Method for producing bioaviation fuel and apparatus for producing bioaviation fuel

Abstract

The present invention provides a method for producing bioaviation fuel and a bioaviation fuel production apparatus that can economically and stably produce char and reformed gas using biomass, and subsequently efficiently produce ethanol and bioaviation fuel. [Solution] A carbonization process that carbonizes biomass to produce carbonized material, A reforming gasification step is performed to carry out a mixed gasification reaction of the carbide with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide. An ethanol production step in which the reformed gas is brought into contact with a C2 oxygenation catalyst and a hydrogenation catalyst to produce ethanol; an ethylene production step in which ethylene is produced in a dehydration reaction step of the ethanol; and an oligomerization reaction step of the ethylene. A method for producing bio-aviation fuel, comprising a mixing step of mixing a metal-containing residue generated together with the reformed gas in the reformed gasification step with the biomass.

Description

【Technical Field】 【0001】 The present invention relates to a method for producing bioaviation fuel and an apparatus for producing bioaviation fuel. 【Background Art】 【0002】 Generally, biomass is a substance derived from organisms that can be used as an energy source or industrial raw material. Biomass includes, for example, thinned wood, rice straw, agricultural products such as bagasse (residue after sugarcane juice extraction), processed products such as food, cotton cloth, clothing fibers, furniture, etc. manufactured from them, construction waste, etc., household waste, organic waste such as sewage sludge and peat. Since biomass is cyclically generated by the action of solar energy, air, water, carbon dioxide gas, soil, etc., it is an infinitely renewable neutral carbon substance. 【0003】 Fermentation methods of bioethanol using food biomass such as rice, corn, sugarcane, and taro as raw materials, production technologies of bioethanol, production systems of bioethanol, etc. have been developed. On the other hand, a method for producing bioethanol using non-food biomass raw materials such as thinned wood and agricultural / industrial waste is useful as a technology for reducing the volume and recycling of agricultural / industrial waste. Currently, the development of production technologies for bioethanol that expand the range of raw material selection is desired. In addition, technological development related to the production of olefins using methanol and ethanol and the production of bioaviation fuel using the oligomerization reaction of the olefins is being studied. 【0004】 Conventionally, as a method for converting non-food biomass into bioethanol, a hydrothermal decomposition method of biomass is known. The hydrothermal decomposition method of biomass is a method of extracting sugar components in the presence of acid or alkali and fermenting the obtained sugar components to obtain bioethanol. The hydrothermal decomposition method of biomass has technical and economic problems related to the production of bioethanol, such as low yield of bioethanol and high production cost. 【0005】 On the other hand, technologies for gasifying biomass have been proposed. One such technology involves directly gasifying biomass using air and steam in a fixed-bed or fluidized-bed gasifier, for example, through a thermochemical gasification reaction. Another technology involves gasifying char obtained from the thermal decomposition of biomass with steam. The gas produced by biomass gasification technology (hereinafter sometimes referred to as "biomass gas" or "reformed gas") is used in gas engine power generation, hydrogen production, production of alcohol fuels such as methanol and ethanol, and synthetic fuels such as Fischer-Tropsch (FT) synthetic oil (see Patent Documents 1-4 and Non-Patent Documents 1-3). [Prior art documents] [Patent Documents] 【0006】 [Patent Document 1] Japanese Patent Publication No. 2008-88434 [Patent Document 2] Patent No. 5342664 [Patent Document 3] International Publication No. 2020 / 166659 [Patent Document 4] International Publication No. 2010 / 092819 [Non-patent literature] 【0007】 [Non-Patent Document 1] Kenichi Sasauchi, "Power Generation Utilization through Pyrolysis Gasification of Biomass," Journal of the Combustion Society of Japan, Vol. 47, No. 139 (2005), pp. 31-39. [Non-Patent Document 2] Masaru Ichikawa (supervisor), "New Developments in Biomass Refinery Catalyst Technology," CMC Publishing (2011), pp. 70-89. [Non-Patent Document 3] Masaru Ichikawa, "New Developments in Hydrogen Energy Technology Utilizing Biomass Resources," Life and Environment, Vol. 61, No. 1 (2016). [Overview of the project] [Problems that the invention aims to solve] 【0008】 However, conventional biomass pyrolysis and carbonization technologies have problems such as low carbonization rates due to inefficient and uniform carbonization of biomass, low yield of reformed gas in the gasification of carbonized material, and inability to efficiently and stably obtain ethanol and bioaviation fuel in the production process of ethanol and bioaviation fuel using the reformed gas. 【0009】 The present invention has been made in view of the above-mentioned problems, and aims to provide a method for producing bioaviation fuel and a bioaviation fuel production apparatus that can improve the carbonization rate of carbides obtained in a carbonization process using biomass, improve the yield of reformed gas by gasification of carbides, and efficiently and stably produce bioethanol and bioaviation fuel. [Means for solving the problem] 【0010】 The present invention has the following aspects. [1] A method for producing bioaviation fuel, comprising: a carbonization step of carbonizing biomass to produce a carbide; a reforming gasification step of carrying out a mixed gasification reaction of the carbide with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane and carbon dioxide; an ethanol production step of contacting the reformed gas with a C2 oxygenation catalyst and a hydrogenation catalyst to produce ethanol; an ethylene production step of producing ethylene in a dehydration reaction step of the ethanol; an oligomerization reaction step of producing C6-C16 isooligomers in an oligomerization reaction of the ethylene; a hydrogenation step of hydrogenating the isooligomers to produce C6-C16 isoparaffin bioaviation fuel; and a mixing step of mixing a metal-containing residue generated together with the reformed gas in the reforming gasification step with the biomass. 【0011】 [2] The method for producing bio-aviation fuel according to [1], wherein the metal-containing residue comprises at least one element selected from the group consisting of alkali metals, alkaline earth metals, B, Al, Fe, and Ni. 【0012】 [3] A method for producing bio-aviation fuel according to [1] or [2], comprising a shift reaction step in which carbon monoxide and methane, as well as water vapor, contained in the residual gas after separation of a liquid product containing ethanol from the gas produced in the ethanol production step are shift-reacted to produce hydrogen and carbon dioxide. 【0013】 [4] A method for producing bio-aviation fuel according to [3], comprising a supply step of separating and recovering carbon dioxide from a mixed gas of hydrogen and carbon dioxide generated in the shift reaction step, supplying the recovered carbon dioxide to the reforming gasification step, and supplying the hydrogen to the reforming gas. 【0014】 [5] A method for producing bio-aviation fuel according to [3] or [4], wherein in the shift reaction step, a shift reaction catalyst is used which comprises at least one element selected from the group consisting of Fe, Ru, Ni, Cu, Zn, K, Li, Mg, Cr, Co, Mo, Zr, Ti, Ce, La, and Nd, and a porous oxide support. 【0015】 [6] A method for producing bio-aviation fuel according to any one of [1] to [5], wherein the carbonization gas generated together with the carbide in the carbonization step is combusted with air, and the resulting combustion gas is used as a heat source to heat and use at least one of the following steps: the carbonization step, the reforming gasification step, the ethanol production step, the shift reaction step, the ethylene production step, the oligomerization reaction step, and the hydrogenation reaction step. 【0016】 [7] The method for producing bio-aviation fuel according to any one of [1] to [6], wherein the C2 oxygenation catalyst comprises Rh, at least one element selected from the group consisting of Mn, Sc, Li, Na, K, Cs, Mg, Ba, Pt, Pd, Ir, Mo, W, V, Zr, Hf, Ti, Y, Ce, and La, and a porous support. 【0017】 [8] The hydrogenation catalyst includes at least one element selected from the group consisting of Pd, Fe, Ni, Pt, Cu, Cr, Zn, K, Na, Ce, and Ti, and a porous support, and is the method for producing bio-aviation fuel according to any one of [1] to [7]. 【0018】 [9] In the ethanol production step, a composite catalyst prepared by mixing the C2 oxygenated catalyst and the hydrogenation catalyst is used, and the mixing volume ratio (C2 oxygenated catalyst / hydrogenation catalyst) of the C2 oxygenated catalyst to the hydrogenation catalyst in the composite catalyst is 0.1 or more and 5 or less, and is the method for producing bio-aviation fuel according to any one of [1] to [8]. 【0019】

[10] A method for producing bio-aviation fuel, comprising an ethylene production step of producing ethylene by a dehydration reaction of ethanol, an oligomerization reaction step of producing a C6-C16 iso-oligomer using the ethylene, and a hydrogenation step of hydrogenating the C6-C16 iso-oligomer to produce bio-aviation fuel. 【0020】

[11] A biomass aviation fuel production apparatus comprising: a reforming gasification furnace; a biomass supply facility; a biomass supply amount adjustment means; a biomass dryer having means for adjusting and controlling the dryness of the biomass; a carbonization furnace having a temperature increase adjustment means; a carbide supply facility for supplying carbide to the reforming gasification furnace; a carbide supply amount adjustment means for adjusting the supply amount of the carbide to the reforming gasification furnace; a supply facility for supplying steam and carbon dioxide to the reforming gasification furnace; a carbon dioxide supply amount adjustment means for adjusting the supply amounts of the steam and the carbon dioxide to the reforming gasification furnace; a reformed gas supply facility for supplying reformed gas to the reforming gasification furnace; an ethanol production facility for producing ethanol by bringing the reformed gas into contact with a C2 oxygenated catalyst and a hydrogenation catalyst; a separation and recovery means for separating and recovering metal-containing residues generated together with the reformed gas from the reformed gas; a metal residue supply facility for supplying and mixing the recovered metal-containing residues to the biomass; a metal-containing residue supply amount adjustment means for adjusting the supply amount of the metal-containing residues to the biomass; a catalyst mixing and preparation facility for mixing and preparing the C2 oxygenated catalyst and the hydrogenation catalyst in the ethanol production facility; and a catalyst mixing amount adjustment means for adjusting the mixing amount of the C2 oxygenated catalyst with respect to the hydrogenation catalyst. 【0021】

[12] A gas separation facility for separating carbon dioxide from a mixture of hydrogen and carbon dioxide contained in the residual gas after separating the liquid product containing ethanol from the reaction gas produced in the bioethanol production facility; a first piping facility for supplying the carbon dioxide recovered in the gas separation facility to the reforming gasifier; a carbon dioxide supply adjustment means for adjusting the amount of the recovered carbon dioxide supplied to the reforming gasifier; a second piping facility for supplying residual hydrogen remaining in the gas separation facility to a hydrogen holder; a hydrogen supply adjustment means for adjusting the amount of the residual hydrogen supplied to the hydrogen holder; and hydrogen generated in the water electrolysis facility. The bio-aviation fuel production apparatus according to

[10] , comprising: a third piping system for supplying to a hydrogen holder; a hydrogen supply adjustment means for adjusting the amount of hydrogen supplied to the hydrogen holder; a supply system for supplying residual hydrogen and hydrogen from the hydrogen holder to the reforming gasifier; a hydrogen supply adjustment means for adjusting the amount of residual hydrogen and hydrogen supplied to the reforming gasifier; a pressurized and circulating supply system for bringing the reformed gas into contact with a composite catalyst; a reformed gas circulation adjustment means for adjusting the amount of reformed gas circulated to the composite catalyst; and a separation and purification system for separating and purifying ethanol from a liquid product containing ethanol. 【0022】

[13] A bio-aviation fuel production apparatus according to

[11] or

[12] , comprising: a combustion furnace for burning the carbonization gas generated in the carbonization furnace; a heat exchanger for heating steam introduced into the reforming gasification furnace; piping equipment for supplying the combustion gas generated in the combustion furnace as heating gas to at least one of the reforming gasification furnace, the biomass dryer, the carbonization furnace, and the shift reaction equipment; gas temperature adjustment means for adjusting the temperature of the gas; gas flow rate adjustment means for adjusting the flow rate of the gas; ethanol separation and purification equipment for separating and purifying the ethanol; ethylene production equipment for producing ethylene by a dehydration reaction of ethanol; oligomerization reactor for producing C6-C16 isooligomers by an oligomerization reaction of the ethylene; and hydrogenation reactor for producing C6-C16 isoparaffin bio-aviation fuel by hydrogenating the isooligomers. [Effects of the Invention] 【0023】 According to the present invention, it is possible to efficiently produce carbides and reformed gases using biomass, and subsequently produce ethanol and bioaviation fuel economically and stably. This provides a method for producing bioaviation fuel and an apparatus for producing bioaviation fuel. [Brief explanation of the drawing] 【0024】 [Figure 1] This is a schematic diagram of a bioaviation fuel manufacturing apparatus for implementing a bioaviation fuel manufacturing method according to one embodiment of the present invention. [Modes for carrying out the invention] 【0025】 In this specification, “biofeaviation fuel” means aviation fuel produced from biomass. In this specification, “~” indicating a numerical range means that the values ​​before and after it are included as the lower and upper limits. 【0026】 [Biofe-aviation fuel production equipment] Figure 1 is a schematic diagram of a bio-aviation fuel production apparatus for carrying out a bio-aviation fuel production method according to one embodiment of the present invention. The bio-aviation fuel production apparatus 100 of this embodiment includes a biomass supply equipment 91, a biomass dryer 12, a carbonization furnace 20, a reforming gasifier 30, a metal residue supply equipment 37, an ethanol production equipment 50, a catalyst mixing and adjusting equipment 57, a biomass supply amount regulator 80, a carbide supply amount regulator 81, a carbon dioxide supply amount adjusting means 83, a reforming gas supply amount regulator 86, a gas mixing regulator 89, and a pressurized gas circulation supply equipment 88. The system includes a carbide supply unit 92, a reformed gas supply unit 93, a metal-containing residue separator and recoverer 94, a metal-containing residue supply unit 37, a metal-containing residue supply rate regulator 82, a catalyst mixing rate regulator 95, a gas-liquid separator 52, a shift reaction hydrogen production unit 53, a water electrolysis unit 40, a hydrogen supply rate regulator 85, a gas separation unit 54, an ethylene producer 42, an oligomerization reactor 43, a distillation unit 44, and a hydrogenation reactor 45. 【0027】 The biomass receiver 11 is positioned in front of the carbonization furnace 20 and receives biomass 1 from the outside. 【0028】 The biomass dryer 12 has means for adjusting and controlling the degree of dryness of the biomass 1. A rotary kiln dryer can be used as the biomass dryer 12. The rotary kiln dryer dries the biomass 1 in the biomass receiver 11 and feeds it into the carbonization furnace 20. The supply of biomass 1 to the carbonization furnace 20 may be continuous or intermittent. 【0029】 The carbonization furnace 20 carbonizes biomass 1 by a pyrolysis carbonization operation. In the pyrolysis carbonization operation, biomass 1 is heated in a low-oxygen or oxygen-free state to cause thermal decomposition. Carbonized material 2 is produced when biomass 1 is thermally decomposed. In addition, carbonization gases 5 other than carbonized material, such as decomposition gas and tar, are also produced. The carbonization furnace 20 may be equipped with a stirring means for stirring the biomass 1. The stirring means may be a known type such as a turntable type or a screen-moving type. 【0030】 The reforming gasifier 30 gasifies the carbide 2. Specifically, the reforming gasifier 30 produces reformed gas 8 (a mixed gas of H2, CO, CH4, and CO2) through a mixed gasification reaction of the carbide 2 with steam 7 and carbon dioxide 9. The reforming gasifier 30 comprises an inner cylinder 30a and an outer cylinder 30b surrounding the inner cylinder 30a. The carbide 2 is contained within the inner cylinder 30a. Heating gas is supplied to the gap between the inner cylinder 30a and the outer cylinder 30b, heating the inner cylinder 30a, and the heat from the inner cylinder 30a heats the carbide, steam, and CO2, causing the reforming gasification to proceed. 【0031】 A first steam supply pipe 33 is connected to the reforming gasifier 30, which supplies steam via a steam supply rate regulator 84. A carbon dioxide supply pipe 32 is also connected to the reforming gasifier 30 via a carbon dioxide supply rate regulator 83. A dust collector 34 is connected to the reforming gasifier 30 via a first reforming gas pipe 35, which separates and recovers metal-containing residue 3 from the reformed gas 8 discharged from the reforming gasifier 30. 【0032】 The dust collector 34 is connected to a gas purifier 36 that removes sulfur and chlorine-containing components from the reformed gas 8 obtained by separating and removing the metal-containing residue 3 in the metal-containing residue separator and recovery unit 94. 【0033】 The metal residue supply equipment 37 supplies and mixes the metal-containing residue recovered by the separation and recovery means 94 with the biomass 1. The supply of metal-containing residue to the biomass 1 may be continuous or intermittent. Here, the ratio of the supply rate of metal-containing residue (kg / h) to the supply rate of biomass 1 (kg / h) (supply rate of metal-containing residue / supply rate of biomass) is preferably 0.01 or more and 10 or less, more preferably 0.05 or more and 5 or less, and even more preferably 0.1 or more and 1 or less. If the ratio is above the lower limit, the carbonization rate of the char and the reforming gasification rate of the char increase. If the ratio is below the upper limit, the mixing efficiency and uniformity of the mixing between the biomass and the metal-containing residue are better. 【0034】 The ethanol production facility 50 produces bioethanol by contacting reformed gas with a composite catalyst 63, which is a mixture of a C2 oxygenation catalyst 58 and a hydrogenation catalyst 59. The bioethanol production facility 50 is equipped with a C2 oxygenation catalyst and a hydrogenation catalyst. When biomass gas is contacted with the C2 oxygenation catalyst, C2 oxygenated compounds such as acetic acid, acetaldehyde, and ethanol are produced from H2, CO, CO2, and CH4 contained in the biomass gas. Derivatives of C2 oxygenated compounds such as methyl acetate and ethyl acetate may also be produced. Further contact with the hydrogenation catalyst produces ethanol from the C2 oxygenated compounds such as acetic acid, acetaldehyde, methyl acetate, and ethyl acetate, increasing the selectivity for ethanol. In this embodiment, the reformed gas supplied to the bioethanol production facility 50 contains CO, H2, CH4, and CO2. Including CH4 and CO2 improves the bioethanol yield compared to cases where CH4 and CO2 are not included. 【0035】 A C2 oxygenation catalyst is a catalyst that efficiently produces the aforementioned C2 oxygenated compound from reformed gas. The C2 oxygenation catalyst contains Rh, at least one element selected from the group consisting of Mn, Sc, Li, Na, K, Cs, Mg, Ba, Pt, Pd, Ir, Mo, W, V, Zr, Hf, Ti, Y, Ce, and La (hereinafter also referred to as element (1)), and a porous support. The C2 oxygenation catalyst may contain two or more elements (1). The atomic ratio of element (1) to Rh is preferably 0.001 to 10, and more preferably 0.01 to 5. Examples of porous support materials include porous oxides such as silica and alumina. 【0036】 The amount of Rh and element (1) supported is, for example, 0.01% to 10% by mass, preferably 0.1% to 5% by mass. Here, the amount of Rh and element (1) supported is the ratio of the total mass of Rh and element (1) to the mass of the porous carrier. 【0037】 C2 oxygenation catalysts can be produced by known methods. For example, a C2 oxygenation catalyst can be obtained by dissolving a catalyst precursor in a solvent, impregnating a porous support with the resulting solution, and performing an activation treatment. Examples of catalyst precursors include salts of Rh and salts of element (1). Examples of salts include hydrochloride salts, nitrates, formates, acetates, alkoxides, and oxygenates. Examples of solvents include ethanol, methanol, and water. 【0038】 Methods for activation include, for example, gradually increasing the temperature in the 250°C to 600°C range in an oxygen-containing atmosphere, or gradually increasing the temperature in the 100°C to 450°C range in a hydrogen gas atmosphere. In addition, as a hydrogen activation treatment, reduction treatment with reducing agents such as hydrazine or boron hydride may be performed. The selection of catalyst precursors, catalyst manufacturing processes, and activation treatment conditions are not limited to these. 【0039】 When producing a C2 oxygenation catalyst in which Rh is supported on a carrier, a supporting method is recommended in which the Rh solution is applied to a porous carrier such as silica or alumina and then injected and permeated into the pores of the carrier. Preferred Rh solutions used in this process include, for example, rhodium chloride, rhodium nitrate solution, hexaamminerhodium acetate solution, or tetraamminerhodium hydroxylate solution. 【0040】 When producing a C2 oxygenation catalyst in which Rh and element (1) are supported on a porous carrier, element (1) may be included in the Rh solution, or the element (1) solution may be separately applied to the Rh-supported porous carrier. The Rh solution and element (1) solution can also be supported simultaneously or sequentially by methods such as immersion, dropwise addition, coating, or spraying within a predetermined temperature range. 【0041】 In the production of a C2 oxygenation catalyst containing Rh and element (1), it is preferable to use at least one chelating agent selected from the group consisting of oxalic acid, citric acid, tartaric acid, lactic acid, and malic acid. Using a chelating agent improves the ethanol production activity compared to when no chelating agent is used. A method for producing a C2 oxygenation catalyst using a chelating agent includes, for example, impregnating a porous support with an Rh solution and an element (1) solution, drying it, and then impregnating it with a chelating agent solution for activation treatment. 【0042】 The hydrogenation catalyst comprises at least one element selected from the group consisting of Pd, Fe, Ni, Pt, Cu, Cr, Zn, K, Na, Ce, and Ti (hereinafter also referred to as element (2)), and a porous support. The hydrogenation catalyst may contain two or more elements (2). 【0043】 Examples of porous carriers include porous oxides such as silica and alumina. The amount of element (2) supported is, for example, 0.01% to 10% by mass, preferably 0.1% to 5% by mass. Here, the amount of element (2) supported is the ratio of the total mass of element (2) to the mass of the porous carrier. 【0044】 Hydrogenation catalysts can be produced by known methods. For example, a hydrogenation catalyst can be obtained by dissolving a catalyst precursor in a solvent, impregnating a porous support with the resulting solution, and activating it. Examples of catalyst precursors include salts of element (2). Examples of salts include hydrochloride salts, nitrates, oxalates, oxygenates, and organic salts. Examples of solvents include ethanol, methanol, and water. 【0045】 Methods for activation include, for example, gradually increasing the temperature in the 250°C to 600°C range in an oxygen-containing atmosphere, or gradually increasing the temperature in the 100°C to 450°C range in a hydrogen gas atmosphere. In addition, as a hydrogen activation treatment, reduction treatment with reducing agents such as hydrazine or boron hydride may be performed. The selection of catalyst precursors, catalyst manufacturing processes, and activation treatment conditions are not limited to these. 【0046】 The C2 oxygenation catalyst and the hydrogenation catalyst may be arranged separately, but from the viewpoint of ethanol yield and ethanol selectivity, it is preferable to arrange them as a composite catalyst by mixing the C2 oxygenation catalyst and the hydrogenation catalyst. When the C2 oxygenation catalyst and the hydrogenation catalyst are arranged separately, the hydrogenation catalyst is placed downstream of the C2 oxygenation catalyst and comes into contact with the biomass gas after contact with the C2 oxygenation catalyst. 【0047】 In a composite catalyst, the volume ratio of the C2 oxygenation catalyst to the hydrogenation catalyst (C2 oxygenation catalyst / hydrogenation catalyst volume ratio) is preferably 0.1 to 5, and more preferably 0.2 to 2. When the C2 oxygenation catalyst / hydrogenation catalyst volume ratio is above the lower limit of the above range, the yield of C2 oxygenated compounds is better, and when it is below the upper limit of the above range, the ethanol selectivity is better. 【0048】 The ethanol production equipment 50 is connected to a catalyst mixer 57 that prepares a composite catalyst 63 by mixing reformed gas 8 with a C2 oxygenation catalyst 58 and a hydrogenation catalyst 59. 【0049】 The ethanol production facility 50 is connected to a shift reaction hydrogen production facility 53 via a gas-liquid separator 52. The shift reaction hydrogen production facility 53 uses the reaction gas produced in the ethanol production facility 50, and after separating the liquid product containing ethanol in the gas-liquid separator 52, it causes a shift reaction between carbon monoxide and methane contained in the residual reaction gas and water vapor to produce hydrogen and carbon dioxide. 【0050】 The shift reaction hydrogen production facility 53 is connected to the gas separation and purification facility 54 via H2 / CO2 gas piping 64. The hydrogen and carbon dioxide generated in the shift reaction hydrogen production facility 53 are supplied to the gas separation and purification facility 54 via H2 / CO2 gas piping 64. 【0051】 The gas separation and purification unit 54 is connected to the hydrogen holder 55 via a hydrogen supply pipe 79. The carbon dioxide 9 separated and recovered in the gas separation and purification unit 54 is supplied to the reforming gasifier 30 via a carbon dioxide supply pipe 32. The carbon dioxide supply pipe 32 is equipped with a carbon dioxide supply rate regulator 83 that adjusts the amount of carbon dioxide supplied to the reforming gasifier 30. 【0052】 The hydrogen holder 55 is connected to the gas mixing and adjusting unit 89 via a hydrogen supply pipe 78. A hydrogen supply rate regulator 85 is provided in the hydrogen supply pipe 78. The hydrogen supply rate regulator 85 adjusts the amount of hydrogen supplied to the hydrogen holder 55 from the water electrolysis equipment 40. 【0053】 The gas mixing and adjusting unit 89 mixes and adjusts hydrogen from the hydrogen holder 55 into the reformed gas. 【0054】 The booster gas circulation supply equipment 88 pressurizes and circulates reformed gas with an adjusted H2 / CO2 volume ratio. 【0055】 The ethanol separation and purification equipment 56 separates and purifies bioethanol from a liquid product containing ethanol. 【0056】 The ethanol production equipment 50 is connected to a gas-liquid separator 52. The gas-liquid separator 52 is connected to an ethanol separation and purification equipment 56 via crude ethanol piping 77. 【0057】 One end of the steam supply pipe 33 is connected to the bottom of the inner cylinder 30a of the reforming gasifier 30. The other end of the steam supply pipe 33 is connected to the water supply 4 via the heat exchanger 31. A steam supply rate regulator 84 may be installed in the steam supply pipe 33. 【0058】 One end of the carbon dioxide supply pipe 32 is connected to the bottom of the inner cylinder 30a of the reforming gasifier 30. The other end of the carbon dioxide supply pipe 32 is connected to the gas separation equipment 54. A carbon dioxide supply rate regulator 83 is also installed in the carbon dioxide supply pipe 32. An example of the carbon dioxide supply rate regulator 83 is a mass flow controller. The supply of carbon dioxide to the reforming gasifier 30 may be continuous or intermittent. 【0059】 A first reformed gas pipeline 35 is connected to the top of the reformed gasification furnace 30. The first reformed gas pipeline 35 discharges the reformed gas 8 from the gasification furnace 30. The reformed gas 8 is supplied to the gas purifier 36 via the first reformed gas pipeline 35. The reformed gas 8 is connected to the ethanol production equipment 50 via the gas purifier 36, a reformed gas supply rate regulator 86, a gas mixing and adjusting unit 89, and a booster gas circulation unit 88. 【0060】 A dust collector 34 equipped with a means for separating and recovering metal-containing residue is installed in the middle of the first reformed gas piping 35, upstream of the gas purifier 36. Metal-containing residue 3 is discharged from the gasifier 30 along with the reformed gas 8. The dust collector 34 separates the reformed gas 8 from the metal-containing residue 3 and recovers the separated metal-containing residue 3. Since the metal-containing residue 3 contains useful metal elements derived from biomass, the recovered metal-containing residue 3 is fed into the biomass receiver 11 via the metal-containing residue discharge piping 39, the metal-containing residue supply regulator 82, and the metal-containing residue supply equipment 37 to be mixed and prepared with biomass. 【0061】 The gas purifier 36 is installed in the middle of the first reformed gas piping 35. Downstream of the gas purifier 36, a gas mixing and adjusting unit 89 is installed via a reformed gas supply rate regulator 86. 【0062】 Multiple combustion gas pipes supply the combustion gas 6 generated by the air combustor 60 to the following waste heat utilization equipment via the combustion gas pipe 70 and the combustion gas flow regulator 61. The system includes a combustion gas pipe 71 that supplies combustion gas to the biomass dryer 12, a combustion gas pipe 72 that supplies combustion gas to the carbonization furnace, a combustion gas pipe 73 that supplies combustion gas to the reforming gasifier 30, a combustion gas pipe 74 that supplies combustion gas to the steam heat exchanger 31, a combustion gas pipe 75 that supplies combustion gas to the ethanol production equipment 50, and a combustion gas pipe 76 that supplies combustion gas to the shift reaction hydrogen production equipment 53. 【0063】 The biomass supply regulator 80 is installed between the biomass receiver 11 and the biomass dryer 12 and adjusts the amount of biomass 1 supplied to the biomass dryer 12. The biomass supply regulator 80 has a means for measuring moisture content. 【0064】 The carbide supply adjustment device 81 is installed between the carbonization furnace 20 and the reforming gasifier 30, and adjusts the amount of carbide 2 supplied to the reforming gasifier 30. 【0065】 The carbon dioxide supply regulator 83 adjusts the amount of steam and carbon dioxide supplied to the reforming gasifier 30. 【0066】 The reformed gas supply regulator 86 adjusts the amount of reformed gas supplied to the reformed gasification furnace 30. 【0067】 The biomass supply equipment 91 adjusts the amount of biomass 1 supplied to the carbonization furnace 20. 【0068】 The carbide supply equipment 92 adjusts the amount of carbide 2 supplied to the reforming gasifier 30. 【0069】 The supply equipment 93 supplies steam and carbon dioxide to the reforming gasifier 30. 【0070】 The separation and recovery means 94 separates and recovers the metal-containing residue generated together with the reformed gas from the reformed gas. 【0071】 The metal-containing residue supply regulator 95 adjusts the amount of metal-containing residue supplied to the biomass 1. 【0072】 The catalyst mixture regulator 96 adjusts the amount of C2 oxygenated catalyst mixed with the hydrogenation catalyst. 【0073】 The air combustor 60 is connected to the carbonization furnace 20. The air combustor 60 generates high-temperature combustion gas 6 by combusting the pyrolysis gas (dry distillation gas 5) produced in the carbonization furnace 20 with air from the air blower 41. 【0074】 The ethanol separation and purification equipment 56 purifies and concentrates ethanol from the liquid product containing ethanol separated in the gas-liquid separator 52. 【0075】 The ethylene producer 42 produces ethylene through the dehydration reaction of ethanol. 【0076】 The oligomerization reactor 43 produces isooligomers through the oligomerization reaction of ethylene. 【0077】 The distillation apparatus 44 separates and recovers C6-C16 isooligomers in the isooligomer distillation process. The remaining C2-C5 light olefins are recycled and fed into the oligomerization reactor. 【0078】 The hydrogenation reactor 45 hydrogenates C6-C16 isooligomers to produce bio-aviation fuel 47 consisting of C6-C16 isoparaffins. 【0079】 According to the bio-aviation fuel manufacturing method and bio-aviation fuel manufacturing equipment of this embodiment, the carbonization rate of biomass can be increased, and reformed gas can be produced efficiently, and thereafter bioethanol and bio-aviation fuel can be produced economically and stably. 【0080】 [Method of producing bioaviation fuel] The method for producing bio-aviation fuel according to this embodiment includes: a carbonization step of carbonizing biomass to produce carbides; a reforming gasification step of performing a mixed gasification reaction of the carbides with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane and carbon dioxide; an ethanol production step of contacting the reformed gas with a C2 oxygenation catalyst and a hydrogenation catalyst to produce ethanol; an ethylene production step of producing ethylene in a dehydration reaction step of the ethanol; an oligomerization step of producing C6-C16 isooligomers in an oligomerization reaction of the ethylene; a hydrogenation step of hydrogenating the isooligomers to produce bio-aviation fuel consisting of C6-C16 isoparaffins; and a mixing step of separating and recovering a metal-containing residue generated together with the reformed gas in the reforming gasification step, and mixing the metal-containing residue with the biomass. The method for producing bio-aviation fuel according to this embodiment uses a bio-aviation fuel production apparatus 100. 【0081】 [biomass] Examples of biomass (or biomass body) 1 used in this embodiment include forest timber such as cedar, pine, and bamboo; agricultural products and waste by-products (such as bagasse) such as rice straw, sugarcane, napier, and sweet sorghum; and industrial waste such as construction waste, cotton, and textile products. The biomass 1 is preferably a pulverized and dried material obtained by crushing biomass produced or discarded in forestry or agriculture. The dimensions of the pulverized material are, for example, 10 mm to 100 mm. One type of biomass 1 may be used alone, or two or more types may be used in combination. 【0082】 Biomass 1 may contain, in addition to carbon, alkali metals and alkaline earth metals such as Na, K, Li, Cs, Ca, Mg, Ba, B, Al, Fe, and Ni, and may be further added and mixed. In this embodiment, the presence of these metals in biomass 1 is preferable because it can reduce tar formation in the carbonization process, improve the carbonization rate of the char, and generate reformed gas more efficiently in the subsequent reformed gasification process. 【0083】 In this embodiment, in order to include an appropriate amount of metal in the crushed biomass chips, in addition to adjusting the type and amount of biomass, substances such as metal compounds that serve as sources of the aforementioned metals may be mixed with the biomass. As such a metal source, it is preferable to use, for example, the metal-containing residue 3 generated together with the reformed gas 8 in the biomass reforming and gasification process. Such metal-containing residue is the residue separated and recovered from the reformed gas generated in the reforming and gasification process. The metal-containing residue may normally be recovered as solids such as metal oxides, carbides, and metal salts. 【0084】 The timing for mixing the metal source, such as metal-containing residue, with the biomass may be such that a mixing step is provided before the carbonization process, or at least one of the metal-containing residue and the metal source may be directly introduced into the carbonization furnace. When mixing the metal-containing residue 3 and at least one of the metal source before the carbonization process, for example, this can be done by introducing them into a biomass receiver and / or a dryer for drying the biomass. In this embodiment, the supply of metal-containing residue to the biomass may be continuous or intermittent. 【0085】 Methods for mixing metals with biomass include, for example, immersing the biomass in a solution in which a metal source, such as metal-containing residue, is dissolved or dispersed in an acidic or alkaline aqueous solution, alcohol, ethers, or hydrocarbons, or spraying the solution onto the biomass to mix and support the metal components. 【0086】 In the carbonization process of this embodiment, the inclusion of each of the aforementioned metals in the biomass raw material promotes carbonization and increases the carbonization rate. The metal content in the metal-containing residue is typically around 0.01g to 100g, or 0.1g to 50g, per 1kg of metal-containing residue. The mass ratio of metal-containing residue to biomass (metal-containing residue ÷ biomass) can range from 0.01 to 0.99, or from 0.1 to 0.9. 【0087】 In this embodiment, when the metal element content of the metal-containing residue and the mass ratio of the metal-containing residue to biomass are within the aforementioned range, the carbonization rate in the biomass carbonization process tends to improve, and in addition, the tar removal rate tends to be better. The increased carbonization rate makes it possible to increase the amount of carbide produced, the amount of reformed gas produced, and the amount of bioethanol produced. This increases the amount of ethylene produced in the subsequent ethylene production process using ethanol and the amount of bio-aviation fuel produced in the ethylene oligomerization reaction process. In this embodiment, the metal content of the metal-containing residue can be measured by ion chromatography, ICP emission spectrometry, and X-ray fluorescence analysis. 【0088】 [Carbonization process] In the bio-aviation fuel production method of this embodiment, a carbonization step is performed to carbonize biomass 1 to produce carbide 2. In the carbonization step, the biomass raw material is heated in a low-oxygen or oxygen-free state to cause thermal decomposition. By thermally decomposing the biomass, carbide and a carbonization gas containing low-molecular-weight fuel gas and heavy component fuels such as tar are produced. In the bio-aviation fuel production method of this embodiment, the carbonization step is performed using a carbonization furnace 20. 【0089】 As the carbonization furnace, one can be appropriately selected from known carbonization furnaces. Examples include carbonization furnaces equipped with external or internal heating devices, and carbonization furnaces equipped with heating material transfer devices such as screws and rotary furnaces. 【0090】 The carbonization conditions for the carbonization step in the bio-aviation fuel production method of this embodiment are as follows: The heating temperature in the carbonization process is preferably, for example, 200°C to 600°C, and more preferably 250°C to 500°C. The residence time in the carbonization process of the bio-aviation fuel production method of this embodiment is preferably, for example, 5 minutes to 100 minutes, and more preferably 10 minutes to 60 minutes. By thermally decomposing the biomass raw material at the above heating temperature and heating time, carbonized material can be efficiently obtained. 【0091】 In the carbonization step of the bio-aviation fuel manufacturing method of this embodiment, the raw materials may be supplied to the carbonization furnace continuously or intermittently. The metal-containing residue may also be supplied to the carbonization furnace continuously or intermittently. 【0092】 [Air combustion process of carbonized gas] In the bio-aviation fuel production method of this embodiment, the carbonization gas 5 generated together with the carbide in the carbonization process may be separated from the carbide, recovered, and burned to produce a high-temperature combustion gas 6. This combustion gas may be introduced into at least one of the carbonization process, the reforming gasification process described later, and the shift reaction hydrogen production process and used as waste heat gas for heating. Specifically, since the carbonized gas contains hydrogen, lower hydrocarbons, and heavy fuel components such as tar, it is transferred to an air combustion furnace 60 equipped with an air blower, and for example, by combustion in an air atmosphere, a high-temperature (1000°C to 1200°C) combustion gas is obtained from which heavy fuel components such as tar have been removed. This combustion gas can be used as a heat source and transferred through piping equipment to each process of the manufacturing method of this embodiment, or to heating processes such as biomass dryers in other external systems, and used as waste heat gas for heating each process. 【0093】 By using the heat from the combustion gas as waste heat gas and utilizing cascade heat for heating in each step of the bio-aviation fuel production method of this embodiment, heating can be performed without using external fuel (heavy oil, electricity, etc.), or with a smaller amount of combustion gas generated by burning external fuel in air than in conventional methods. 【0094】 The manufacturing process in this embodiment that can utilize such waste heat gas includes, for example, the drying of biomass, the carbonization process (heating of the carbonization furnace 20), the reforming gasification process (heating of the reforming gasifier 30), the bioethanol production process, the steam heat exchanger 31, the shift reaction hydrogen production equipment 53, the ethylene producer 42, the oligomerization reactor 43, and the hydrogenation reactor 45. As a result, in the bio-aviation fuel production method of this embodiment, in addition to the economic effect of reducing the production costs of reformed gas, bioethanol, and bio-aviation fuel, it can also contribute to the reduction of global warming by reducing carbon dioxide emissions. 【0095】 [Reformed Gasification Process] The method for producing bio-aviation fuel according to this embodiment includes a reforming gasification step in which the carbide obtained in the carbonization step is introduced into a connected gasifier, and the carbide is subjected to a cogasification reaction with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide (hereinafter also referred to as H2, CO, CH4, and CO2). 【0096】 In the reforming gasification step of the bio-aviation fuel production method of this embodiment, it is believed that reformed gas is produced by the following reforming gasification reaction between carbide, water vapor, and carbon dioxide. (1) Reaction of carbides with water vapor: [ka] (2) Reaction of carbides with carbon dioxide: [ka] (3) Shift reaction: [ka] (4) Methanation reaction: [ka] 【0097】 In the reforming gasification step of the bio-aviation fuel manufacturing method of this embodiment, the reactions (1) and (2) described above are particularly accelerated by supplying carbon dioxide mixed with water vapor. Therefore, the reformed gas can be produced efficiently, and the amount of reformed gas produced can be increased. By using carbon dioxide mixed with water vapor in the above reaction, it is possible to increase the amount of reformed gas produced by, for example, 1.2 to 2.5 times compared to reforming gas with water vapor alone. 【0098】 In the reforming gasification process of the bio-aviation fuel manufacturing method of this embodiment, water such as tap water 4 is heated to generate steam 7, and this steam can be used. The carbon dioxide 9 used in the reforming gasification process of the bio-aviation fuel manufacturing method of this embodiment may be introduced into the reforming gasifier from a system separate from the bio-aviation fuel manufacturing method of this embodiment, or carbon dioxide emitted from the shift reaction hydrogen production equipment 53, which will be described later, may be introduced into the reforming gasifier 30. 【0099】 In the reforming gasification process of the bio-aviation fuel manufacturing method of this embodiment, the supply of carbide 2 to the reforming gasifier 30 can be appropriately adjusted by the carbide supply rate regulator 81 in order to efficiently produce reformed gas. For example, the supply rate can be between 10 kg / h and 10,000 kg / h, or between 50 kg / h and 5,000 kg / h. The amount of steam supplied to the reforming gas reactor can be appropriately adjusted. 【0100】 For example, the amount of steam supplied per 1 kg / h of carbide supplied may be between 0.5 kg / h and 10 kg / h, or between 2 kg / h and 5 kg / h. The amount of carbon dioxide supplied to the reforming gas reactor can be adjusted as appropriate, but for example, the amount of carbon dioxide supplied per 1 kg / h of carbide supplied may be between 0.1 Nm³ / h and 10 Nm³ / h, or between 0.5 Nm³ / h and 5 Nm³ / h. 【0101】 Furthermore, the ratio of the carbon dioxide supply to the sum of the water vapor supply (carbon dioxide supply ÷ (water vapor supply + carbon dioxide supply)) can be, for example, 1 volume% to 85 volume%, or 10 volume% to 60 volume%, etc. 【0102】 In the reforming gasification step of the bio-aviation fuel manufacturing method of this embodiment, the temperature of the reforming gasifier 30 can be appropriately adjusted to efficiently produce the reformed gas, but for example, it can be 600°C to 1200°C, preferably 800°C to 900°C. As a heating means for the reforming gasifier 30, for example, the combustion gas obtained by burning the above-mentioned carbonization gas may be used as waste heat gas for heating. 【0103】 Steam 7, for example, tap water 4, is heated in a steam heat exchanger 31 to a range of 50°C to 800°C and supplied to the reforming gasification furnace 30. When heating the tap water using a heat exchanger, waste heat gas from the reforming gasification furnace may be introduced into the heat exchanger for heating. Furthermore, the waste heat gas from the heat exchanger 31 that has heated the tap water may be introduced into another process (for example, a bioethanol production facility 50, a shift reaction hydrogen production facility 53, an ethylene production facility 42, and an oligomerization reactor, etc.) and used for heating. 【0104】 The pressure of the reforming gasifier 30 in the reforming gasification process can be adjusted as appropriate, but for example, it can be set to 0.05 MPa or more and 0.5 MPa or less. 【0105】 The reformed gas 8 obtained in the reformed gasification step of the bio-aviation fuel production method of this embodiment contains hydrogen (H2) and carbon monoxide (CO), and typically contains hydrogen (H2), carbon monoxide (CO), methane (CH4), and carbon dioxide (CO2). 【0106】 [Separation and recovery process of metal-containing residue] In this embodiment, the system may also include a separation and recovery process for metal-containing residue, discharge and supply equipment, and supply amount adjustment means for separating and recovering the metal-containing residue generated together with the reformed gas 8 in the reformed gasification process, and supplying the recovered metal-containing residue to the biomass. That is, in the reformed gasification process, the metal contained in the carbide remains as metal-containing residue 3, but the metal-containing residue 3 is separated from the reformed gas 8 and recovered. As a recovery method, for example, the reformed gas containing metal-containing residue discharged from the reformed gasification furnace is separated from the reformed gas and metal-containing residue using a dust collector 34 such as a cyclone and a bag filter, and the separated metal-containing residue is recovered. 【0107】 The metal-containing residue 3 is recycled and supplied to the biomass receiver 11, dryer 12, or the carbonization process before the carbonization process, and is mixed with the biomass as described above. This increases the carbonization rate and the amount of reformed gas produced in the carbonization and gasification processes of the bio-aviation fuel production method of this embodiment. The effect of recycling the metal-containing residue 3 to the biomass 1 to increase the carbonization rate and the amount of reformed gas produced in the biomass may increase with the number of recycling cycles in this embodiment. 【0108】 The metal-containing residue 3 contains at least one element selected from the group consisting of alkali metals and alkaline earth metals such as Na, K, Li, Ca, Mg, and Ba, as well as B, Al, Fe, and Ni, because the metals contained in the biomass 1 are recovered as residues in the gasification process. 【0109】 The reformed gas 8 from which the metal-containing residue 3 has been removed by the separation device is transferred to the bioethanol production process and used for bioethanol production, or it may be used for other purposes, such as hydrogen production and power generation in gasification power generation facilities. 【0110】 [Reformed gas purification process] The gas purifier 36 removes sulfur-containing components from the reformed gas 8. The reformed gas 8, generated by the mixed gasification of carbon 2 with water vapor 7 and carbon dioxide 9, contains sulfur-containing substances such as hydrogen sulfide and COS. These sulfur-containing substances act as catalyst poisons and may reduce the catalytic activity and impair the stability of the bioethanol production facility. By removing the sulfur-containing components, the stability of the catalytic activity in the bioethanol production facility is improved. 【0111】 The gas purifier 36 is preferably equipped with a gas purifying member in which at least one metal selected from the group consisting of Cu, Zn, Cr, Ce, Fe, Mo, and Co is supported on a porous carrier such as silica, alumina, or zeolite. When such a gas purifying member is brought into contact with biomass gas, sulfur-containing components bind to the metal and porous carrier and are chemically removed from the reformed gas 8. 【0112】 However, the gas purifier 36 is not limited to those produced by the chemical methods described above. For example, other common technologies, such as gas purification techniques using gas adsorbents like activated carbon or various zeolites, can also be used in combination. In addition to desulfurization, the gas purification equipment may also remove nitrogen-containing components such as ammonia and NOx, and chlorine-containing components such as HCl. 【0113】 [Bioethanol manufacturing process] The bioethanol production facility 50 is equipped with a C2 oxygenation catalyst 58 and a hydrogenation catalyst 59. 【0114】 When reformed gas 8 is brought into contact with the C2 oxygenation catalyst 58, C2 oxygenated compounds such as acetic acid, acetaldehyde, and ethanol are produced from H2, CO, CO2, and CH4 contained in the reformed gas 8. Derivatives of C2 oxygenated compounds, such as methyl acetate and ethyl acetate, may also be produced as by-products. Further contact with the hydrogenation catalyst 59 leads to the hydrogenation of acetic acid, acetaldehyde, methyl acetate, ethyl acetate, etc., which are efficiently converted to ethanol. This increases the amount of ethanol produced and also improves the selectivity of ethanol. 【0115】 Next, the reformed gas 8 is pressurized in a booster in a booster gas circulation supply equipment 88 to a predetermined reaction pressure, and then continuously circulated and supplied to the bioethanol production equipment 50. The reformed gas supplied to the bioethanol production equipment comes into contact with a composite catalyst 63, which is prepared by mixing a C2 oxygenation catalyst 58 and a hydrogenation catalyst 59, to produce a liquid product containing bioethanol. 【0116】 The reaction pressure in the bioethanol production facility 50 is preferably 0.1 MPa to 5 MPa, and more preferably 1 MPa to 3.5 MPa. The reaction temperature is preferably 200°C to 350°C, and more preferably 250°C to 300°C. The airtime velocity of the biomass gas (SV: velocity of synthesis gas L / h / volume of catalyst L) is 1000 h -1 ~35,000h -1 Preferably, 3000 h-1 ~25,000h -1 This is more preferable. In the bioethanol production equipment 50 of this embodiment, for example, bioethanol can be obtained with an ethanol selectivity of 50% to 85% and an ethanol yield (STY: g / L-cat / h) of 250 g / L-cat / h to 850 g / L-cat / h. 【0117】 The outlet of the bioethanol production equipment 50 is connected to a gas-liquid separator 52. This separates the liquid product containing ethanol (also called crude ethanol) from the reaction gas. The gas-liquid separator may be of a known type. 【0118】 [Production of H2 and CO2] The reaction gas separated by the gas-liquid separator may be recirculated and supplied to the bioethanol production facility, but in this embodiment, the reaction gas (a mixed gas containing CO, CH4, and CO2) may also be introduced into the shift reaction hydrogen production facility 53 to produce H2 and CO2. 【0119】 The shift reaction hydrogen production equipment 53 produces a mixed gas of H2 and CO2 by bringing the CO and methane in the reaction gas separated in the gas-liquid separator 52 into contact with a shift reaction catalyst in the presence of water vapor, as described below, through the shift reaction. [ka] [ka] 【0120】 In this embodiment, various types of shift reaction catalysts can be selected depending on their intended use. For example, one example is a catalyst containing at least one element selected from the group consisting of Fe, Ru, Ni, Cu, Zn, K, Li, Mg, Cr, Co, Mo, Zr, Ti, Ce, La, and Nd (hereinafter also referred to as element (3)). The shift reaction catalyst may contain two or more elements (3). Furthermore, element (3) may be supported on a support. Examples of supports include porous oxides such as silica and alumina. 【0121】 [CO2 supply] In the shift reaction hydrogen production facility 53, the mixed gas of H2 and CO2 generated may be separated from carbon dioxide 9 in the gas separation and purification unit 54, and the recovered CO2 may be supplied to the reforming gasifier 30 via the carbon dioxide supply regulator 84. 【0122】 [Hydrogen supply] Residual hydrogen is supplied to the hydrogen holder 55 via the hydrogen supply pipe 79. The reformed gas and hydrogen may be mixed and adjusted before being supplied to the bioethanol production equipment. In this embodiment, by adjusting the H2 / CO mixing ratio of the reformed gas, which is preferable for bioethanol production, via a gas mixing and adjusting device, the bioethanol production yield and ethanol selectivity can be significantly improved. This increases the amount of ethylene produced in the subsequent ethylene production process using ethanol and the amount of bio-aviation fuel produced in the ethylene oligomerization reaction process. 【0123】 The gas separation equipment 54 separates CO2 from the mixed gas of H2 and CO2 generated in the shift reaction hydrogen production equipment 53. Examples of the gas separation equipment 54 include a PSA type gas separator and a ceramic membrane type gas separator. Either one of these gas separators may be used, or both may be used. 【0124】 In this embodiment, the shift reaction hydrogen production equipment 53 and the gas separation equipment 54 are connected via H2 / CO2 piping 64. CO2 emitted from the gas separation equipment 54 is supplied to the reforming gasifier 30 via carbon dioxide supply piping 32. Hydrogen is also supplied to the hydrogen holder 55 via the gas separation equipment 54 and hydrogen piping 79. 【0125】 In this embodiment, the water electrolysis equipment 40 and the water electrolysis hydrogen supply regulator 87 are also connected to the hydrogen holder 55. Commercial electricity can be used as the power source for the water electrolysis equipment, but it is preferable to use renewable energy sources such as solar and wind power generation, as well as electricity obtained from nuclear reactor power generation, in order to reduce carbon dioxide emissions in the bio-aviation fuel production process. 【0126】 The hydrogen holder 55 is connected to the gas mixing and adjusting unit 89 via hydrogen piping 79. Hydrogen 10, whose supply amount is adjusted by the hydrogen supply amount regulator 85, is mixed and supplied from the hydrogen holder 55 to the reformed gas 8. This increases the H2 / CO volume ratio in the reformed gas 8, and in the ethanol production process, the H2 / CO volume ratio is preferably adjusted to 1 to 3, more preferably to 1.5 to 2.5, and then pressurized and circulated by the pressurized gas circulation supply equipment 88 before being introduced into the ethanol production equipment 50 to carry out the ethanol production reaction. 【0127】 [Bioethanol purification process] In this embodiment, crude ethanol (50-60% by weight concentration) separated in the gas-liquid separator 52 is purified via an ethanol separation and purification facility 56 equipped with a distillation column and a membrane separation device. The distillation column concentrates and separates ethanol from the ethanol liquid product, and also separates and recovers low-boiling point by-product residues such as acetic acid, acetaldehyde, propanol, and methanol from the liquid product. The distillation column may be of known type, for example, a multi-stage Raschig ring distillation column 37 and a silicon membrane separation device 38. 【0128】 In this embodiment, the ethanol concentration of the crude ethanol liquid product produced in the bioethanol production facility is, for example, 53% to 60% by mass. It is concentrated to 80% to 85% using a commercially available distillation column. For example, it can be separated and purified to an even higher ethanol concentration using a commercially available ceramic membrane separation device. The ethanol concentration of the purified product is, for example, 86% to 99%. 【0129】 [Ethylene manufacturing process] In this embodiment, the high-purity bioethanol generated is used to produce ethylene via an ethylene producer 42. Ethylene is produced in an ethanol dehydration reactor equipped with silica and alumina supports treated with phosphoric acid or MgO at a pressure of 0.1 MPa to 1 MPa and a temperature of 250°C to 480°C. After that, impurities are removed and the mixture is pressurized and stored in a booster. The reaction conditions and catalyst for the bioethanol dehydration process may be those of known origin. 【0130】 [Ethylene oligomerization process] In this embodiment, ethylene generated in the ethylene production process is used to produce C6-C16 isooligomers in an oligomerization reactor 43 with a yield of 85%-90%. The oligomerization reaction of ethylene is carried out at 120°C-250°C and 2MPa-5MPa in the presence of a metal complex catalyst containing Co, Ti, and Zr. The C2-C5 light olefins generated in the oligomerization process are separated and recovered in a distiller, and the recovered light olefins are recycled back into the oligomerization reactor. This improves the amount and yield of C6-C16 isooligomers produced. The catalyst and reaction conditions in the ethylene oligomerization process may be those known to be used. 【0131】 [Hydrogenation process] In this embodiment, the C6-C16 isooligomers separated and recovered via the oligomerization reactor 43 and distillation apparatus 44 are subjected to hydrogenation treatment in a hydrogenation treatment apparatus 45 to produce bio-aviation fuel with a conversion rate of 85%-90% for C6-C16 isoparaffins. The hydrogenation treatment is carried out in the presence of a precious metal catalyst containing Pt, Pd, and Ir, under reaction conditions of 250°C-350°C and 1MPa-5MPa. The catalyst and reaction conditions in the hydrogenation process in this embodiment may be known ones. 【0132】 The bio-aviation fuel manufacturing method of this embodiment allows for an increased carbonization rate of biomass, enabling efficient production of reformed gas and subsequent economical and stable production of bioethanol. This allows for highly efficient and stable production of ethylene in the subsequent ethylene production process using ethanol and of C6-C16 isoparaffins produced in the ethylene oligomerization reaction process as bio-aviation fuel. 【0133】 Although the present invention has been described above with reference to examples of embodiments, the present invention is not limited to the above-described examples of embodiments, and can be freely modified within the scope of the present invention. 【0134】 Examples of the present invention are shown below, but these examples are for illustrative purposes only and do not limit the content of the present invention. [Examples] 【0135】 A test was conducted to produce bio-aviation fuel using a bio-aviation fuel production apparatus configured as shown in Figure 1. In this test, 250 kg / h of construction waste chips (moisture content 27% by mass) were fed into a dryer and a carbonization furnace, and the carbonization rate (wt%) of the carbides in the carbonization furnace, the amount of reformed gas produced in the reforming gasifier (Nm3 / h), the composition of the reformed gas components (vol%), the amount of bioethanol produced (kg / h), and the amount of bio-aviation fuel produced (kg / h) were measured. In this test, 105 kg / h of steam and 70 Nm3 / h of CO2 were fed into the reforming gasifier to perform mixed gasification. 【0136】 The experimental results for the carbonization rate, reformed gas production volume, reformed gas composition, ethanol production volume, and bio-aviation fuel (C6-C16 isoparaffin) production volume when metal-containing residue (10 kg / h) separated and recovered by a cyclone dust collector is recycled and supplied to a construction waste chip receiver, and when it is not supplied, are shown in Example 1 and Comparative Example 1. The reaction conditions for ethylene production by the dehydration reaction of ethanol in this test were 480°C and 0.5 MPa. The oligomination reaction of ethylene was carried out under reaction conditions of 120°C to 250°C and 2.5 MPa to 5 MPa. 【0137】 The composition of reformed gas components and the analysis of liquid components including CO, hydrogen, CO2, CH4 in the outlet gas of the shift reaction hydrogen production plant, and ethanol generated in the ethanol production plant were measured using a Gaskuropack and a thermal conductivity type gas chromatograph analyzer (Shimadzu GC-14B) and an FID gas chromatograph analyzer (Shimadzu GC-8A) filled with molecular sieves 13X. The flow rate of the exhaust gas was measured using a wet gas flow meter. 【0138】 The metallic element content of the metal-containing residue was measured using an ICP emission spectrometer (Shimadzu ICPS-8100) and an X-ray fluorescence spectrometer (Hitachi High-Tech EA1400). The metallic content per 1 kg of the metal-containing residue obtained in this test was Na 25 g / kg, K 85 g / kg, Ca 36 g / kg, Mg 7.5 g / kg, Ba 5 g / kg, Fe 7.5 g / kg, and Ni 1.8 g / kg. 【0139】 [C2 oxygenation catalyst 1] Chlorides or nitrates of Rh, Mg, V, Hf, Ir, and Ce were dissolved in a mixed solvent of ethanol and water in an atomic ratio of 1:0.3:0.2:0.5:0.3 to obtain an aqueous ethanol solution. This aqueous ethanol solution was impregnated into a silica support (specific surface area 315 m2 / g), and then activated by heating to 150°C over 1 hour under a gas stream of hydrogen and nitrogen gas (1:3 volume ratio), holding for 2 hours, heating to 450°C over 2 hours, holding for 2 hours, and then cooling to room temperature. This prepared C2 oxygenated catalyst 1 with Rh, Mg, V, Hf, Ir, and Ce supported on the silica support. 【0140】 [Hydrogenation catalyst 1] Cu, Cr nitrate, Ti, and Mo chloride were dissolved in a mixed solvent of ethanol and water in an atomic ratio of Cu:Cr:Ti:Mo of 1:0.8:0.2:0.15 to obtain an aqueous ethanol solution. This aqueous ethanol solution was impregnated into a silica support (specific surface area 365 m2 / g), and then activated by heating to 100°C over 1 hour under a gas stream of hydrogen and nitrogen gas (1:2 volume ratio), holding for 2 hours, heating to 450°C over 2 hours, holding for 3 hours, and then cooling to room temperature. This prepared hydrogenation catalyst 1 with Cu, Cr, Ti, and Mo supported on the silica support. 【0141】 A composite catalyst prepared by mixing 100 kg of C2 oxygenation catalyst and 200 kg of hydrogenation catalyst in a commercially available mixing and preparation device was packed into a titanium-coated stainless steel reactor. Bioethanol was produced by contacting the reformed gas with the composite catalyst. The bulk density of the prepared catalyst in this test was 0.5 kg / L. 【0142】 [Table 1] TIFF0007872555000008.tif58140 【0143】 These results demonstrate that the carbonization rate, reformed gas production volume, and ethanol and bio-aviation fuel production volume in the carbonization process using construction waste chips are significantly improved when metal-containing residue is recycled and supplied (Example 1) compared to when it is not recycled and supplied (Comparative Example 1). [Examples] 【0144】 Using sugarcane bagasse, tests were conducted in the same manner as in Example 1 for carbonization rate, reformed gas production, ethanol production, and bio-aviation fuel production. Sugarcane bagasse was fed at a rate of 350 kg per hour. The carbonization operation was carried out under conditions of carbonization furnace temperature of 250°C to 420°C. Table 2 shows the test results for the reformed gas production (Nm3 / h), reformed gas component composition (vol%), and ethanol production (kg-EtOH / h) and bio-aviation fuel (C6-C16 isoparaffin) production (kg / h) in the bioethanol production process using the reformed gas, when the carbonized material reforming gasification process was carried out at a temperature of 900°C with a mixed supply of 150 kg / h of water vapor and 100 Nm3 / h of CO2 (Example 2), and when 150 kg / h of water vapor was supplied alone (Comparative Example 2). The reaction conditions for ethylene production by ethanol dehydration in this test were 480°C and 0.5 MPa. The oligomerization reaction of ethylene was carried out under reaction conditions of 120°C to 250°C and 2.5 MPa to 5 MPa. 【0145】 In this experiment, metal-containing residue separated and recovered by a cyclone dust collector was mixed and fed into a bagasse (sugarcane juice residue) receiver at a rate of 15 kg per hour for carbonization and gasification. The metal content per 1 kg of metal-containing residue obtained in this experiment was Na 45 g / kg, K 65 g / kg, Ca 50 g / kg, Mg 15 g / kg, Ba 2.5 g / kg, Li 1.5 g / kg, Fe 2.8 g / kg, and Ni 0.5 g / kg. 【0146】 [C2 oxygenation catalyst 2] Chlorides of Rh, Mn, Li, Sc, and Ce were dissolved in a mixed solvent of ethanol and water in an atomic ratio of 1:0.05:0.30:0.10:0.05 to obtain an aqueous ethanol solution. This aqueous ethanol solution was impregnated into a silica support (specific surface area 385 m2 / g), and then activated by heating to 100°C over 1 hour under a gas stream of hydrogen and nitrogen gas (1:4 volume ratio), holding for 2 hours, heating to 400°C over 2 hours, holding for 2 hours, and then cooling to room temperature. This prepared C2 oxygenated catalyst 2 with Rh, Mn, Li, Sc, and Ce supported on the silica support. 【0147】 [Hydrogenation catalyst 2] The nitrates of Pd, Cu, Zn, K, and Zr were dissolved in a mixed solvent of ethanol and water in an atomic ratio of 1:0.8:0.2:0.15 to obtain aqueous ethanol solutions. 【0148】 After impregnating a silica support (specific surface area 265 m2 / g) with this ethanol aqueous solution, the silica support was heated to 100°C over 1 hour under a gas stream of hydrogen and nitrogen gas (1:2 volume ratio), held for 2 hours, then heated to 400°C over 2 hours, held for 2 hours, and cooled to room temperature. This activated the silica support, and hydrogenation catalyst 2 was prepared with Pd, Cu, Zn, K, and Zr supported on it. The bulk density of the prepared catalyst in this test was 0.5 kg / L. 【0149】 A composite catalyst prepared by mixing a C2 oxygenation catalyst (160 kg) and a hydrogenation catalyst (320 kg) in a mixing and preparing device was packed into a Ti-coated stainless steel reactor. Bioethanol was produced by contacting the reformed gas with the composite catalyst. The reaction conditions for ethylene production by the dehydration reaction of ethanol in this test were 480°C and 0.5 MPa. The oligomination reaction of ethylene was carried out under reaction conditions of 120°C to 250°C and 2.5 MPa to 5 MPa. 【0150】 [Table 2] 【0151】 These results demonstrate that in the reforming and gasification process of charred materials using bagasse, the residue from sugarcane juice extraction, the reformed gas composition, gas production volume, ethanol production volume, and bio-aviation fuel production volume under mixed supply conditions of steam and CO2 (Example 2) are significantly increased compared to the case of supplying steam alone (Comparative Example 2). [Examples] 【0152】 In an embodiment similar to Example 2, 450 kg / h of cedar chips (moisture content 35%) were used as biomass for carbonization and gasification. The resulting reformed gas was then contacted with a composite catalyst prepared by mixing C2 oxygen-containing catalyst 2 and hydrogenation catalyst 2 to produce bioethanol. 【0153】 In this test, the reaction gas separated by a gas-liquid separator in the ethanol production facility was fed into a shift reaction hydrogen production facility, and the resulting hydrogen-CO2 mixed gas was separated from the CO2 using a ceramic membrane separator. The residual hydrogen was then stored in a hydrogen holder. Table 3 shows the CO conversion rate (ethanol / CO molar ratio %), ethanol selectivity (%), ethanol yield (STY: g-EtOH / L-cat / h), and bio-aviation fuel production amount (kg / h) for the case where hydrogen was supplied from the hydrogen holder to the reformed gas by gas mixing preparation and adjusted to an H2 / CO volume ratio of 2.5 in the reformed gas (Example 3), and for the case where no hydrogen was supplied (Comparative Example 3). 【0154】 [Table 3] 【0155】 These results demonstrate that when hydrogen generated in the shift reaction hydrogen production facility is supplied to the reformed gas (Example 3), the ethanol selectivity and ethanol yield increase compared to when hydrogen is not supplied (Comparative Example 3). This increases the amount of ethylene produced in the subsequent ethylene production process using ethanol and the amount of bio-aviation fuel produced in the ethylene oligomerization reaction process. [Examples] 【0156】 In an ethanol production apparatus and embodiment similar to that of Example 1, a composite catalyst obtained by mixing C2 oxygenation catalyst 1 and hydrogenation catalyst 1 in a mass ratio of 1:1 using a catalyst mixing and preparing device was packed into a Ti-coated stainless steel reaction tube. The reformed gas was then subjected to a reaction at 2.5 MPa, 285°C, and SV=25,000 h. -1 Table 4 shows the CO conversion rate, ethanol selectivity, bioethanol yield (STY: g-EtOH / L-cat / h), and bio-aviation fuel production amount (kg / h) in ethanol production when ethanol is produced by catalytic circulation reaction with a composite catalyst (Example 4) and when the same amount of C2 oxygenated catalyst 1 is separately stacked in the reactor with the hydrogenation catalyst 1 in the upper layer and the hydrogenation catalyst 1 in the lower layer (Comparative Example 4). 【0157】 [Table 4] 【0158】 This demonstrated that when a composite catalyst prepared by mixing a C2 oxygenation catalyst and a hydrogenation catalyst was used (Example 4), the ethanol yield, ethanol selectivity, and bio-aviation fuel production volume were significantly improved compared to when the C2 oxygenation catalyst and the hydrogenation catalyst were stacked separately (Comparative Example 4). [Industrial applicability] 【0159】 According to the present invention, it is possible to provide a method for producing bio-aviation fuel and a bio-aviation fuel production apparatus that can efficiently produce reformed gas using biomass and subsequently produce bioethanol economically and stably. [Explanation of symbols] 【0160】 1. Biomass 2. Carbides 3 Metal-containing residue 4 Water supply 5. Drying gas (containing tar) 6. Combustion gases 7. Water vapor 8. Reformed gas 9. Carbon dioxide 10 Hydrogen 11. Biomass receiver 12 Biomass dryer 20 Carbonization furnace 30 Reforming Gasifier 31. Steam heat exchanger 32. Carbon dioxide supply piping 33 Steam supply piping 34 Dust collector 35. First reformed gas piping 36 Gas Purifier 37 Metal-containing residue supply equipment 38 Metal-containing residue receiver 39 Metal-containing residue discharge piping 40 Water electrolysis equipment 41 Air blower 42 Ethylene producer 43. Oligosaccharide Reactor 44 Distillation apparatus 45 Hydrogenation reactor 46. ​​Light Olefin Recycling Piping 47. Bio-aviation fuel 50 Ethanol production facilities 51 Hydrogen supply piping 52 Gas-liquid separator 53 Shift Reaction Hydrogen Production Equipment 54 Gas separation and purification equipment 55 Hydrogen holder 56 Ethanol Separation and Purification Equipment 57 Catalyst Mixing Preparator (Catalyst Mixing Preparation Equipment) 58 C2 oxygenation catalyst 59 Hydrogenation catalyst 60 Air Combustor 61 Combustion gas flow regulator 62. Combined catalyst introduction equipment 63. Compound catalyst 64 H2 / CO2 gas piping 70 Combustion gas piping equipment 71. Combustion gas piping (for dryers) 72 Combustion gas piping (for carbonization furnace) 73 Combustion gas piping (for reforming gasification furnace) 74. Combustion gas piping (for steam heat exchangers) 75. Combustion gas piping (for ethanol production equipment) 76. Combustion gas piping (for shift reaction hydrogen production equipment) 77 Piping for crude ethanol 78 Hydrogen supply piping 79 Hydrogen supply piping 80. Biomass supply adjustment device (biomass supply adjustment means) 81 Carbide supply amount regulator (carbide supply amount adjustment means) 82. Metal-containing residue supply adjustment device (metal-containing residue separation and recovery means) 83. Carbon dioxide supply regulator (carbon dioxide supply adjustment means) 84. Steam supply regulator 85 Hydrogen supply regulator 86. Reformed gas supply rate regulator (reformed gas supply equipment) 87 Water electrolysis hydrogen supply amount regulator 88. Booster gas circulation supply equipment 89 Gas Mixing and Adjusting Device 90 Bioethanol 91 Biomass supply facilities 92. Carbide supply equipment 93. Reformed Gas Supply Equipment 94. Metal-containing residue separation and recovery device (means for separating and recovering metal-containing residue) 95 Catalyst mixture amount regulator (catalyst mixture amount adjustment means) 96 Combustion gas piping (for ethylene production equipment) 97 Combustion gas piping (for oligomerization reactor) 98 Combustion gas piping (for hydrogenation reactor) 100 Bio-aviation fuel production equipment

Claims

[Claim 1] The carbonization process involves carbonizing biomass to produce carbonized material, A reforming gasification step is performed to carry out a mixed gasification reaction of the carbide with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide. An ethanol production process comprising contacting the reformed gas with a C2 oxygenation catalyst and a hydrogenation catalyst to produce ethanol, An ethylene production process in which ethylene is produced in the ethanol dehydration reaction step, The ethylene oligomerization reaction step, A method for producing bio-aviation fuel, comprising a mixing step of mixing a metal-containing residue generated together with the reformed gas in the reformed gasification step with the biomass. [Claim 2] The method for producing bio-aviation fuel according to claim 1, wherein the metal-containing residue comprises at least one element selected from the group consisting of alkali metals, alkaline earth metals, B, Al, Fe, and Ni. [Claim 3] A method for producing bio-aviation fuel according to claim 1, comprising a shift reaction step in which carbon monoxide and methane contained in the residual gas after separating a liquid product containing ethanol from the gas produced in the ethanol production step are subjected to a shift reaction in the presence of water vapor to produce hydrogen and carbon dioxide. [Claim 4] A method for producing bio-aviation fuel according to claim 3, comprising a supply step of separating and recovering carbon dioxide from a mixed gas of hydrogen and carbon dioxide generated in the shift reaction step, supplying the recovered carbon dioxide to the reforming gasification step, and supplying the hydrogen to the reformed gas. [Claim 5] A method for producing bio-aviation fuel according to claim 3, wherein in the shift reaction step, a shift reaction catalyst is used that comprises at least one element selected from the group consisting of Fe, Ru, Ni, Cu, Zn, K, Li, Mg, Cr, Co, Mo, Zr, Ti, Ce, La, and Nd, and a porous oxide support. [Claim 6] A method for producing bio-aviation fuel according to claim 3 or 4, wherein the carbonization gas generated together with the carbonized material in the carbonization step is combusted with air, and the resulting combustion gas is used as a heat source to heat and use at least one of the steps of the carbonization step, the reforming gasification step, the ethanol production step, and the shift reaction step. [Claim 7] The method for producing bio-aviation fuel according to claim 1, wherein the C2 oxygenation catalyst comprises Rh, at least one element selected from the group consisting of Mn, Sc, Li, Na, K, Cs, Mg, Ba, Pt, Pd, Ir, Mo, W, V, Zr, Hf, Ti, Y, Ce, and La, and a porous support. [Claim 8] The method for producing bio-aviation fuel according to claim 1, wherein the hydrogenation catalyst comprises at least one element selected from the group consisting of Pd, Fe, Ni, Pt, Cu, Cr, Zn, K, Na, Ce, and Ti, and a porous support. [Claim 9] A method for producing bio-aviation fuel according to claim 1, wherein in the ethanol production step, a composite catalyst is used which is prepared by mixing the C2 oxygenation catalyst and the hydrogenation catalyst, and the mixed volume ratio of the C2 oxygenation catalyst to the hydrogenation catalyst in the composite catalyst (C2 oxygenation catalyst / hydrogenation catalyst) is 0.1 or more and 5 or less. [Claim 10] An ethylene production process comprising the dehydration reaction of ethanol to produce ethylene, An oligomerization step to produce C6-C16 isooligomers using the ethylene, A recycling process for light olein, which separates and recovers the light olefin produced as a by-product in the ethylene oligomerization process and feeds it back into the oligomerization process, A method for producing bioaviation fuel according to claim 1, comprising a hydrogenation step of hydrogenating the isooligomer to produce bioaviation fuel. [Claim 11] Reforming gasifier and Biomass supply facilities and means for adjusting the amount of biomass supply, A biomass dryer having means for adjusting and controlling the degree of dryness of the biomass, A carbonization furnace having a temperature control mechanism, A carbide supply facility that supplies carbides to the aforementioned reforming gasifier, A carbide supply amount adjustment means for adjusting the amount of carbide supplied to the reforming gasifier, A supply facility for supplying steam and carbon dioxide to the reforming gasifier, A carbon dioxide supply adjustment means for adjusting the amount of steam and carbon dioxide supplied to the reforming gasifier, A bioethanol production facility is connected to a reformed gas supply facility that supplies reformed gas from the reformed gasification furnace, and the reformed gas is brought into contact with a C2 oxygenation catalyst and a hydrogenation catalyst to produce bioethanol. A separation and recovery means for separating and recovering metal-containing residue generated together with the reformed gas from the reformed gas, A metal residue supply facility that supplies and mixes the recovered metal-containing residue with the biomass, A means for adjusting the amount of metal-containing residue supplied to the biomass, The bioethanol production facility includes a catalyst mixing and preparation apparatus for obtaining a composite catalyst by mixing and preparing a C2 oxygenation catalyst and the hydrogenation catalyst, A catalyst mixing amount adjustment means for adjusting the amount of the C2 oxygenation catalyst mixed with the hydrogenation catalyst, An ethylene production facility that produces ethylene from the aforementioned bioethanol, An oligomerization reactor that produces C6-C16 isooligomers from ethylene by an oligomerization reaction, A distillation apparatus for separating and recovering the isooligomer, A bio-aviation fuel production apparatus comprising a hydrogenation reactor that hydrogenates the iso-oligomer to produce bio-aviation fuel. [Claim 12] A gas separation apparatus for separating carbon dioxide from a mixture of hydrogen and carbon dioxide contained in the residual gas after separating the liquid product containing ethanol produced in the bioethanol production apparatus, A first piping system for supplying carbon dioxide recovered in the gas separation equipment to the reforming gasifier, A carbon dioxide supply adjustment means for adjusting the amount of carbon dioxide recovered and supplied to the reforming gasification furnace, A second piping system for supplying residual hydrogen remaining in the gas separation equipment to a hydrogen holder, A hydrogen supply amount adjustment means for adjusting the amount of residual hydrogen supplied to the hydrogen holder, A third piping system for supplying hydrogen generated in a water electrolysis facility to the hydrogen holder, A hydrogen supply amount adjustment means for adjusting the amount of hydrogen supplied to the hydrogen holder, A supply facility for supplying the residual hydrogen and the hydrogen from the hydrogen holder to the reforming gasifier, A hydrogen supply adjustment means for adjusting the amount of residual hydrogen and hydrogen supplied to the reforming gasifier, A reformed gas circulation rate adjustment means for adjusting the amount of reformed gas circulated to the composite catalyst, The facility includes a separation and purification apparatus for separating and purifying ethanol from a liquid product containing ethanol, The apparatus for producing bio-aviation fuel according to claim 11, wherein the reformed gas supply equipment is a pressurized and circulating supply equipment that brings the reformed gas into contact with the composite catalyst. [Claim 13] A combustion furnace for burning the carbonization gas generated in the carbonization furnace, A heat exchanger for heating the steam introduced into the reforming gasifier, The bio-aviation fuel production apparatus according to claim 11 or 12, further comprising a piping system for supplying the combustion gas generated in the combustion furnace as a heating gas to at least one of the reforming gasifier, the biomass dryer, the carbonizer, and the shift reaction equipment.

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