 1000°C or higher, synthesis gas can be efficiently produced from methane and water by the reverse reaction of the reaction shown in formula (4) above. This improves the utilization rate of the C4- component and the production efficiency of the C5+ component.

[0031] The reforming unit 14 may be supplied with the C4- components separated in the first distillation separation unit 28, the second distillation separation unit 36, and / or the third distillation separation unit 38. The reforming unit 14 also reforms these C4- components into methane, hydrogen, carbon monoxide, and carbon dioxide. This improves the utilization rate of the C4- components and increases the production efficiency of the C5+ components. The C4- components discharged from each distillation separation unit may be supplied to the reforming unit 14 after being combined, or they may be supplied to the reforming unit 14 independently of each other.

[0032] Either supplying the recycled gas separated in the first separation unit 6 to the synthesis gas production unit 2 and using the recycled gas for synthesis gas production, or supplying the recycled gas to the hydrocarbon production unit 4 and using the recycled gas for hydrocarbon production, may be carried out by only one of these methods.

[0033] Next, the flow from the first distillation separation unit 28 onward will be described. The first distillation separation unit 28 is supplied with the effluent from the hydrocarbon production unit 4, more specifically, the effluent from which the recycled gas has been separated in the first separation unit 6. In this embodiment, the effluent (liquid component containing C5+ components) from which the recycled gas has been separated in the first separation unit 6 and the water has been separated in the oil-water separator 24 is sent to the first distillation separation unit 28. The first distillation separation unit 28 separates at least a first fraction and a second fraction from the effluent. The second fraction is a lighter fraction than the first fraction. The first distillation separation unit 28 can be configured with a known distillation apparatus.

[0034] The first fraction of this embodiment includes a wax fraction. The second fraction includes a naphtha fraction and an intermediate fraction. The first distillation separation unit 28 of this embodiment also separates the naphtha fraction and the intermediate fraction contained in the second fraction. The naphtha fraction includes, for example, liquid hydrocarbons with a boiling point of 150°C or less (e.g., 5 to 9 carbon atoms). The intermediate fraction includes, for example, hydrocarbons with a boiling point greater than 150°C to 360°C (10 to 21 carbon atoms). The wax fraction includes, for example, hydrocarbons with a boiling point greater than 360°C (22 or more carbon atoms). Note that each fraction may also contain hydrocarbons mainly contained in other fractions. Furthermore, the first distillation separation unit 28 also separates C4- components that could not be separated from the effluent by the first separation unit 6. These C4- components are supplied to the reforming unit 14 as needed.

[0035] The second fraction separated in the first distillation separation unit 28 is sent to the hydrogenation purification unit 30. The hydrogenation purification unit 30 receives hydrogen from an external source and performs a hydrogenation purification treatment on the second fraction. This hydrogen may be supplied from the water electrolysis module 12. The hydrogenation purification unit 30 can be configured with a known hydrogenation apparatus. Figures 3(A), 3(B), and 3(C) show an example of a reaction occurring in the hydrogenation purification unit 30. Examples of catalysts used in the hydrogenation purification unit 30 include metals with hydrogenating ability, such as iridium, nickel, platinum, and palladium, supported on a metal oxide or other carrier. Through the hydrogenation purification treatment in the hydrogenation purification unit 30, as shown in Figure 3(A), the olefin in the second fraction is converted to paraffin. Also, as shown in Figure 3(B), the alcohol in the second fraction is converted to paraffin. These changes improve the oxidation stability of the second fraction. Furthermore, as shown in Figure 3(C), n-paraffins in the second fraction are converted to i-paraffins. This improves the low-temperature fluidity of the second fraction. The second fraction, which has undergone hydrogenation purification in the hydrogenation purification unit 30, is sent to the second distillation separation unit 36.

[0036] A portion of the first fraction separated in the first distillation separation unit 28 is sent to the hydrocracking unit 32. The hydrocracking unit 32 receives hydrogen from an external source and performs hydrocracking treatment on the first fraction. The hydrogen may be supplied from the water electrolysis module 12. The hydrocracking unit 32 can be configured with a known hydrocracking apparatus. Figure 3(D) shows an example of a reaction occurring in the hydrocracking unit 32. Examples of catalysts used in the hydrocracking unit 32 include a combination of a metal with hydrogenation ability such as iridium, nickel, platinum, and palladium, and a solid acid catalyst with decomposition ability such as silica-alumina or zeolite. The metal with hydrogenation ability may be supported on a carrier such as a solid acid catalyst with decomposition ability (first embodiment), or on a carrier such as a metal oxide that does not have decomposition ability (second embodiment). Furthermore, the catalyst used in the hydrocracking unit 32 may be a solid acid catalyst that does not support a metal (third embodiment). The first embodiment can be used alone. The second and third embodiments are used in combination with other embodiments. When two or more catalysts are used, the two or more catalysts may be physically mixed or layered. As shown in Figure 3(D), the long-chain paraffins are decomposed by the hydrocracking treatment in the hydrocracking section 32. This lightens the first fraction. Also, similar to the hydropurification treatment in the hydropurification section 30, olefins and alcohols in the first fraction are converted to paraffins. In addition, n-paraffins in the first fraction are converted to i-paraffins. This improves the oxidation stability and low-temperature fluidity of the first fraction. The first fraction that has undergone hydrocracking treatment in the hydrocracking section 32 is sent to the second distillation separation section 36.

[0037] Furthermore, the second fraction subjected to hydrogenation purification in the hydrogenation purification unit 30 and the first fraction subjected to hydrocracking in the hydrocracking unit 32 may be sent to separate distillation separation units. For example, the second fraction subjected to hydrogenation purification in the hydrogenation purification unit 30 may be sent to the second distillation separation unit 36, and the first fraction subjected to hydrocracking in the hydrocracking unit 32 may be sent to a fourth distillation separation unit (not shown) separate from the second distillation separation unit 36 ​​and the third distillation separation unit 38.

[0038] The second distillation separation unit 36 ​​receives the second fraction, which has been subjected to hydrorefining treatment in the hydrorefining unit 30, and the first fraction, which has been subjected to hydrocracking treatment in the hydrocracking unit 32, and distills the second and first fractions. The second distillation separation unit 36 ​​can be configured with a known distillation apparatus. The second distillation separation unit 36 ​​separates at least one component selected from the group consisting of C4-, naphtha fraction, kerosene fraction (kerosene, jet fuel), diesel fuel fraction, and a fraction heavier than diesel fuel. In this embodiment, as an example, all of the C4- component, naphtha fraction, kerosene fraction, diesel fuel fraction, and the fraction heavier than diesel fuel are separated. This yields kerosene or diesel fuel as fuel. The C4- component is supplied to the reforming unit 14 as needed. Some or all of the fraction heavier than diesel fuel is returned to the hydrocracking unit 32 as needed. The hydrocracking unit 32 receives a supply of some or all of the heavier fractions than diesel fuel and subjects these fractions to hydrocracking treatment.

[0039] A portion of the first fraction separated in the first distillation separation section 28 is sent to the catalytic cracking section 34. For example, all of the first fraction, excluding the portion sent to the hydrocracking section 32, is sent to the catalytic cracking section 34. The catalytic cracking section 34 performs catalytic cracking on the first fraction. The catalytic cracking section 34 can be configured with a known catalytic cracking apparatus. As an example, the catalytic cracking section 34 is configured with a fluidized bed catalytic cracking apparatus (FCC), but it is not limited to this configuration and may also be a fixed bed type, etc. Figures 3(E), 3(F), and 3(G) show examples of reactions occurring in the catalytic cracking section 34. As shown in Figure 3(E), the catalytic cracking treatment in the catalytic cracking section 34 decomposes long-chain paraffins and produces olefins. Also, as shown in Figure 3(F), hydrogen is transferred between hydrocarbon molecules, producing, for example, aromatic compounds. Note that compounds other than aromatic compounds may also be produced by hydrogen transfer between hydrocarbon molecules, which is not limited to cyclic hydrocarbons. Furthermore, as shown in Figure 3(G), similar to the hydrogenation purification process in the hydrogenation purification section 30, n-paraffins in the first fraction are converted to i-paraffins. As a result, the first fraction after catalytic cracking contains a large amount of olefins and aromatic compounds. Note that the chemical formulas shown in Figures 3(A) to 3(G) are examples and are not limited to the structures described. Also, R1 to R in Figures 3(A) to 3(G) 14 These are hydrocarbon groups that may have substituents on their side chains, and each of them may be the same or different from the others.

[0040] The first fraction, which has undergone catalytic cracking in the catalytic cracking section 34, is sent to the third distillation separation section 38. Note that coke may be generated during the catalytic cracking process. This coke is discharged from the catalytic cracking section 34. One example of a method for discharging the coke is to supply oxygen to the catalytic cracking section 34 to burn the coke and discharge it as carbon dioxide or carbon monoxide. The third distillation separation section 38 receives the first fraction, which has undergone catalytic cracking in the catalytic cracking section 34, and distills the first fraction. The third distillation separation section 38 can be configured using a known distillation apparatus. The third distillation separation section 38 separates at least one component selected from the group consisting of C4-, gasoline fraction, light cycle oil (LCO), and heavy clarified oil (CLO). In this embodiment, as an example, all of the C4-, gasoline fraction, light cycle oil, and clarified oil are separated. This yields gasoline or heavy oil as fuel. The C4 component is supplied to the reforming section 14 as needed. Some or all of the CLO is returned to the catalytic cracking section 34 as needed. The catalytic cracking section 34 receives some or all of the clarified oil and also subjects the clarified oil to catalytic cracking treatment. LCO can be used, for example, as a heavy oil base or a light oil base. CLO can be used, for example, as a heavy oil base.

[0041] As described above, the fuel production apparatus 1 of this embodiment distributes the first fraction separated in the first distillation separation unit 28 to the hydrocracking unit 32 and the catalytic cracking unit 34. Then, kerosene fractions, light oil fractions, etc. are separated from the first fraction that has undergone hydrocracking treatment in the hydrocracking unit 32, and gasoline fractions, heavy oil fractions, etc. are separated from the first fraction that has undergone catalytic cracking treatment in the catalytic cracking unit 34. As a result, various fuels such as kerosene, light oil, gasoline, and heavy oil can be efficiently produced from the products of the FT reaction. In particular, by providing the catalytic cracking unit 34, it is possible to produce more high-octane olefins and aromatic compounds suitable for gasoline compared to the case where only the hydrocracking unit 32 is provided. Therefore, the gasoline yield can be increased. Furthermore, the yield of various fuels can be easily adjusted by adjusting the distribution ratio of the first fraction to the hydrocracking unit 32 and the catalytic cracking unit 34.

[0042] Furthermore, the fuel production apparatus 1 supplies the second fraction to the hydrorefining unit 30, where it separates the kerosene fraction and the light oil fraction from the second fraction after hydrorefining treatment. This allows for the more efficient production of various fuels.

[0043] The embodiments described above can be modified in the following ways:

[0044] (Variation 1) Figure 4 is a schematic diagram of the fuel production apparatus 1 according to Modification 1. This modification has the same configuration as the embodiment, except that the arrangement of the third separation section 20 and the fifth separation section 22 is reversed. The following description of this modification will focus on the configurations that differ from the embodiment, and the explanation of common configurations will be omitted as appropriate. In addition, the configuration downstream of the first distillation separation section 28 is the same as that of the embodiment and is therefore not shown.

[0045] A portion of the recycled gas flowing out of the first separation unit 6 is returned directly to the hydrocarbon production unit 4. The hydrocarbon production unit 4 receives a portion of the recycled gas from the first separation unit 6 and uses this recycled gas in the production of the C5+ component. The remaining recycled gas is sent to the fifth separation unit 22, which is located between the first separation unit 6 and the synthesis gas production unit 2. The fifth separation unit 22 separates hydrogen and carbon dioxide from the recycled gas. The hydrogen and carbon dioxide separated in the fifth separation unit 22 are supplied to the second separation unit 8. In addition, a portion of the carbon monoxide in the recycled gas may also be separated in the fifth separation unit 22.

[0046] The second separation unit 8 separates the hydrogen and carbon dioxide supplied from the fifth separation unit 22 into hydrogen and carbon dioxide. The hydrogen separated in the second separation unit 8 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this hydrogen to produce the C5+ component. The carbon dioxide separated in the second separation unit 8 is supplied to the synthesis gas production unit 2. The synthesis gas production unit 2 also uses this carbon dioxide to produce synthesis gas.

[0047] The recycled gas from which hydrogen and carbon dioxide have been separated in the fifth separation unit 22 is sent to the third separation unit 20, which is located between the fifth separation unit 22 and the synthesis gas production unit 2. The third separation unit 20 separates carbon monoxide from the recycled gas supplied from the fifth separation unit 22. The carbon monoxide separated in the third separation unit 20 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this carbon monoxide in the production of the C5+ component.

[0048] The recycled gas from which carbon monoxide has been separated in the third separation unit 20 is sent to a reforming unit 14 located between the third separation unit 20 and the synthesis gas production unit 2. The reforming unit 14 reforms the C4- component contained in the recycled gas into methane, hydrogen, carbon monoxide, and carbon dioxide. The reforming unit 14 can also receive C4- component from each distillation separation unit. The reforming unit 14 also reforms this C4- component into methane, hydrogen, carbon monoxide, and carbon dioxide. The recycled gas containing methane, hydrogen, carbon monoxide, and carbon dioxide produced in the reforming unit 14 is sent to the synthesis gas production unit 2. The synthesis gas production unit 2 also uses the methane, hydrogen, carbon monoxide, and carbon dioxide contained in the recycled gas for the production of synthesis gas. When the reaction temperature of the synthesis gas production unit 2 is set to 700°C or higher, preferably 800°C or higher, and more preferably 1000°C or higher, synthesis gas can be efficiently produced from methane and water by the reverse reaction of the reaction shown in formula (4) above.

[0049] (Modification 2) Figure 5 is a schematic diagram of the fuel production apparatus 1 according to Modification 2. This modification has the same configuration as the embodiment, except that the fuel production apparatus 1 is equipped with a fourth separation unit 26 instead of a fifth separation unit 22. The following description of this modification will focus on the configurations that differ from the embodiment, and the description of common configurations will be omitted as appropriate. Furthermore, the configuration downstream of the first distillation separation unit 28 is the same as that of the embodiment and is therefore not shown.

[0050] A portion of the recycled gas flowing out of the first separation unit 6 is returned directly to the hydrocarbon production unit 4. The hydrocarbon production unit 4 receives a portion of the recycled gas from the first separation unit 6 and uses this recycled gas in the production of C5+ components. The remaining recycled gas is sent to the third separation unit 20, which is located between the first separation unit 6 and the synthesis gas production unit 2. The third separation unit 20 separates carbon monoxide from the recycled gas. The carbon monoxide separated in the third separation unit 20 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this carbon monoxide in the production of C5+ components.

[0051] The recycled gas from which carbon monoxide has been separated in the third separation unit 20 is sent to the fourth separation unit 26, which is located between the third separation unit 20 and the synthesis gas production unit 2. The fourth separation unit 26 separates hydrogen from the recycled gas supplied from the third separation unit 20. The fourth separation unit 26 can use a known separator that separates hydrogen by, for example, the PSA method or membrane separation method. The hydrogen separated in the fourth separation unit 26 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this hydrogen to produce the C5+ component. This improves the utilization rate of hydrogen. In addition, the separation of hydrogen in the fourth separation unit 26 reduces the load on the reforming unit 14 and suppresses an increase in the size of the equipment. Therefore, the process efficiency of the fuel production apparatus 1 can be improved.

[0052] The recycled gas from which hydrogen has been separated in the fourth separation unit 26 is sent to a reforming unit 14 located between the fourth separation unit 26 and the synthesis gas production unit 2. The reforming unit 14 reforms the C4- component contained in the recycled gas into methane, hydrogen, carbon monoxide, and carbon dioxide. The reforming unit 14 can also receive C4- component from each distillation separation unit. The reforming unit 14 also reforms this C4- component into methane, hydrogen, carbon monoxide, and carbon dioxide. The recycled gas containing methane, hydrogen, carbon monoxide, and carbon dioxide generated in the reforming unit 14 is sent to the synthesis gas production unit 2. The synthesis gas production unit 2 also uses the methane, hydrogen, carbon monoxide, and carbon dioxide contained in the recycled gas for the production of synthesis gas. When the reaction temperature of the synthesis gas production unit 2 is set to 700°C or higher, preferably 800°C or higher, and more preferably 1000°C or higher, synthesis gas can be efficiently produced from methane and water by the reverse reaction of the reaction shown in formula (4) above.

[0053] (Variation 3) Figure 6 is a schematic diagram of the fuel production apparatus 1 according to Modification 3. This modification has the same configuration as Modification 2, except that the arrangement of the third separation section 20 and the fourth separation section 26 is reversed. Hereinafter, this modification will be described focusing on the configurations that differ from the embodiment and Modification 2, and the description of common configurations will be omitted as appropriate. Furthermore, the configuration downstream of the first distillation separation section 28 is the same as in the embodiment and is therefore not shown.

[0054] A portion of the recycled gas flowing out of the first separation unit 6 is returned directly to the hydrocarbon production unit 4. The hydrocarbon production unit 4 receives a portion of the recycled gas from the first separation unit 6 and uses this recycled gas in the production of C5+ components. The remaining recycled gas is sent to the fourth separation unit 26, which is located between the first separation unit 6 and the synthesis gas production unit 2. The fourth separation unit 26 separates hydrogen from the recycled gas. The hydrogen separated in the fourth separation unit 26 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this hydrogen in the production of C5+ components.

[0055] The recycled gas from which hydrogen has been separated in the fourth separation unit 26 is sent to the third separation unit 20, which is located between the fourth separation unit 26 and the synthesis gas production unit 2. The third separation unit 20 separates carbon monoxide from the recycled gas supplied from the fourth separation unit 26. The carbon monoxide separated in the third separation unit 20 is supplied to the hydrocarbon production unit 4. The hydrocarbon production unit 4 also uses this carbon monoxide in the production of the C5+ component.

[0056] The recycled gas from which carbon monoxide has been separated in the third separation unit 20 is sent to a reforming unit 14 located between the third separation unit 20 and the synthesis gas production unit 2. The reforming unit 14 reforms the C4- component contained in the recycled gas into methane, hydrogen, carbon monoxide, and carbon dioxide. The reforming unit 14 can also receive C4- component from each distillation separation unit. The reforming unit 14 also reforms this C4- component into methane, hydrogen, carbon monoxide, and carbon dioxide. The recycled gas containing methane, hydrogen, carbon monoxide, and carbon dioxide produced in the reforming unit 14 is sent to the synthesis gas production unit 2. The synthesis gas production unit 2 also uses the methane, hydrogen, carbon monoxide, and carbon dioxide contained in the recycled gas for the production of synthesis gas. When the reaction temperature of the synthesis gas production unit 2 is set to 700°C or higher, preferably 800°C or higher, and more preferably 1000°C or higher, synthesis gas can be efficiently produced from methane and water by the reverse reaction of the reaction shown in formula (4) above.

[0057] (Modification 4) Figure 7 is a schematic diagram of the fuel production apparatus 1 according to Modification 4. This modification has the same configuration as the embodiment, except that only the third separation unit 20 is located in the recycled gas line from the first separation unit 6 to the reforming unit 14. The following description of this modification will focus on the configurations that differ from the embodiment, and the description of common configurations will be omitted as appropriate. Also, the configuration downstream of the first distillation separation unit 28 is the same as in the embodiment and will therefore not be shown. In this modification, the third separation unit 20 separates carbon monoxide from the recycled gas sent from the first separation unit 6. The carbon monoxide separated in the third separation unit 20 is used in the hydrocarbon production unit 4 to produce the C5+ component. The recycled gas, which contains hydrogen, carbon dioxide, and the C4- component from which carbon monoxide has been separated in the third separation unit 20, is sent to the reforming unit 14. The reforming unit 14 reforms the C4- component contained in the recycled gas supplied from the third separation unit 20 into methane, etc. The recycled gas containing methane and other substances generated in the reforming unit 14 is used in the synthesis gas production unit 2.

[0058] (Other variations) A portion of the recycled gas may be discharged outside the system. The hydrogen gas and carbon dioxide gas supplied as raw materials to the synthesis gas production unit 2 may contain impurities such as nitrogen and sulfur compounds originating from their respective production sources. In addition, nitrogen compounds and oxygen-containing compounds may be produced as by-products by the reactions in each section, including the synthesis gas production unit 2, the hydrocarbon production unit 4, and the reforming unit 14. If the supply of recycled gas to the synthesis gas production unit 2, the hydrocarbon production unit 4, and the reforming unit 14 is repeated, these impurities and by-products will become concentrated, making the catalysts in each section more susceptible to poisoning.

[0059] Therefore, it is preferable that the fuel production apparatus 1 can intermittently discharge all of the gas outside the system as needed. Alternatively, it is preferable that a portion of the gas can be discharged outside the system continuously or intermittently as needed. The location from which the gas is discharged in the fuel production apparatus 1 can be set as appropriate. Examples of the piping in this embodiment include the piping connecting the first separation unit 6 and the hydrocarbon production unit 4 (for recycled gas), the piping connecting the first separation unit 6 and the third separation unit 20, the piping connecting the third separation unit 20 and the hydrocarbon production unit 4, the piping connecting the third separation unit 20 and the fifth separation unit 22, the piping connecting the fifth separation unit 22 and the second separation unit 8, the piping connecting the fifth separation unit 22 and the reforming unit 14, the piping connecting the reforming unit 14 and the synthesis gas production unit 2, the piping connecting the second separation unit 8 and the synthesis gas production unit 2 (for recycled CO2), the piping connecting the synthesis gas production unit 2 and the second separation unit 8 (for synthesis gas), the piping connecting the second separation unit 8 and the hydrocarbon production unit 4, the piping connecting the first distillation separation unit 28 and the reforming unit 14, the piping connecting the second distillation separation unit 36 ​​and the reforming unit 14, and the piping connecting the third distillation separation unit 38 and the reforming unit 14. The same applies to each modified example, including piping connecting each separation unit, piping connecting each separation unit to the hydrocarbon production unit 4, the reforming unit 14, or the synthesis gas production unit 2, and piping connecting each distillation separation unit to the reforming unit 14. In addition, methods for removing impurities and by-products by adsorption or chemical reaction can be considered to prevent catalyst poisoning.

[0060] The present invention may be specified by the following items. [1st item] A synthesis gas production unit (2) that uses carbon dioxide and hydrogen to produce synthesis gas containing carbon monoxide and hydrogen, A hydrocarbon production unit (4) that produces hydrocarbons (C5+) using synthesis gas, A first distillation separation unit (28) separates at least a first fraction and a second fraction that is lighter than the first fraction from the effluent from the hydrocarbon production unit (4), A hydrocracking section (32) that applies hydrocracking treatment to a portion of the first fraction, It comprises a contact decomposition section (34) that applies a contact decomposition treatment to the remaining portion of the first fraction, Fuel production equipment (1). [Second item] The apparatus includes a hydrogenation purification section (30) for performing hydrogenation purification on the second fraction. Fuel manufacturing apparatus (1) as described in item 1. [3rd item] The system includes a first separation unit (6) that separates recycled gas containing light hydrocarbons (C4-) with four or fewer carbon atoms from the spillage from the hydrocarbon production unit (4). At least one of the following is performed: supplying recycled gas to the synthesis gas production unit (2) and using the recycled gas for synthesis gas production, and supplying recycled gas to the hydrocarbon production unit (4) and using the recycled gas for hydrocarbon (C5+) production. A fuel manufacturing apparatus (1) as described in item 1 or item 2. [4th item] Synthesis gas also contains carbon dioxide, The fuel production apparatus (1) includes a second separation unit (8) that separates carbon dioxide from synthesis gas. The synthesis gas production unit (2) receives the carbon dioxide separated by the second separation unit (8) and uses the carbon dioxide in the production of synthesis gas. Fuel manufacturing apparatus (1) as described in item 3. [Item 5] Recycled gas also contains carbon monoxide. The fuel production apparatus (1) includes a third separation unit (20) that separates carbon monoxide from the recycled gas, The hydrocarbon production unit (4) receives the carbon monoxide separated by the third separation unit (20) and uses the carbon monoxide in the production of hydrocarbons (C5+). Fuel manufacturing apparatus as described in item 3 or 4 (1). [Item 6] Recycled gas also contains hydrogen. The fuel production apparatus (1) includes a fourth separation unit (26) that separates hydrogen from the recycled gas. The hydrocarbon production unit (4) receives the hydrogen separated by the fourth separation unit (26) and uses this hydrogen for the production of hydrocarbons (C5+). A fuel manufacturing apparatus (1) as described in any of items 3 through 5. [Item 7] Recycled gas also contains hydrogen, carbon monoxide, and carbon dioxide. The fuel production device (1) is A third separation unit (20) separates carbon monoxide from the recycled gas, The system includes a fifth separation unit (22) that receives a supply of recycled gas from which carbon monoxide has been separated in a third separation unit (20), and separates hydrogen and carbon dioxide from the recycled gas, The second separation unit (8) receives the hydrogen and carbon dioxide separated by the fifth separation unit (22) and separates the hydrogen and carbon dioxide into hydrogen and carbon dioxide. The hydrocarbon production unit (4) receives carbon monoxide separated by the third separation unit (20) and hydrogen separated by the second separation unit (8), and uses the carbon monoxide and hydrogen in the production of hydrocarbons (C5+). Fuel manufacturing apparatus (1) as described in item 4. [Item 8] Recycled gas also contains hydrogen and carbon monoxide. The fuel production device (1) is A third separation unit (20) separates carbon monoxide from the recycled gas, The system includes a fourth separation unit (26) that receives a supply of recycled gas from which carbon monoxide has been separated in a third separation unit (20), and separates hydrogen from the recycled gas, The hydrocarbon production unit (4) receives carbon monoxide separated by the third separation unit (20) and hydrogen separated by the fourth separation unit (26), and uses the carbon monoxide and hydrogen in the production of hydrocarbons (C5+). A fuel manufacturing apparatus (1) as described in any of items 3 through 6. [Item 9] Recycled gas also contains hydrogen, carbon monoxide, and carbon dioxide. The fuel production device (1) is A fifth separation unit (22) separates hydrogen and carbon dioxide from the recycled gas, The system includes a third separation unit (3) that receives a supply of recycled gas from which hydrogen and carbon dioxide have been separated in the fifth separation unit (22), and separates carbon monoxide from the recycled gas, The second separation unit (8) receives the hydrogen and carbon dioxide separated by the fifth separation unit (22) and separates the hydrogen and carbon dioxide into hydrogen and carbon dioxide. The hydrocarbon production unit (4) receives carbon monoxide separated by the third separation unit (20) and hydrogen separated by the second separation unit (8), and uses the carbon monoxide and hydrogen in the production of hydrocarbons (C5+). Fuel manufacturing apparatus (1) as described in item 4. [Item 10] Recycled gas also contains hydrogen and carbon monoxide. The fuel production device (1) is A fourth separation unit (26) separates hydrogen from the recycled gas, The system includes a third separation unit (20) that receives a supply of recycled gas from which hydrogen has been separated in a fourth separation unit (26) and separates carbon monoxide from the recycled gas, The hydrocarbon production unit (4) receives hydrogen separated by the fourth separation unit (26) and carbon monoxide separated by the third separation unit (20), and uses the hydrogen and carbon monoxide in the production of hydrocarbons (C5+). A fuel manufacturing apparatus (1) as described in any of items 3 through 6. [Item 11] It is equipped with a reforming section (14) that reforms light hydrocarbons (C4-) into methane, The synthesis gas production unit (2) receives the methane produced by the reforming unit (14) and uses the methane in the production of synthesis gas. A fuel manufacturing apparatus (1) as described in any of items 3 through 10. [Item 12] The first distillation separation unit (28) receives the effluent from which the recycled gas has been separated in the first separation unit (6), and separates light hydrocarbons (C4-) from the effluent. The reforming unit (14) receives light hydrocarbons (C4-) from the first distillation separation unit (28) and reforms the light hydrocarbons (C4-) into methane. Fuel manufacturing apparatus as described in item 11 (1). [Item 13] A hydrogenation purification section (30) that performs hydrogenation purification on the second fraction, A second distillation separation unit (36) receives a supply of a second fraction that has undergone hydrogenation purification in a hydrogenation purification unit (30) and a first fraction that has undergone hydrogen cracking in a hydrocracking unit (32), and distills the second fraction and the first fraction. The apparatus includes a third distillation separation unit (38) that receives a supply of a first fraction that has undergone catalytic cracking treatment in a catalytic cracking unit (34) and distills the first fraction, The second distillation separation section (36) separates light hydrocarbons (C4-) from the second and first fractions. The third distillation separation section (38) separates light hydrocarbons (C4-) from the first fraction. The reforming unit (14) receives light hydrocarbons (C4-) from at least one of the second distillation separation unit (36) and the third distillation separation unit (38), and reforms the light hydrocarbons (C4-) into methane. Fuel manufacturing apparatus as described in item 11 (1). [Item 14] Recycled gas also contains carbon monoxide. The fuel production apparatus (1) includes a third separation unit (20) that separates carbon monoxide from the recycled gas, The system includes a reforming unit (14) that receives the recycled gas from which carbon monoxide has been separated in the third separation unit (30) and reforms the light hydrocarbons (C4-) contained in the recycled gas into methane, The hydrocarbon production unit (4) receives the carbon monoxide separated by the third separation unit (20) and uses the carbon monoxide in the production of hydrocarbons (C5+). The synthesis gas production unit (2) receives the methane produced by the reforming unit (14) and uses the methane in the production of synthesis gas. A fuel manufacturing apparatus (1) as described in any of items 3 through 13. [Item 15] A second distillation separation unit (36) receives a supply of a second fraction that has undergone hydrogenation purification in a hydrogenation purification unit (30) and a first fraction that has undergone hydrogen cracking in a hydrocracking unit (32), and distills the second fraction and the first fraction. The apparatus includes a third distillation separation unit (38) that receives a supply of a first fraction that has undergone catalytic cracking treatment in a catalytic cracking unit (34) and distills the first fraction, The second distillation separation unit (36) separates at least one selected from the group consisting of light hydrocarbons (C4-) with 4 or fewer carbon atoms, naphtha fraction, kerosene fraction, diesel fuel fraction, and fraction heavier than diesel fuel from the second fraction that has undergone hydropurification treatment and the first fraction that has undergone hydrocracking treatment. The third distillation separation section (38) separates at least one selected from the group consisting of light hydrocarbons (C4-) having 4 or fewer carbon atoms, gasoline fraction, light cycle oil, and clarified oil from the first fraction that has undergone catalytic cracking treatment. A fuel manufacturing apparatus (1) as described in any of items 2 through 14. [Item 16] The second distillation separation section (36) separates the heavier fraction from the diesel fuel. The hydrocracking unit (32) receives a portion or all of the fraction heavier than diesel fuel separated by the second distillation separation unit (36), and subjects the fraction to hydrocracking treatment. Fuel manufacturing apparatus as described in item 15 (1). [Item 17] The third distillation separation section (38) separates the clarified oil, The catalytic cracking unit (34) receives part or all of the clarified oil separated by the third distillation separation unit (38) and performs catalytic cracking treatment on the clarified oil. Fuel manufacturing apparatus as described in item 15 or item 16 (1). [Item 18] A synthesis gas production process that uses carbon dioxide and hydrogen to produce synthesis gas containing carbon monoxide and hydrogen, A hydrocarbon manufacturing process that produces hydrocarbons (C5+) using synthesis gas, A first distillation separation step separates at least a first fraction and a second fraction that is lighter than the first fraction from the effluent from the hydrocarbon manufacturing process, A hydrocracking process in which a portion of the first fraction is subjected to hydrocracking treatment, A catalytic cracking step is included in which the remaining portion of the first fraction is subjected to catalytic cracking treatment. Fuel production method. [Industrial applicability]

[0061] This invention can be used in fuel manufacturing apparatus and fuel manufacturing methods. [Explanation of Symbols]

[0062] 1 Fuel production unit, 2 Synthesis gas production unit, 4 Hydrocarbon production unit, 6 First separation unit, 8 Second separation unit, 14 Reforming unit, 20 Third separation unit, 22 Fifth separation unit, 26 Fourth separation unit, 28 First distillation separation unit, 30 Hydrogenation and purification unit, 32 Hydrocracking unit, 34 Catalytic cracking unit, 36 Second distillation separation unit, 38 Third distillation separation unit.

Claims

1. A synthesis gas production unit that uses carbon dioxide and hydrogen to produce synthesis gas containing carbon monoxide and hydrogen, A hydrocarbon production unit that produces hydrocarbons using the aforementioned synthesis gas, A first distillation separation unit separates at least a first fraction and a second fraction that is lighter than the first fraction from the effluent from the hydrocarbon production unit, A hydrocracking unit that subjects a portion of the first fraction to hydrocracking treatment, The apparatus comprises a contact decomposition unit that applies a contact decomposition treatment to another portion of the first fraction, Fuel production equipment.

2. The apparatus includes a hydrogenation purification section that performs hydrogenation purification on the second fraction. The fuel manufacturing apparatus according to claim 1.

3. The system includes a first separation unit that separates recycled gas containing light hydrocarbons with four or fewer carbon atoms from the waste product discharged from the hydrocarbon production unit. At least one of the following is performed: supplying the recycled gas to the synthesis gas production unit and using the recycled gas in the production of the synthesis gas, and supplying the recycled gas to the hydrocarbon production unit and using the recycled gas in the production of the hydrocarbon. A fuel production apparatus according to claim 1 or 2.

4. The aforementioned synthesis gas also contains carbon dioxide, The fuel production apparatus includes a second separation unit for separating carbon dioxide from the synthesis gas. The synthesis gas production unit receives the carbon dioxide separated by the second separation unit and uses the carbon dioxide in the production of the synthesis gas. The fuel manufacturing apparatus according to claim 3.

5. The aforementioned recycled gas also contains carbon monoxide. The fuel production apparatus includes a third separation unit for separating carbon monoxide from the recycled gas. The hydrocarbon production unit receives the carbon monoxide separated by the third separation unit and uses the carbon monoxide in the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 3.

6. The aforementioned recycled gas also contains hydrogen, The fuel production apparatus includes a fourth separation unit for separating hydrogen from the recycled gas. The hydrocarbon production unit receives the hydrogen separated by the fourth separation unit and uses the hydrogen for the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 3.

7. The aforementioned recycled gas also contains hydrogen, carbon monoxide, and carbon dioxide. The fuel production apparatus, A third separation unit for separating carbon monoxide from the recycled gas, The system includes a fifth separation unit that receives the recycled gas from which carbon monoxide has been separated in the third separation unit and separates hydrogen and carbon dioxide from the recycled gas, The second separation unit receives the hydrogen and carbon dioxide separated by the fifth separation unit and separates the hydrogen and carbon dioxide into hydrogen and carbon dioxide. The hydrocarbon production unit receives the carbon monoxide separated by the third separation unit and the hydrogen separated by the second separation unit, and uses the carbon monoxide and hydrogen in the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 4.

8. The aforementioned recycled gas also contains hydrogen and carbon monoxide. The fuel production apparatus, A third separation unit for separating carbon monoxide from the recycled gas, The system includes a fourth separation unit that receives the recycled gas from which carbon monoxide has been separated in the third separation unit and separates hydrogen from the recycled gas, The hydrocarbon production unit receives the carbon monoxide separated by the third separation unit and the hydrogen separated by the fourth separation unit, and uses the carbon monoxide and hydrogen in the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 3.

9. The aforementioned recycled gas also contains hydrogen, carbon monoxide, and carbon dioxide. The fuel production apparatus, A fifth separation unit separates hydrogen and carbon dioxide from the recycled gas, The system includes a third separation unit that receives the recycled gas from which hydrogen and carbon dioxide have been separated in the fifth separation unit, and separates carbon monoxide from the recycled gas, The second separation unit receives the hydrogen and carbon dioxide separated by the fifth separation unit and separates the hydrogen and carbon dioxide into hydrogen and carbon dioxide. The hydrocarbon production unit receives the carbon monoxide separated by the third separation unit and the hydrogen separated by the second separation unit, and uses the carbon monoxide and hydrogen in the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 4.

10. The aforementioned recycled gas also contains hydrogen and carbon monoxide. The fuel production apparatus, A fourth separation unit for separating hydrogen from the aforementioned recycled gas, The system includes a third separation unit that receives the recycled gas from which hydrogen has been separated in the fourth separation unit and separates carbon monoxide from the recycled gas, The hydrocarbon production unit receives the hydrogen separated by the fourth separation unit and the carbon monoxide separated by the third separation unit, and uses the hydrogen and carbon monoxide in the production of the hydrocarbons. The fuel manufacturing apparatus according to claim 3.

11. The unit comprises a reforming section for reforming the aforementioned light hydrocarbons into methane, The synthesis gas production unit receives the methane produced by the reforming unit and uses the methane in the production of the synthesis gas. The fuel manufacturing apparatus according to claim 3.

12. The first distillation separation unit receives the effluent from which the recycled gas has been separated in the first separation unit, and separates the light hydrocarbons from the effluent. The reforming unit receives the light hydrocarbons from the first distillation separation unit and also reforms the light hydrocarbons into methane. The fuel manufacturing apparatus according to claim 11.

13. A hydrogenation purification unit that performs hydrogenation purification on the second fraction, A second distillation separation unit receives the second fraction, which has been subjected to hydrogenation purification in the hydrogenation purification unit, and the first fraction, which has been subjected to hydrogen cracking in the hydrogen cracking unit, and distills the second fraction and the first fraction. The system includes a third distillation separation unit that receives the first fraction, which has been subjected to catalytic cracking treatment in the catalytic cracking unit, and distills the first fraction, The second distillation separation unit separates the light hydrocarbons from the second fraction that has undergone the hydrogenation purification treatment and the first fraction that has undergone the hydrocracking treatment. The third distillation separation unit separates the light hydrocarbons from the first fraction that has undergone the catalytic cracking treatment. The reforming unit receives the light hydrocarbons from at least one of the second distillation separation unit and the third distillation separation unit, and reforms the light hydrocarbons into methane. The fuel manufacturing apparatus according to claim 11.

14. The aforementioned recycled gas also contains carbon monoxide. The fuel production apparatus includes a third separation unit that separates carbon monoxide from the recycled gas, The system includes a reforming unit that receives the recycled gas from which carbon monoxide has been separated in the third separation unit and reforms the light hydrocarbons contained in the recycled gas into methane, The hydrocarbon production unit receives the carbon monoxide separated by the third separation unit and uses the carbon monoxide in the production of the hydrocarbons. The synthesis gas production unit receives the methane produced by the reforming unit and uses the methane in the production of the synthesis gas. The fuel manufacturing apparatus according to claim 3.

15. A second distillation separation unit receives the second fraction, which has been subjected to hydrogenation purification in the hydrogenation purification unit, and the first fraction, which has been subjected to hydrogen cracking in the hydrogen cracking unit, and distills the second fraction and the first fraction. The system includes a third distillation separation unit that receives the first fraction, which has been subjected to catalytic cracking treatment in the catalytic cracking unit, and distills the first fraction, The second distillation separation unit separates at least one selected from the group consisting of light hydrocarbons having 4 or fewer carbon atoms, naphtha fraction, kerosene fraction, diesel fuel fraction, and fraction heavier than diesel fuel from the second fraction subjected to the hydrogenation purification treatment and the first fraction subjected to the hydrocracking treatment. The third distillation separation unit separates from the first fraction subjected to the catalytic cracking treatment at least one selected from the group consisting of light hydrocarbons having 4 or fewer carbon atoms, gasoline fraction, light cycle oil, and clarified oil. The fuel manufacturing apparatus according to claim 2.

16. The second distillation separation unit separates the heavier fraction from the light oil, The hydrocracking unit receives a portion or all of the fraction heavier than the diesel fuel separated by the second distillation separation unit, and subjects the fraction to hydrocracking treatment. The fuel manufacturing apparatus according to claim 15.

17. The third distillation separation unit separates the clarified oil, The catalytic cracking unit receives a portion or all of the clarified oil separated by the third distillation separation unit and performs a catalytic cracking treatment on the clarified oil. The fuel manufacturing apparatus according to claim 15.

18. A synthesis gas production process that uses carbon dioxide and hydrogen to produce synthesis gas containing carbon monoxide and hydrogen, A hydrocarbon manufacturing process for producing hydrocarbons using the aforementioned synthesis gas, A first distillation separation step for separating at least a first fraction and a second fraction that is lighter than the first fraction from the effluent from the hydrocarbon manufacturing process, A hydrocracking step in which a portion of the first fraction is subjected to hydrocracking treatment, A catalytic cracking step is performed on another portion of the first fraction, Fuel production method.

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