Method for producing syngas and fuel production system

Abstract

To provide a method for producing syngas and a fuel production system that can effectively utilize hydrogen, improve energy efficiency, and reduce environmental load.SOLUTION: A method for producing syngas for manufacturing fuel from a biomass feedstock comprises a step of supplying hydrogen to the biomass feedstock such that a mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03, and does not include a step of supplying steam.SELECTED DRAWING: None

Description

[Technical Field]

[0001] The present invention relates to a method for producing synthesis gas and a fuel production system. [Background technology]

[0002] Efforts aimed at mitigating or reducing the impact of climate change have been ongoing for some time, and research and development into reducing carbon dioxide emissions is being carried out to achieve this. In recent years, synthetic fuels made from hydrogen generated from electricity generated by renewable energy sources and carbon sources such as biomass and carbon dioxide emitted from factories have been attracting attention as an alternative to fossil fuels.

[0003] The general procedure for producing liquid fuels such as methanol and gasoline using biomass as a feedstock is as follows: A liquid fuel is produced from biomass feedstock through the following steps: a gasification process in which biomass feedstock that has undergone a specified pretreatment is gasified together with water and oxygen in a gasifier to produce a synthesis gas containing hydrogen and carbon monoxide; a cleaning process in which the synthesis gas produced is cleaned and tar is removed; an H2 / CO ratio adjustment process in which the H2 / CO ratio of the synthesis gas that has undergone the cleaning process is adjusted to a target ratio appropriate for the liquid fuel to be produced; a desulfurization process in which sulfur components are removed from the synthesis gas that has undergone the H2 / CO ratio adjustment process; and a fuel production process in which liquid fuel is produced from the synthesis gas that has undergone the desulfurization process.

[0004] In many cases, the H2 / CO ratio of the synthesis gas produced through the gasification process does not reach the target ratio, resulting in a hydrogen deficiency. For this reason, in the H2 / CO ratio adjustment process, hydrogen is generated by reacting carbon monoxide with water, and the H2 / CO ratio is raised to the target ratio.

[0005] Patent Document 1 discloses an invention in which, in a fuel production system for producing synthetic fuel from biomass feedstock as described above, hydrogen is produced using electricity generated from renewable energy, and the produced hydrogen is mixed with synthesis gas produced by a gasification furnace to adjust the H2 / CO ratio to a target ratio. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] Patent Publication No. 2021-147505 Summary of the Invention [Problem to be solved by the invention]

[0007] In the fuel production system disclosed in Patent Document 1, hydrogen is produced by an electrolysis device using electricity generated by renewable energy, and the produced hydrogen is stored in a hydrogen tank. Here, wind power and solar power, which are assumed as renewable energy sources in Patent Document 1, are not always generated in constant amounts, so the amount of hydrogen remaining in the hydrogen tank can fluctuate significantly depending on environmental conditions. Therefore, if the remaining hydrogen level approaches the lower limit of the hydrogen tank, it may become impossible to supply a sufficient amount of hydrogen to the gasification furnace, etc., which may ultimately increase carbon dioxide emissions in the gasification process, H2 / CO ratio adjustment process, etc. As a result, the carbon dioxide emission intensity (the amount of carbon dioxide emitted to produce a unit amount of liquid fuel, also known as "carbon intensity") of the liquid fuel produced by the fuel production system may worsen.

[0008] Furthermore, conventionally, in order to operate a fuel production system, it is necessary to heat the reaction field, raw materials, etc. to a predetermined temperature, but since synthesis gas cannot be produced in the unsteady state during the temperature rise, there is a problem of poor energy efficiency. Furthermore, if the hydrogen gas produced in the fuel production system exceeds the capacity of the hydrogen tank, it can only be used as fuel or vented, which poses the problem of ineffective use of hydrogen.

[0009] In order to solve the above problems, the present application aims to provide a synthesis gas production method and a fuel production system that can effectively utilize hydrogen, improve energy efficiency, and reduce the burden on the environment, thereby contributing to mitigating or reducing the impact of climate change. [Means for solving the problem]

[0010] [1] A method for producing synthesis gas for producing fuel from biomass feedstock, comprising: The method includes a step of supplying hydrogen to a biomass raw material so that a mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; A method for producing synthesis gas that does not include a step of supplying steam.

[0011] The synthesis gas production method of the present invention can effectively utilize hydrogen as a raw material for synthesis gas production even when the fuel production system is in an unsteady state in the preparation stage. Furthermore, because the supply of hydrogen increases, sufficient amounts of synthesis gas can be produced even when there is no supply of high-purity, high-pressure hydrogen or steam. This reduces the energy consumption required to produce high-purity, high-pressure hydrogen and steam, improving energy efficiency. Furthermore, as the supply of hydrogen increases, reactions that consume carbon dioxide as a raw material also proceed more easily, which reduces carbon dioxide emissions and the burden on the environment.

[0012] [2] A method for producing synthesis gas for producing fuel from biomass feedstock, comprising: The method includes a step of supplying hydrogen to a biomass raw material so that a mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; A method for producing synthesis gas, comprising a step of supplying steam to a biomass feedstock so that the mass ratio expressed as [mass of steam] / [mass of biomass] is 1.0 or less.

[0013] The synthesis gas production method of the present invention can effectively utilize hydrogen as a raw material for synthesis gas production even when the fuel production system is in an unsteady state in the preparation stage. Furthermore, because the hydrogen supply volume increases, sufficient amounts of synthesis gas can be produced even when the supply of high-purity, high-pressure hydrogen and steam is low. This reduces the energy consumption required to produce high-purity, high-pressure hydrogen and steam, improving energy efficiency. Furthermore, as the supply of hydrogen increases, reactions that consume carbon dioxide as a raw material also proceed more easily, which reduces carbon dioxide emissions and the burden on the environment.

[0014] [3] The method for producing a synthesis gas according to [1] or [2], wherein the gasification of the biomass feedstock is carried out at a temperature of 700°C or higher but lower than 850°C.

[0015] The synthesis gas production method of the present invention can effectively utilize hydrogen as a raw material for synthesis gas production even when the temperature of the gasification furnace is low, at 700°C or higher but lower than 850°C, in an unsteady state where the fuel production system is in the preparation stage.

[0016] [4] The method for producing a synthesis gas according to [1] or [2], wherein the supply amount of the hydrogen gas is 100 L / day or more.

[0017] The synthesis gas production method of the present invention can effectively utilize hydrogen as a raw material for synthesis gas production by supplying sufficient hydrogen at a rate of 100 L / day or more, even when the fuel production system is in an unsteady state in the preparation stage. Furthermore, because the supply of hydrogen increases, sufficient amounts of synthesis gas can be produced even when there is no or little steam supply, which reduces the energy consumption required to produce steam and improves energy efficiency.

[0018] [5] A fuel production system for producing liquid fuel from biomass feedstock, comprising: a gasification apparatus including a gasification furnace that reacts biomass raw material, hydrogen, carbon monoxide, and carbon dioxide to produce a synthesis gas containing hydrocarbons by the synthesis gas production method according to [1]; a hydrogen supply means for supplying hydrogen to the gasification apparatus so that the mass ratio expressed as [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; Equipped with A fuel production system comprising: a steam supply control means for stopping the supply of steam from a steam supply means that supplies steam to the gasification apparatus.

[0019] The fuel production system of the present invention can effectively utilize hydrogen as a raw material for producing synthesis gas even when the fuel production system is in an unsteady state in the preparation stage. Furthermore, because the supply of hydrogen increases, sufficient amounts of synthesis gas can be produced even when there is no supply of high-purity, high-pressure hydrogen or steam. This reduces the energy consumption required to produce high-purity, high-pressure hydrogen and steam, improving energy efficiency. Furthermore, as the supply of hydrogen increases, reactions that consume carbon dioxide as a raw material also proceed more easily, which reduces carbon dioxide emissions and the burden on the environment.

[0020] [6] A fuel production system for producing liquid fuel from biomass feedstock, comprising: a gasification apparatus including a gasification furnace that reacts biomass raw material, hydrogen, carbon monoxide, and carbon dioxide to produce a synthesis gas containing hydrocarbons by the synthesis gas production method according to [2]; a hydrogen supply means for supplying hydrogen to the gasification apparatus so that the mass ratio expressed as [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; Equipped with A fuel production system comprising: a steam supply control means for supplying steam from a steam supply means that supplies steam to the gasification apparatus so that a mass ratio expressed as [mass of steam] / [mass of biomass] is 1.0 or less.

[0021] The fuel production system of the present invention can effectively utilize hydrogen as a raw material for producing synthesis gas even when the fuel production system is in an unsteady state in the preparation stage. Furthermore, because the hydrogen supply volume increases, sufficient amounts of synthesis gas can be produced even when the supply of high-purity, high-pressure hydrogen and steam is low. This reduces the energy consumption required to produce high-purity, high-pressure hydrogen and steam, improving energy efficiency. Furthermore, as the supply of hydrogen increases, reactions that consume carbon dioxide as a raw material also proceed more easily, which reduces carbon dioxide emissions and the burden on the environment.

[0022] [7] The fuel production system according to [5] or [6], further comprising a hydrogen gas supply control means (1) that supplies hydrogen to the gasification device when the temperature inside the gasification furnace is 700°C or higher and lower than 850°C.

[0023] The fuel production system of the present invention can effectively utilize hydrogen as a raw material for producing synthesis gas even when the temperature of the gasifier is low, at or above 700°C and below 850°C, in an unsteady state in which the fuel production system is in the preparation stage.

[0024] [8] A fuel production system according to [5] or [6], comprising a hydrogen gas supply control means (2) that supplies hydrogen to the gasification apparatus when the supply amount of the hydrogen gas that can be supplied to the gasification apparatus is 100 L / day or more.

[0025] The fuel production system of the present invention can supply sufficient hydrogen at a rate of 100 L / day or more, even when the fuel production system is in an unsteady state during preparation, thereby enabling effective use of hydrogen as a raw material for synthesis gas production. Furthermore, because the supply of hydrogen increases, sufficient amounts of synthesis gas can be produced even when there is no or little steam supply, which reduces the energy consumption required to produce steam and improves energy efficiency.

[0026] [9] A liquid fuel synthesis gas supply means for using the synthesis gas as a liquid fuel raw material when the gasification rate of the biomass raw material is 50 mol% or more; The fuel production system according to [5] or [6], further comprising a heat source synthesis gas supply means for using the synthesis gas as a heat source for the gasification furnace when the gasification rate of the biomass feedstock is less than 50 mol%.

[0027] The fuel production system of the present invention can produce synthesis gas even when the fuel production system is in an unsteady state in the preparation stage, and can effectively utilize this synthesis gas for use as a raw material for liquid fuel. Furthermore, even if the gasification rate is insufficient, the obtained synthesis gas can be used as a heat source for the gasification furnace, thereby reducing energy consumption and improving energy efficiency. Furthermore, by effectively utilizing the synthesis gas obtained, the amount of emissions into the environment can be reduced, thereby reducing the burden on the environment. [Effects of the Invention]

[0028] According to the present invention, it is possible to provide a synthesis gas production method and a fuel production system that can effectively utilize hydrogen, improve energy efficiency, and reduce the burden on the environment. [Brief explanation of the drawings]

[0029] [Figure 1] 1 is a flowchart showing a configuration of a fuel production method according to an embodiment of the present invention. [Figure 2] 1 is a schematic diagram illustrating a fuel production system according to an embodiment of the invention. [Figure 3] FIG. 1 is a schematic diagram illustrating a fuel production system according to another embodiment of the present invention. [Figure 4] FIG. 3 is a diagram showing the relationship between the concentration of each component of the synthesis gas in the gasification furnace and the amount of hydrogen supplied to the gasification furnace. [Figure 5]1 is a diagram comparing the amount and breakdown of carbon dioxide generated in the entire system when a predetermined amount of synthesis gas with a predetermined target ratio is produced, between a conventional fuel production system and the fuel production system according to this embodiment. FIG. [Figure 6] FIG. 4 is a diagram showing various thresholds set for the remaining amount of hydrogen in a hydrogen tank. [Figure 7] 10 is a flowchart showing a specific procedure of a normal control process. [Figure 8] 10 is a flowchart showing a specific procedure during low-temperature operation. [Figure 9] FIG. 1 is a diagram showing the relationship between the concentration of each component of the synthesis gas generated in the gasification furnace and the temperature of the gasification furnace when the amount of hydrogen supplied from outside the gasification furnace is set to 0. [Figure 10] 1 is a graph showing the results of Example 1, and is a graph showing the relationship between the H / B ratio and the gasification rate of biomass feedstock when steam is supplied. [Figure 11] 1 is a graph showing the results of Example 2, and is a graph showing the relationship between the S / B ratio, the H / B ratio, and the gasification rate of the biomass feedstock when steam is supplied. [Figure 12] 1 is a graph showing the results of Example 3, illustrating the relationship between the H / B ratio and the gasification rate of biomass feedstock when steam was supplied and when it was not supplied. [Figure 13] 10 is a graph showing the results of Example 3, specifically showing the relationship between the H / B ratio and the temperature inside the gasification furnace when steam was supplied. [Figure 14] 10 is a graph showing the results of Example 3, specifically showing the relationship between the H / B ratio and the temperature inside the gasification furnace when steam was not supplied. [Figure 15] 1 is a graph showing the results of Example 4, which is a graph showing the relationship between the H / B ratio and the gasification rate of biomass feedstock when steam was not supplied under low temperature conditions inside the gasification furnace. DETAILED DESCRIPTION OF THE INVENTION

[0030] Hereinafter, an embodiment of the fuel production method of the present invention will be specifically described, but the present invention is not limited to the following embodiment.

[0031] <<Fuel manufacturing method>> A fuel production method according to one embodiment of the present invention includes a step of supplying hydrogen gas during gasification of a biomass feedstock so that the mass ratio expressed as [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.05.

[0032] FIG. 1 is a flowchart showing the configuration of a fuel production method according to this embodiment. As shown in FIG. 1 , the fuel production method according to the embodiment includes a biomass feedstock supply step S2 in which a biomass feedstock is supplied to a gasification furnace for producing a synthesis gas, a hydrogen supply step S12 in which hydrogen is supplied to the gasification furnace, a synthesis gas production step S3 in which a synthesis gas containing hydrocarbons is produced by reacting the biomass feedstock, hydrogen, steam, etc., a Fischer-Tropsch synthesis step S6 in which a Fischer-Tropsch oil is produced by subjecting the produced synthesis gas to a Fischer-Tropsch synthesis reaction, and a heavy fraction (approximately C ) contained in the Fischer-Tropsch oil. 21 or more) is hydrocracking using hydrogen gas to change the carbon number to C 20 and a fractionation step S8 in which the Fischer-Tropsch oil is hydrocracking and then fractionated to obtain a liquid fuel and the FT off-gas. In the fuel production method according to the embodiment, in the hydrogen supply step S12 of supplying hydrogen to the gasification furnace, hydrogen gas is supplied so that the mass ratio expressed as [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.05.

[0033] In the biomass raw material supply step S2, biomass raw materials such as rice husks, bagasse, and wood are subjected to a predetermined pretreatment, and the pretreated biomass raw materials are supplied via a raw material supply line to a gasification furnace of a gasification apparatus that performs the synthesis gas production step S3. Here, the pretreatment of the biomass raw materials includes, for example, a drying step for drying the raw materials and a crushing step for crushing the raw materials.

[0034] In the hydrogen supply step S12, hydrogen is supplied to the gasification furnace of the gasification apparatus. The hydrogen may be generated by, for example, electrolysis of water. The amount of hydrogen supplied is such that the mass ratio, expressed as [mass of hydrogen gas] / [mass of biomass], is 0.01 to 0.05, preferably 0.01 to 0.04, and more preferably 0.01 to 0.03. When the mass ratio is within the above range, it becomes easier to adjust the proportion of hydrogen contained in the synthesis gas supplied to the Fischer-Tropsch synthesis step S6 to a higher value, and carbon dioxide is more easily consumed as a raw material. This makes it possible to produce synthesis gas even without supplying steam, and hydrogen can be effectively utilized, which makes it easier to further improve energy efficiency.

[0035] In the fuel production method according to this embodiment, the steam supply step S9 for supplying steam to the gasification furnace of the gasification device is not required, but in fuel production methods according to other embodiments, a step of supplying steam so that the mass ratio expressed as [mass of steam] / [mass of biomass] is 1.0 or less may be included. When steam is supplied, the mass ratio expressed as [mass of steam] / [mass of biomass] is preferably 0.01 to 1.0, more preferably 0.05 to 0.8, and even more preferably 0.1 to 0.6. When the mass ratio is within the above range, it becomes easier to adjust the proportion of hydrogen contained in the synthesis gas supplied to the Fischer-Tropsch synthesis step S6 to be higher, and carbon dioxide can be more easily consumed as a raw material, which makes it easier to improve energy efficiency.

[0036] When water vapor is supplied, the temperature of the water vapor is preferably less than 500° C. When the temperature of the water vapor is within the above range, it becomes easier to reduce the amount of energy consumed for heating the water vapor.

[0037] In the synthesis gas production step S3, the biomass raw material, hydrogen, carbon monoxide, and carbon dioxide are reacted to produce a synthesis gas containing hydrocarbons. When hydrogen, carbon monoxide, and carbon dioxide are fed into a gasification furnace to which biomass raw materials have been fed, a total of eight types of gasification reactions and their reverse reactions, such as those shown in the following formulas (1-1) to (1-8), proceed in the gasification furnace, producing synthesis gas containing hydrogen, carbon monoxide, and hydrocarbons.

[0038] [ka]

[0039] [ka]

[0040] In the present invention, since hydrogen is supplied, the reactions represented by the above formulas (1-3) and (1-5) to (1-7) using hydrogen as a raw material proceed more easily, and the content of hydrocarbon gas in the synthesis gas tends to increase. The content of hydrocarbon gas in the synthesis gas is preferably 10% by mass or less, and more preferably 8% by mass or less, based on the total mass of the synthesis gas. The above numerical range can be achieved by appropriately adjusting the reaction temperature (gasification furnace temperature) during gasification, the amount of hydrogen gas supplied, and the amount of steam supplied. When the content of hydrocarbon gas is within the above range, the synthesis gas containing hydrocarbon gas can be used as fuel for heating the gasification furnace or as a raw material for producing liquid fuel, thereby improving energy efficiency.

[0041] The gasification of the biomass feedstock is preferably carried out at a temperature of 700° C. or higher but lower than 900° C., and more preferably at a temperature of 700° C. or higher but lower than 850° C. When the gasification temperature is within the above range, it becomes easier to reduce energy consumption for heating the gasification furnace.

[0042] The supply rate of the hydrogen gas is preferably 100 L / day or more, more preferably 200 L / day or more, and even more preferably 300 L / day or more. When the supply rate of the hydrogen gas is within the above range, the hydrogen gas is supplied to the gasification of the biomass feedstock, and excess hydrogen gas can also be supplied as fuel for heating the gasification furnace.

[0043] A fuel production system according to an embodiment of the present invention will be described below with reference to the drawings. do.

[0044] 2 is a diagram showing the configuration of a fuel production system 1 according to this embodiment. The fuel production system 1 includes a biomass material supplying device 2 that supplies biomass material, a gasification device 3 that gasifies the biomass material supplied from the biomass material supplying device 2 and produces a synthesis gas containing hydrogen and carbon monoxide, an FT device 6 that produces liquid fuel from the synthesis gas supplied from the gasification device 3, a hydrogen production device 10 that produces hydrogen, a hydrogen tank 12 that stores the hydrogen gas produced in the hydrogen production device 10, and a control device 13 that controls these devices, and produces liquid fuel from biomass material using these devices.

[0045] The biomass raw material supply device 2 performs predetermined pretreatment on biomass raw materials such as rice husks, bagasse, and wood, and supplies the pretreated biomass raw materials to the gasification furnace of the gasification device 3 via a raw material supply path. Here, the pretreatment of the biomass raw materials includes, for example, a drying process for drying the raw materials and a crushing process for crushing the raw materials. The method for supplying the biomass raw material to the gasification furnace is not particularly limited, and any known supply method can be used.

[0046] The gasification device 3 may include a gasification furnace that gasifies the biomass raw material supplied through the raw material supply path, a gasification furnace sensor group consisting of multiple sensors that detect the internal condition of the gasification furnace, a steam supply device that supplies steam into the gasification furnace, an oxygen supply device that supplies oxygen into the gasification furnace, a heating device that heats the gasification furnace, a scrubber that cleans the synthesis gas discharged from the gasification furnace, and a desulfurization device that removes sulfur components from the synthesis gas cleaned by the scrubber and supplies the cleaned synthesis gas to the FT device 4. The reaction conditions for producing the synthesis gas are not particularly limited, and known reaction conditions can be used.

[0047] The steam supply device 9 vaporizes water stored in a water tank (not shown) and supplies the vapor to the gasification furnace. The heating device heats the gasification furnace by consuming fuel supplied from a fuel tank (not shown) and electricity supplied from a power source (not shown). The amount of steam supplied from the steam supply device to the gasification furnace and the amount of heat input from the heating device to the gasification furnace are controlled by the control device 13. Note that in the fuel production system 1 according to this embodiment, by supplying hydrogen from the hydrogen production device 10 (described below) to the gasification furnace or the raw material supply path, it may become unnecessary to actively supply steam from the steam supply device to the gasification furnace. In this case, the steam supply device can be omitted from the fuel production system 1. The method for producing and supplying steam is not particularly limited, and any known production and supply method can be used.The method for heating the gasification furnace is not particularly limited, and any known heating method can be used.

[0048] When water, oxygen, heat, etc. are fed into a gasification furnace into which biomass raw materials have been fed using the steam supply device, oxygen supply device, and heating device described above, a total of eight types of gasification reactions and their reverse reactions, such as those shown in the above formulas (1-1) to (1-8), proceed in the gasification furnace, and synthesis gas containing hydrogen, carbon monoxide, and hydrocarbons is produced.

[0049] The gasification furnace sensor group is composed of, for example, a pressure sensor that detects the pressure inside the gasification furnace, a temperature sensor that detects the temperature inside the gasification furnace, an H2 / CO sensor that detects the H2 / CO ratio corresponding to the ratio of hydrogen to carbon monoxide in the synthesis gas inside the gasification furnace, and a CO2 sensor that detects carbon dioxide inside the gasification furnace, etc. Detection signals of these sensors that make up the gasification furnace sensor group are sent to the control device 13.

[0050] The gasification device 3 may mix the synthesis gas produced by the gasification reactions and their reverse reactions shown in the above formulas (1-1) to (1-8) with hydrogen supplied from the hydrogen production device 10 described below, to adjust the H2 / CO ratio of the synthesis gas to a predetermined target ratio corresponding to the liquid fuel to be produced (for example, when producing methanol, the target H2 / CO ratio is 2), and then supply this synthesis gas to the FT device 4.

[0051] The hydrogen production device 10 includes an electrolysis device (not shown) and generates hydrogen using electric power. The device for generating hydrogen using electricity is not particularly limited, and any known device can be used, such as a device that generates hydrogen by electrolysis of water. The hydrogen tank 12 stores the hydrogen produced by the hydrogen production device 10. The hydrogen is supplied from the hydrogen tank 12 to the gasification device 3. There are no particular limitations on the hydrogen tank, and any known tank can be used. For example, a pressure-resistant tank can be used. The hydrogen tank may be made of metal or resin.

[0052] A hydrogen filling pump (not shown) may be provided between the hydrogen production device 10 and the hydrogen tank 12. The hydrogen filling pump compresses hydrogen produced by the electrolysis device and fills it into the hydrogen tank 12. The amount of hydrogen filled by the hydrogen filling pump is controlled by the control device 13. The hydrogen tank 12 stores the hydrogen compressed by the hydrogen filling pump. A pressure sensor detects the internal tank pressure of the hydrogen tank 12 and transmits a detection signal to the control device 13. The remaining amount of hydrogen in the hydrogen tank 12 is calculated by the control device 13 based on the detection signal from the pressure sensor. Therefore, in this embodiment, a hydrogen remaining amount acquisition device (not shown) that acquires the remaining amount of hydrogen in the hydrogen tank 12 is composed of the pressure sensor and the control device 13.

[0053] The system may have a hydrogen supply pump (not shown) as hydrogen supply means for supplying hydrogen from the hydrogen tank 12 to the gasification apparatus 3. The hydrogen supply pump supplies hydrogen stored in the hydrogen tank 12 into the gasification furnace of the gasification apparatus 3. The amount of hydrogen supplied from the hydrogen supply pump into the gasification furnace is controlled by the control device 13. Note that, in the fuel production system 1 according to this embodiment, a case is described in which hydrogen stored in the hydrogen tank 12 is supplied into the gasification furnace by the hydrogen supply pump, but the present invention is not limited to this. The hydrogen stored in the hydrogen tank 12 may be supplied upstream of the gasification furnace, more specifically, into the raw material supply path for the biomass raw material.

[0054] The control device 13 is a computer that controls the amount of steam supplied by the steam supply device, the amount of heat input by the heating device, the amount of hydrogen produced by the electrolysis device, the amount of hydrogen filled by the hydrogen filling pump, and the amount of hydrogen supplied by the hydrogen supply pump, based on detection signals from the gasification furnace sensors and detection signals from the pressure sensor of the hydrogen tank 12, etc. The gasification furnace may further include a hydrogen gas supply control means (1) for supplying hydrogen stored in the hydrogen tank to the gasification device when the temperature inside the gasification furnace is 700°C or higher and lower than 850°C. The system may be provided with a hydrogen gas supply control means (2) that supplies hydrogen stored in the hydrogen tank to the gasification system when the amount of hydrogen gas that can be supplied to the gasification system is 100 L / day or more. The gasification system may further include a steam supply control means for stopping the supply of steam from the steam supply means to the gasification system when the temperature of the steam is less than 500°C. Alternatively, the gasification apparatus may be provided with a steam supply control means that supplies steam from the steam supply means to the gasification apparatus when the temperature of the steam is less than 500°C so that the mass ratio expressed as [mass of steam] / [mass of biomass] is 1.0 or less. When the gasification rate of the biomass feedstock is 50 mol % or more, it is preferable to provide a liquid fuel synthesis gas supply means for using the synthesis gas as a feedstock for liquid fuel. When the gasification rate of the biomass feedstock is less than 50 mol %, it is preferable to provide a heat source synthesis gas supply means for using the synthesis gas as a heat source for the gasification furnace.

[0055] A specific procedure for controlling the amount of hydrogen supply and the like by the control device 13 will be described. The control device 13 calculates the optimal operating point of the gasifier based on the detection signals from the gasifier sensors. Here, the operating point of the gasifier includes the amount of biomass material supplied by the biomass material supply device, the amount of steam supplied by the steam supply device, the amount of hydrogen supplied by the hydrogen supply pump, and the amount of heat input by the heating device. The optimal operating point refers to an operating point where the H2 / CO ratio of the synthesis gas discharged from the gasifier becomes a target ratio. The control device 13 stores a basic map that associates the detection signals from the gasifier sensors with the optimal operating point, and the control device 13 calculates the optimal operating point by searching the basic map based on the detection signals from the gasifier sensors. Specifically, a map correlating the biomass supply amount, steam supply amount, and hydrogen supply amount with the synthesis gas production amount is stored in the control device 13. Using the procedure described above, the control device 13 calculates the biomass supply amount, steam supply amount, and hydrogen supply amount that minimize the carbon dioxide emission intensity of the liquid fuel based on the map.

[0056] The optimal operating point of the gasifier varies depending on the type and properties of the biomass material fed into the gasifier. For this reason, different basic maps are stored in the control device 13 for each type and property of the biomass material, and it is preferable to calculate the optimal operating point by switching the basic map to be referenced depending on the type and properties of the biomass material fed into the gasifier. This allows the control device 13 to change the amount of hydrogen supplied by the hydrogen supply pump depending on the type and properties of the biomass material fed into the gasifier, and adjust the H2 / CO ratio of the synthesis gas discharged from the gasifier to a target ratio. In addition, in this embodiment, the case where the optimal operating point is calculated based on the basic map has been described, but the present invention is not limited to this. The optimal operating point may be calculated by performing a predetermined calculation based on the detection signals of the gasification furnace sensors and the type and properties of the biomass material fed into the gasification furnace.

[0057] The control device 13 controls the amount of biomass raw material supplied by the biomass raw material supply device, the amount of steam supplied by the steam supply device, the amount of hydrogen supplied by the hydrogen supply pump, and the amount of heat input by the heating device so as to achieve the calculated optimal operating point.

[0058] In addition, when maintaining the remaining amount of hydrogen in the hydrogen tank 12 within a normal range so that it does not fluctuate significantly, it is preferable that the control device 13 adjusts the amount of hydrogen produced by the hydrogen production device and the amount of hydrogen filled into the hydrogen tank 12 so that they are equal to the amount of hydrogen supplied by the hydrogen supply pump.

[0059] In the fuel production system 1, hydrogen extracted from the hydrogen tank 12 is supplied to the gasification device 3, while hydrogen produced by the electrolysis device is filled into the hydrogen tank 12. Therefore, as a means for reducing the remaining amount of hydrogen, the control device 13 can selectively execute either a hydrogen usage amount increase control, which reduces the remaining amount of hydrogen by increasing the amount of hydrogen used in the gasification device 3 and the amount of hydrogen supplied by the hydrogen supply pump, or a hydrogen production amount decrease control, which reduces the remaining amount of hydrogen by decreasing the amount of hydrogen produced by the hydrogen production device and the amount of hydrogen filled by the hydrogen filling pump.

[0060] The control device 13 reduces the H2 / CO ratio of the synthesis gas produced by the reaction in the gasification furnace by changing the operation point from the optimum operation point during execution of the normal control process.

[0061] The control device 13 is capable of performing either or a combination of a furnace temperature reduction process that reduces the temperature of the gasification furnace and a water reduction process that reduces the amount of steam supplied to the gasification furnace as a means of reducing the H2 / CO ratio of the synthesis gas.

[0062] 3 is a diagram showing the configuration of a fuel production system 11 according to another embodiment. The configuration is the same as that shown in FIG. 2, except that the order of the fractionator (L) 8 and the hydrocracker 7 is reversed and a hydrorefining unit 17 is provided downstream of the fractionator (L) 8.

[0063] Next, with reference to FIGS. 4 and 5, the effects of supplying hydrogen into the gasification furnace or the raw material supply path of the gasification apparatus 3 will be described.

[0064] Figure 4 shows the relationship between the concentration [vol %] of each component of the synthesis gas in the gasifier and the amount of hydrogen supplied [kg / h] to the gasifier. The results shown in Figure 4 were obtained by performing a simulation under specified conditions. In Figure 4, the thick solid line indicates the hydrogen concentration of the synthesis gas in the gasifier, the thick dashed line indicates the carbon monoxide concentration of the synthesis gas in the gasifier, and the thin solid line indicates the carbon dioxide concentration of the synthesis gas in the gasifier. Also in Figure 4, the thick dashed line indicates the amount of carbon dioxide [kg / h] produced by the entire system when a predetermined amount of synthesis gas with a predetermined target ratio is produced by the gasifier 3.

[0065] 5 is a diagram comparing the amount of carbon dioxide [kg / h] and its breakdown generated in the entire system when a predetermined amount of synthesis gas with a predetermined target ratio is produced, between a conventional fuel production system and the fuel production system 1 according to this embodiment. Here, the conventional fuel production system refers to one in which the H2 / CO ratio of the synthesis gas produced by the gasification apparatus 3 is adjusted to the target ratio using water, without supplying hydrogen to the gasification apparatus 3 from the outside.

[0066] As shown in Figure 4, when the amount of hydrogen supplied to the gasifier is set to 0, the H2 / CO ratio of the synthesis gas in the gasifier is lower than the target ratio. Therefore, in order to increase the H2 / CO ratio of the synthesis gas generated by the gasifier 3 to the target ratio, an H2 / CO ratio adjustment process must be performed in which the excess carbon monoxide in the synthesis gas generated in the gasifier is reacted with water to increase the H2 / CO ratio. However, performing this H2 / CO ratio adjustment process generates carbon dioxide. For this reason, in conventional fuel production systems, carbon dioxide is generated not only in the gasification process in the gasifier but also in the H2 / CO ratio adjustment process, as shown in Figure 5.

[0067] In contrast, as shown by dashed line 2a in Figure 4, increasing the amount of hydrogen supplied to the gasifier increases the hydrogen concentration of the synthesis gas in the gasifier. Therefore, by controlling the amount of hydrogen supplied to the gasifier to a predetermined amount, the H2 / CO ratio of the synthesis gas in the gasifier can be adjusted to a target ratio. Therefore, with the fuel production system 1 according to this embodiment, there is no need to actively perform the H2 / CO ratio adjustment process, and therefore the amount of carbon dioxide can be reduced at least by that amount compared to conventional fuel production systems.

[0068] Furthermore, by increasing the amount of hydrogen supplied to the gasifier, the amount of steam supplied to the gasifier can be reduced compared to conventional fuel production systems. As a result, the reactions in the gasifier that generate carbon monoxide and carbon dioxide, as shown in the above formulas (1-1) to (1-8), can be suppressed. Therefore, as shown in FIG. 4, as the amount of hydrogen supplied to the gasifier increases, the carbon monoxide and carbon dioxide concentrations in the synthesis gas in the gasifier decrease. Therefore, as shown in FIG. 5, the fuel production system 1 according to this embodiment can reduce the amount of carbon dioxide generated in the gasification process in the gasifier compared to conventional fuel production systems. As described above, the fuel production system 1 according to this embodiment can suppress the amount of carbon dioxide generated throughout the entire fuel production system 1.

[0069] Fig. 6 is a diagram showing various thresholds set for the remaining amount of hydrogen in the hydrogen tank 12, and is a diagram for explaining the concept of the synthesis gas production process shown in Figs. 7 and 8. The normal range in Fig. 6 is, for example, a range in which the supply amount of hydrogen gas to the gasification device can be maintained between 100 L / day and 300 L / day. The upper limit hydrogen amount in Figure 6 corresponds to the upper limit of the amount of hydrogen that can be stored in the hydrogen tank 12. Therefore, the hydrogen tank 12 cannot be filled with hydrogen exceeding the upper limit hydrogen amount. The lower limit hydrogen amount in Figure 6 corresponds to the minimum amount of hydrogen that must be secured in the hydrogen tank 12 in order for the hydrogen supply pump to supply the hydrogen in the hydrogen tank 12 to the gasification furnace. Therefore, if the remaining amount of hydrogen falls below the lower limit hydrogen amount, hydrogen cannot be supplied to the gasification furnace by the hydrogen supply pump.

[0070] In the synthesis gas production process, an upper threshold for the remaining hydrogen amount is set, which is slightly smaller than the upper limit amount of hydrogen, and a lower threshold that is smaller than this upper threshold and slightly larger than the lower limit amount of hydrogen, and the gasification device 3 and hydrogen production device 10 are controlled so that the remaining hydrogen amount in the hydrogen tank 12 is maintained as much as possible within the normal range between these upper and lower thresholds, in other words, so that the remaining hydrogen amount does not deviate from the normal range and reach the upper or lower limit amount of hydrogen.

[0071] FIG. 7 is a flowchart showing a specific procedure of the normal control process. First, the control device 13 confirms that the temperature of the gasifier is in a normal state, that is, 850° C. or higher, based on the detection signal of the temperature sensor. Next, the control device 13 determines whether the temperature of the water vapor is 500°C or higher based on the detection signal of the temperature sensor. If the result of this determination is YES, the control device 13 further calculates the remaining amount of hydrogen in the hydrogen tank 12 based on the detection signal of the pressure sensor, and determines whether this remaining amount of hydrogen is equal to or higher than an upper threshold. If the result of this determination is YES, the control device 13 supplies both water vapor and hydrogen gas to produce synthesis gas, and if the result is NO, the control device 13 produces synthesis gas by supplying water vapor to the biomass raw material without supplying hydrogen gas. On the other hand, if the determination as to whether the temperature of the steam is 500°C or higher is NO, the control device 13 further calculates the remaining amount of hydrogen in the hydrogen tank 12 based on the detection signal of the pressure sensor and determines whether this remaining amount of hydrogen is equal to or greater than the upper threshold. If the determination result is YES, the control device 13 produces synthesis gas by supplying only hydrogen gas to the biomass raw material without supplying steam, and if the determination result is NO, synthesis gas is not produced.

[0072] If the result of the determination of the remaining hydrogen amount is NO, i.e., if the remaining hydrogen amount in the hydrogen tank 12 is within the normal range, it can be said that there is room to accept the hydrogen generated by the electrolysis device and to supply the amount of hydrogen required in the gasification furnace. For example, this is a state in which the amount of hydrogen gas supplied to the gasification device is less than 100 L / day.

[0073] If the remaining amount of hydrogen in the hydrogen tank 12 is equal to or greater than the upper threshold, the control device 13 increases the amount of hydrogen supplied as a raw material for synthesis gas production. As shown in Figure 6, when the remaining amount of hydrogen is equal to or greater than the upper threshold, it is necessary to reduce the remaining amount of hydrogen so that it does not exceed the upper hydrogen limit. As described above, if the remaining amount of hydrogen exceeds the upper hydrogen limit, it will no longer be possible to fill the hydrogen tank 12 with hydrogen. For this reason, the control device 13 reduces the remaining amount of hydrogen by increasing the amount of hydrogen supplied as a raw material for synthesis gas production.

[0074] When the remaining amount of hydrogen in the hydrogen tank 12 is below the lower threshold, the control device 13 does not increase the supply of hydrogen as a raw material for synthesis gas production or does not produce synthesis gas. As shown in FIG. 6 , when the remaining amount of hydrogen is below the lower threshold, it is necessary to increase the remaining amount of hydrogen so that it does not fall below the lower hydrogen limit. However, this increases energy consumption because the hydrogen production device must be operated to supply hydrogen. Furthermore, the hydrogen production device produces high-purity, high-pressure hydrogen to supply hydrogen to the FT unit, hydrocracker, hydrorefining unit, etc. Therefore, supplying high-purity, high-pressure hydrogen as a raw material for synthesis gas production is energy inefficient. Furthermore, as described above, when the remaining amount of hydrogen falls below the lower hydrogen limit, the hydrogen supply pump cannot supply hydrogen to the FT unit, hydrocracker, hydrorefining unit, etc. Therefore, when the remaining amount of hydrogen in the hydrogen tank 12 is below the lower threshold, the control device 13 does not increase the supply of hydrogen as a raw material for synthesis gas production or does not produce synthesis gas.

[0075] The synthesis gas conversion rate is calculated from the amount of substance of the synthesis gas obtained and the amount of biomass feedstock supplied, and it is determined whether it is 50 mol% or more. If the result of this determination is YES, the synthesis gas is supplied to the subsequent FT unit to proceed with fuel production. On the other hand, if the result is NO, the synthesis gas is burned as fuel to heat the gasification furnace of the synthesis gas unit. The gasification rate is calculated using the following formula. Gasification rate (mol%) = [amount of carbon-containing gases (CO, CO2, CH4, C2H4, etc.) contained in the synthesis gas] / [amount of carbon components in the biomass raw material] x 100

[0076] As described above, in the synthesis gas production process shown in Figure 7, when the remaining hydrogen amount is equal to or greater than the upper threshold, the supply amount of hydrogen as a raw material for synthesis gas production is increased, and when the remaining hydrogen amount is less than the lower threshold, the supply amount of hydrogen as a raw material for synthesis gas production is not increased, or synthesis gas production is not performed, so that the remaining hydrogen amount is maintained within a normal range.

[0077] FIG. 8 is a flowchart showing a specific procedure for low-temperature operation. First, the control device 13 determines whether the temperature of the gasifier is in a low temperature state, that is, whether it is equal to or higher than 700°C and lower than 850°C, based on the detection signal from the temperature sensor. If the result of this determination is NO because the temperature of the gasifier is lower than 700°C, synthesis gas is not produced. If the result of this determination is YES, the subsequent flow is the same as the normal control process in FIG. 7.

[0078] As described above, in the synthesis gas production process shown in Figure 8, similar to the synthesis gas production process shown in Figure 7, when the remaining hydrogen amount is equal to or greater than the upper threshold, the supply amount of hydrogen as a raw material for synthesis gas production is increased, and when the remaining hydrogen amount is less than the lower threshold, the supply amount of hydrogen as a raw material for synthesis gas production is not increased, or synthesis gas production is not performed, so that the remaining hydrogen amount is maintained within a normal range.

[0079] The effects of the present invention during low-temperature operation will now be described. Figure 9 shows the relationship between the concentration of each component in the synthesis gas generated in the gasifier and the temperature of the gasifier when the amount of hydrogen supplied from outside the gasifier is set to 0. As shown in Figure 9, lowering the temperature of the gasifier increases the proportion of carbon monoxide in the synthesis gas, while decreasing the proportions of hydrogen and carbon dioxide in the synthesis gas. In other words, lowering the temperature of the gasifier decreases the H2 / CO ratio of the synthesis gas generated by the reaction in the gasifier. Taking advantage of this, in the furnace temperature reduction process, the control device 13 forcibly lowers the temperature of the gasifier by reducing the amount of heat input by the heating device relative to the optimal operating point determined in the normal control process, thereby reducing the H2 / CO ratio generated by the reaction in the gasifier.

[0080] As shown in Figure 9, lowering the temperature of the gasifier reduces the proportion of carbon dioxide in the synthesis gas. Furthermore, reducing the amount of heat input by the heating device also reduces the amount of energy consumed by the heating device, so the amount of carbon dioxide produced in the gasification device 3 can be reduced.

[0081] The effects of the present invention when there is no or little water vapor supply will be described below. As shown in the above formulas (1-1) to (1-8), reducing the amount of water supplied to the gasifier reduces the proportion of hydrogen in the synthesis gas. Taking advantage of this, in the water reduction process, the control device 13 reduces the amount of steam supplied by the steam supply device relative to the optimal operating point determined in the normal control process, thereby reducing the H2 / CO ratio generated by the reaction in the gasifier. Reducing the amount of steam supplied to the gasifier also reduces the latent heat of water and the amount of heat input by the heating device. Therefore, the control device 13 may maintain a constant temperature in the gasifier by reducing the amount of steam supplied by the steam supply device and the amount of heat input by the heating device.

[0082] As shown in the above formulas (1-1) to (1-8), reducing the amount of steam supplied to the gasifier reduces the proportion of carbon dioxide in the synthesis gas. Furthermore, reducing the amount of heat input by the heating device also reduces the amount of energy consumed by the heating device, thereby reducing the amount of carbon dioxide produced in the gasification device 3.

[0083] The effects of the present invention achieved by increasing the amount of hydrogen supplied will be described below. By increasing the amount of hydrogen supplied, the reactions represented by the above formulas (1-3) and (1-5) to (1-7) using hydrogen as a raw material are more likely to proceed, and the content of hydrocarbon gas tends to increase. As a result, the obtained synthesis gas can be used as fuel to heat the gasification furnace, or the synthesis gas can be supplied to FT synthesis and used as a raw material for fuel production. In other words, hydrogen can be used effectively by using it as a raw material rather than as a fuel itself. Furthermore, by supplying hydrogen, there is no need to actively supply steam into the gasification furnace, which improves energy efficiency. Furthermore, increasing the amount of hydrogen supplied tends to reduce the carbon dioxide content in the synthesis gas, which reduces the amount of carbon dioxide generated in the entire fuel production system.

[0084] Although one embodiment of the present invention has been described above, the present invention is not limited to this, and the detailed configuration may be modified as appropriate within the scope of the spirit of the present invention. [Example]

[0085] The present invention will be explained in more detail below with reference to examples, but the present invention is not limited to the following examples.

[0086] <Example 1> A gasifier reaction tube with a diameter of 90 mm and a length of 1100 mm was used. The biomass feedstock was supplied at a rate of 0.5 g / min and the gasifier temperature was 850°C to produce synthesis gas. Steam was supplied so that the mass ratio (H / B ratio) of [mass of steam] / [mass of biomass feedstock] was 1.0, and the hydrogen supply rate was adjusted so that the mass ratio (H / B ratio) of [mass of hydrogen] / [mass of biomass feedstock] was 0, 0.01, 0.02, 0.03, and 0.04, respectively. The gasification efficiency for each hydrogen supply rate was calculated. The results are shown in Figure 10.

[0087] As shown in Figure 10, the gasification rate increased by up to 13 mol% by supplying hydrogen so that the H / B ratio was in the range of 0.01 to 0.04. Furthermore, it was found that even when the amount of water vapor supplied was small, an improvement in the gasification rate was observed by increasing the amount of hydrogen supplied.

[0088] <Example 2> Synthesis gas was produced in the same manner as in Example 1, except that steam was supplied so that the mass ratios (hereinafter also referred to as S / B ratios) expressed as [mass of steam] / [mass of biomass feedstock] were 0.5 and 1, respectively, and the amount of hydrogen supplied was adjusted so that the mass ratios expressed as [mass of hydrogen] / [mass of biomass feedstock] were 0 and 0.01, respectively. The gasification efficiency for each amount of hydrogen supplied was calculated. The results are shown in Figure 11.

[0089] As shown in Figure 11, when the S / B ratio was 0.5 and the H / B ratio was 0.01, the gasification rate increased by up to 13 mol% compared to when the S / B ratio was 1.0 and the H / B ratio was 0. Furthermore, it was found that even when the amount of water vapor supplied was small, an improvement in the gasification rate was observed by increasing the amount of hydrogen supplied.

[0090] <Example 3> The gasification furnace reaction tube was 30 mm in diameter and 600 mm in length. The biomass feed rate was 0.5 g / min, the gasification furnace temperature was 850°C, and the hydrogen feed rate was adjusted so that the mass ratio (mass of hydrogen / mass of biomass feed) was 0, 0.02, and 0.04, respectively, to produce synthesis gas. The gasification efficiency was calculated for each hydrogen feed rate with and without steam supply. The results are shown in Figure 12.

[0091] As shown in Figure 12, when comparing the cases where steam is supplied and where it is not supplied, it was confirmed that the gasification rate is improved when steam is not supplied. Furthermore, it was found that even when steam is not supplied, the gasification rate can be improved by increasing the amount of hydrogen supplied.

[0092] FIG. 13 is a graph showing the change in temperature inside the gasification furnace when steam was supplied in Example 3, and FIG. 14 is a graph showing the change in temperature inside the gasification furnace when steam was not supplied in Example 3. Comparing Figures 13 and 14, it can be seen that the temperature changes are completely different, and therefore it was found that the type of reaction that occurs preferentially among the reactions of the above formulas (1-1) to (1-8) is different when steam is supplied and when steam is not supplied. Specifically, the content of hydrocarbons in the synthesis gas produced was 3 mol% higher when steam was not supplied than when steam was supplied. This also shows that the type of reaction in gasification is different when steam was supplied and when steam was not supplied.

[0093] <Example 4> Synthesis gas was produced in the same manner as in Example 3, except that the temperature of the gasifier was 700°C, the amount of hydrogen supplied was adjusted so that the mass ratios expressed as [mass of hydrogen] / [mass of biomass feedstock] were 0, 0.02, and 0.04, respectively, and steam was not supplied. The gasification efficiency for each amount of hydrogen supplied was calculated. The results are shown in Figure 15.

[0094] As shown in Figure 15, it was confirmed that the gasification rate was improved by supplying hydrogen even under relatively low temperature conditions and without supplying steam. Furthermore, it was found that even without supplying steam, the gasification rate was improved when the H / B ratio was within a specific range. [Explanation of symbols]

[0095] 1, 11 Fuel production system 2. Biomass raw material supply device 3 Gasifier 4 Gas purification equipment 5. Gas pressure generator 6. Fischer-Tropsch Unit (FT Unit) 7 Hydrocracker 8 Fractionation equipment 9. Steam supply device 10 Hydrogen production equipment 12 Hydrogen Tank 17 Hydrotreating Unit

Claims

1. A method for producing synthesis gas for producing fuel from biomass feedstock, comprising: supplying hydrogen to the biomass feedstock so that the mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; A method for producing synthesis gas that does not include a step of supplying steam.

2. A method for producing synthesis gas for producing fuel from biomass feedstock, comprising: supplying hydrogen to the biomass feedstock so that the mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; A method for producing a synthesis gas, comprising: supplying water vapor to a biomass feedstock so that a mass ratio expressed as [mass of water vapor] / [mass of biomass] is 1.0 or less.

3. The method for producing a synthesis gas according to claim 1 or 2, wherein the gasification of the biomass feedstock is carried out at a temperature of 700°C or higher and lower than 850°C.

4. The method for producing a synthesis gas according to claim 1 or 2, wherein the supply amount of the hydrogen gas is 100 L / day or more.

5. A fuel production system for producing liquid fuel from biomass feedstock, a gasification apparatus including a gasification furnace that reacts a biomass feedstock, hydrogen, carbon monoxide, and carbon dioxide to produce a synthesis gas containing hydrocarbons by the synthesis gas production method according to claim 1; a hydrogen supply means for supplying hydrogen to the gasification apparatus so that the mass ratio expressed as [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; Equipped with A fuel production system comprising: a steam supply control means for stopping the supply of steam from a steam supply means that supplies steam to the gasification apparatus.

6. A fuel production system for producing liquid fuel from biomass feedstock, a gasification apparatus including a gasification furnace that reacts a biomass feedstock, hydrogen, carbon monoxide, and carbon dioxide to produce a synthesis gas containing hydrocarbons by the synthesis gas production method according to claim 2; a hydrogen supply means for supplying hydrogen to the gasification apparatus so that the mass ratio represented by [mass of hydrogen gas] / [mass of biomass] is 0.01 to 0.03; Equipped with A fuel production system comprising: a steam supply control means for supplying steam from a steam supply means that supplies steam to the gasification apparatus so that a mass ratio expressed as [mass of steam] / [mass of biomass] is 1.0 or less.

7. 7. The fuel production system according to claim 5, further comprising a hydrogen gas supply control means (1) for supplying hydrogen to the gasification device when the temperature inside the gasification furnace is 700°C or higher and lower than 850°C.

8. 7. The fuel production system according to claim 5, further comprising a hydrogen gas supply control means (2) that supplies hydrogen to the gasification apparatus when the supply amount of the hydrogen gas that can be supplied to the gasification apparatus is 100 L / day or more.

9. a synthesis gas supply means for supplying synthesis gas for liquid fuel, for using the synthesis gas as a liquid fuel raw material when the gasification rate of the biomass raw material is 50 mol % or more; 7. The fuel production system according to claim 5, further comprising: a heat source synthesis gas supply means for using the synthesis gas as a heat source for the gasification furnace when the gasification rate of the biomass feedstock is less than 50 mol%.

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