Biojet fuel production method and biojet fuel production device

Abstract

The present invention aims to provide a method and an apparatus for producing biojet fuel that can efficiently and stably produce biojet fuel using biomass such as sewage sludge and organic waste. [Solution] The present invention provides a method for producing biojet fuel, which includes a carbonization process for carbonizing biomass such as sewage sludge and organic waste to produce a carbonized product, a reformed-gasification process for gasifying the carbonized product with steam and carbon dioxide to produce a reformed gas, an olefin production process for contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms, an oligomerization reaction process for oligomerizing the olefins to produce iso-oligomers having 6 to 16 carbon atoms, a hydrogenation process for hydrogenating the iso-oligomers to produce a biojet fuel containing isoparaffin, and a process for separating and recovering metal-containing residue generated in the reformed-gasification process and mixing it with the biomass.

Description

[Technical field]

[0001] The present invention relates to a method and an apparatus for producing biojet fuel. [Background technology]

[0002] Organic waste such as sewage sludge, peat, and industrial waste is discharged in large quantities as biomass waste, and their disposal has become an environmental problem. For this reason, there is an increasing need to develop technologies for reducing the volume of sewage sludge and organic waste and for utilizing them as energy resources, such as methane fermentation technology and gasification power generation. Up until now, sewage sludge has generally been used as a fuel for combustion or buried as waste. In recent years, a technology for pyrolysis and gasification of sewage sludge at high temperatures using oxygen, air, and steam, a technology for producing charcoal by carbonizing sewage sludge, and a technology for using it as an alternative fuel for thermal power generation have been developed (Patent Documents 1-3, Non-Patent Documents 1-2).

[0003] Specifically, Patent Document 1 discloses a sewage sludge pyrolysis gasification power generation system that generates power using pyrolysis gas produced by pyrolyzing sewage sludge. Patent Document 2 discloses a method for producing a carbonized material by heating sewage sludge or biomass containing sewage sludge to 250°C or higher while passing a heated gas through it to remove volatile components in the biomass, and then indirectly heating it at 400-500°C to carbonize it. Patent Document 3 discloses a method for converting sludge into fuel, which comprises drying sewage sludge, adding woody biomass to the dried sewage sludge, and carbonizing the sludge to produce pyrolysis gas and charcoal. Non-Patent Document 1 discloses a sewage sludge carbonization system in which sewage sludge is dewatered to a moisture content of about 80%, is further dried, and then is charged into a carbonization furnace for carbonization. Non-patent document 2 discloses a method for producing carbonized sewage sludge fuel in which sewage sludge is dehydrated, further dried to a moisture content of 25%, and then heated and pyrolyzed in a rotary kiln to convert it into a carbonized material, which is then used as carbonized fuel.

[0004] Other technologies that have been developed include the direct reformed gas production method, in which organic waste such as grass, rice straw, bagasse, and other agricultural waste, and peat, construction wood, cotton, paper, and food waste are reacted directly with steam, oxygen, and air at high temperatures to produce reformed gas, and the two-stage gas production technology, in which biomass raw materials are carbonized by dry distillation and the resulting carbonized material is reacted with steam to produce reformed gas. The reformed gas produced by these biomass gasification technologies is a mixed gas containing carbon monoxide (CO), hydrogen (H2), methane (CH4), ethane (C2H6), carbon dioxide (CO2), etc. Conventional methods for using the reformed gas include as fuel for gas engine power generation and hydrogen production by applying hydrogen extraction technology from the reformed gas (Patent Documents 4-6, Non-Patent Documents 3-5).

[0005] Specifically, Patent Document 4 discloses reformed gas produced from biomass that can be used in gas engines and gas turbines. Patent Document 5 discloses refining gas obtained from biomass gas and using the refined gas as fuel to drive a gas turbine. Patent Document 6 discloses obtaining a carbonized material from biomass or organic waste as a raw material, further pyrolyzing it with steam and air to generate water gas, and using the water gas as fuel for an internal combustion engine that is easy to operate with daily start-up and shutdown. Non-Patent Documents 3 and 4 disclose techniques and problems of gasifying biomass and using it for power generation. Non-Patent Document 5 discloses a technique of producing biogas in a reformed gasifier using woody biomass such as forest resources as a raw material, and further storing the hydrogen in the biogas in methylhexane to use it for hydrogen stations and hydrogen power generation.

[0006] However, in the conventional technology, in addition to low molecular weight fuel gas, heavy components such as oily components and tar are generated in the carbonization process, which may cause serious loads and obstacles to the subsequent reformed gas and hydrogen production. In addition, in recent years, from the viewpoint of economics and environmental load, there has been a demand for energy saving in the reformed gasification of the carbonized material and hydrogen production, reduction in the production costs of the reformed gas and hydrogen, and reduction in the emissions of global warming substances such as carbon dioxide resulting from the consumption of external fuels such as heavy oil, kerosene, and electricity.

[0007] On the other hand, from the viewpoint of reducing emissions of substances that cause global warming, carbon neutral jet fuel has become an important theme, especially in the aviation industry. Biojet fuel produced from biomass and the like has attracted attention as a way to achieve such carbon neutrality (Patent Documents 7 and 8). Patent Documents 7 and 8 disclose a method for producing a biojet fuel consisting of isomerized hydrocarbons having 7 to 14 carbon atoms by heating and catalytically reforming oil derived from biomass. However, these conventional methods for producing biojet fuel using biomass as a raw material are insufficient for efficiently and stably producing biojet fuel. [Prior art documents] [Patent documents]

[0008] [Patent Document 1] Patent Publication No. 2002-256884 [Patent Document 2] Patent Publication No. 2007-84728 [Patent Document 3] Patent No. 3861093 [Patent Document 4] International Publication No. WO2008 / 050727 [Patent Document 5] Patent No. 4295793 [Patent Document 6] JP2004-35837A [Patent Document 7] International Publication No. WO2023 / 085337 [Patent Document 8] International Publication No. WO2024 / 071264 [Non-patent literature]

[0009] [Non-Patent Document 1] Susumu Shimura, Tadatoshi Ko, Makoto Kitabayashi, Kenji Shimizu, "Use of sewage sludge carbonized material as biomass fuel," Electric Steel Manufacturing, Vol. 78, No. 1, pp. 73-78 (2007) [Non-Patent Document 2] Takeshi Amari, Mizuhiko Tanaka, Yoichi Koga, Satoshi Okuno, Akira Tajima, "Sewage sludge carbonization fuel production and biomass power generation," Proceedings of the 16th Environmental Engineering Symposium 2006, Japan Society of Mechanical Engineers, pp. 151-153 (2006) [Non-Patent Document 3] Edited by Masaru Ichikawa, "New Developments in Biomass Refinery Catalyst Technology", CMC Publishing (2011), pp70-77, pp99-106 [Non-Patent Document 4] Kenichi Sasauchi, "Power Generation from Biomass Pyrolysis Gasification", Journal of the Combustion Society of Japan, Vol. 47, No. 139 (2005), pp. 31-39 [Non-Patent Document 5] Masaru Ichikawa, "New developments in hydrogen energy technology utilizing biomass resources," Life and Environment, Vol. 61, No. 1 (2016), pp. 27-32 Summary of the Invention [Problem to be solved by the invention]

[0010] The present invention has been made in consideration of the problems of the conventional technology as described above, and provides a method and apparatus for producing biojet fuel that can efficiently and stably produce biojet fuel using biomass such as sewage sludge and organic waste. [Means for solving the problem]

[0011] The present invention relates to a method for producing a biojet fuel, and includes a carbonization step of carbonizing biomass to produce a carbonized product, a reformed-gasification step of gasifying the carbonized product with steam and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane and carbon dioxide, an olefin production step of contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms, an oligomerization reaction step of oligomerizing the olefins to produce iso-oligomers having 6 to 16 carbon atoms, a hydrogenation step of hydrogenating the iso-oligomers to produce isoparaffins and producing a biojet fuel containing the isoparaffins, and a separation and recovery step of separating and recovering a metal-containing residue generated together with the reformed gas in the reformed-gasification step from the reformed gas and mixing the recovered metal-containing residue with the biomass.

[0012] In the present invention, the metal-containing residue may contain at least one element selected from the group consisting of alkali metals and alkaline earth metals including sodium, potassium, lithium, calcium, magnesium, and barium, boron, aluminum, iron, and nickel.

[0013] In the present invention, the olefin production step may include a separation step of separating a reaction gas generated by contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst into a mixed gas containing carbon monoxide and methane, and an olefin having 2 to 4 carbon atoms.

[0014] The present invention may further comprise a shift reaction hydrogen production step in which carbon monoxide and methane in the reaction gas generated in the olefin production step are reacted with steam to produce hydrogen and carbon dioxide.

[0015] In the present invention, carbon dioxide generated in the shift reaction hydrogen production step may be introduced into the reformed gasification step, and hydrogen generated in the shift reaction hydrogen production step may be mixed with the reformed gas obtained from the reformed gasification step.

[0016] In the present invention, in the shift reaction hydrogen production step, a shift reaction catalyst containing at least one element selected from the group consisting of iron, ruthenium, nickel, copper, zinc, potassium, lithium, magnesium, chromium, cobalt, molybdenum, zirconia, titanium, cerium, lanthanum, and neodymium, and a porous oxide support may be used.

[0017] In the present invention, the carbonization gas generated together with the carbonized material in the carbonization process may be combusted and introduced into at least one of the carbonization process, the reforming gasification process, the steam heat exchange process, the steam heat exchange process, the olefin production process, and the oligomerization reaction process.

[0018] In the present invention, the carbonization gas generated together with the carbonized material in the carbonization process may be combusted and introduced into at least one of the carbonization process, the reforming gasification process, the steam heat exchange process, the shift reaction hydrogen production process, the olefin production process, and the oligomerization reaction process.

[0019] In the present invention, the methanol synthesis catalyst may contain at least one element selected from the group consisting of copper, zinc, chromium, manganese, scandium, lithium, sodium, potassium, cesium, magnesium, barium, platinum, palladium, iridium, molybdenum, tungsten, vanadium, zirconium, hafnium, titanium, yttrium, cerium, and lanthanum, and a porous support.

[0020] In the present invention, the mesoporous catalyst may contain a porous support made of a mesoporous zeolite and a mesoporous clay mineral.

[0021] In the present invention, the olefin production step may use a composite catalyst prepared by mixing the methanol synthesis catalyst and the mesoporous catalyst, and a mixing volume ratio of the methanol synthesis catalyst to the mesoporous catalyst in the methanol synthesis catalyst may be 0.1 to 5.

[0022] The present invention relates to an apparatus for producing biojet fuel, and includes a carbonization furnace for introducing biomass and producing a carbonized product, a reforming gasification furnace for introducing the carbonized product obtained in the carbonization furnace and subjecting it to a gasification reaction with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide, an olefin production facility for introducing the reformed gas obtained in the reforming gasification furnace and contacting it with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms, an oligomerization reaction facility for introducing the olefins and subjecting them to an oligomerization reaction to produce isoparaffins having 6 to 16 carbon atoms, and a hydrogenation facility for introducing the isoparaffins obtained in the oligomerization reaction facility and hydrogenating them to produce a biojet fuel, and further includes a separation and recovery means for separating and recovering a metal-containing residue generated together with the reformed gas in the reforming gasification furnace from the reformed gas, and a means for introducing the metal-containing residue recovered by the separation and recovery means into the biomass.

[0023] In the present invention, the plant may further include a shift reaction facility for producing hydrogen and carbon dioxide by reacting carbon monoxide and methane in the reaction gas generated in the olefin production facility with steam.

[0024] In the present invention, the olefin production facility may be equipped with a separation means for separating the generated reaction gas into olefins having 2 to 4 carbon atoms and a gas containing carbon monoxide and methane.

[0025] In the present invention, the shift reaction facility may include a transfer means for transferring the produced carbon dioxide to the reforming gasification furnace.

[0026] In the present invention, a combustion device is provided that combusts the carbonization gas discharged from the carbonization furnace, and the combustion device may be provided with a supply means that supplies the combusted gas as a heating gas to at least one of the carbonization furnace, the reforming gasification furnace, the olefin production equipment, the oligomerization reaction equipment, and the hydrogenation equipment.

[0027] In the present invention, a combustion device is provided that combusts the carbonization gas discharged from the carbonization furnace, and the combustion device may be provided with a supply means that supplies the combusted gas as a heating gas to at least one of the carbonization furnace, the reforming gasification furnace, the olefin production equipment, the oligomerization reaction equipment, the hydrogenation equipment, and the shift reaction equipment. Effect of the Invention

[0028] According to the present invention, it is possible to provide a method and an apparatus for producing biojet fuel that can efficiently and stably produce biojet fuel using biomass such as sewage sludge and organic waste. [Brief description of the drawings]

[0029] [Figure 1] FIG. 1 is a schematic diagram showing an apparatus according to an embodiment of the present invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0030] Hereinafter, an embodiment of a method for producing a biojet fuel and an apparatus for producing a biojet fuel (hereinafter, simply referred to as a production method and a production apparatus) according to the present invention will be described. In the present specification, when a numerical range is indicated by "~", it means that the numerical values ​​before and after it are included as the lower and upper limits (i.e., the range is between the values ​​indicated).

[0031] (First embodiment: method for producing biojet fuel) In this embodiment, a method for producing biojet fuel is described. The method for producing a biojet fuel according to the present embodiment includes the steps of: The method for producing biojet fuel comprises a carbonization step of carbonizing biomass to produce a carbonized product, a reformed-gasification step of gasifying the carbonized product with steam and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane and carbon dioxide, an olefin production step of contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms, an oligomerization reaction step of oligomerizing the olefins to produce isoparaffins having 6 to 16 carbon atoms, and a hydrogenation step of hydrogenating the isoparaffins to obtain a biojet fuel, wherein a metal-containing residue generated together with the reformed gas in the reformed-gasification step is separated and recovered from the reformed gas, and the recovered metal-containing residue is mixed with the biomass.

[0032] [biomass] The biomass used as the raw material in this embodiment will be described. The biomass used in this embodiment is a reusable organic resource derived from plants or animals, and is not particularly limited as long as it is not a fossil fuel such as petroleum, but examples of the biomass include sewage sludge and organic waste. Examples of sewage sludge include sewage sludge generally generated in sewage treatment facilities and the like. When used in the method of this embodiment, the sewage sludge can be dehydrated and adjusted to a moisture content of about 80%. In addition, sewage sludge generated in sewage treatment facilities and the like may be used for methane gas production by methane fermentation treatment or the like, but the method of this embodiment can use sewage sludge before or after methane fermentation treatment. Sewage sludge is usually pulverized from a state of dehydrated cake dehydrated to about 80% by mass, and may be further dried in a kiln dryer or the like to a moisture content of about 15% to 30% by mass.

[0033] Examples of organic waste include felled forest materials such as cedar, pine, and bamboo, agricultural products and by-products such as rice straw and sugarcane, construction waste, industrial waste such as cotton and textile products, natural materials such as peat and driftwood, and crushed materials obtained by crushing these materials (hereinafter also referred to as raw material chips). The size of the raw material chips is, for example, 5 to 100 mm. The organic waste may be used alone or in combination of two or more types.

[0034] The organic waste may be dried in the same manner as the sewage sludge, using the kiln dryer, etc. In this case, the organic waste may be dried together with the sewage sludge, or may be dried in a dryer separate from the sewage sludge, and then mixed with the sewage sludge and subjected to the carbonization step.

[0035] As the biomass as the raw material in this embodiment, the above-mentioned sewage sludge and organic waste may be used alone, or the above-mentioned sewage sludge and organic waste may be used together. In this embodiment, a case where both sewage sludge and organic waste are used as biomass will be described.

[0036] The exhaust gas discharged from such a dryer may be utilized as an exhaust gas in the production method of this embodiment, or may be transferred to a system other than the production method. Generally, dried sewage sludge contains a relatively small amount of carbon (e.g., about 25 to 35% by mass), while organic waste contains a relatively large amount of carbon (e.g., about 35 to 45% by mass). Therefore, by adding organic waste to sewage sludge, the amount of carbonized material obtained in the carbonization process can be increased. The mixing ratio of the sewage sludge and the organic waste can be appropriately adjusted, and for example, the mass ratio of the sewage sludge to the organic waste may be in the range of 0.01 to 99.

[0037] In addition to carbon, sewage sludge and organic waste may contain alkali metals and alkaline earth metals including sodium, potassium, lithium, cesium, calcium, magnesium, barium, etc., boron, aluminum, iron, nickel, etc., and these metals may be further added and mixed in. When these metals are contained in the raw material, it is preferable because they can promote carbonization in the carbonization step and generate reformed gas more efficiently in the reformed gasification step described below.

[0038] In this embodiment, in order to allow the sewage sludge and organic waste to contain an appropriate amount of metal, the type and amount of the sewage sludge and organic waste may be adjusted, and substances such as compounds that serve as sources of the above-mentioned metals may be mixed with the sewage sludge and organic waste. As such a metal source, for example, a metal-containing residue generated together with the reformed gas in the reforming gasification process may be used. Such a metal-containing residue is a residue separated and recovered from the reformed gas generated in the reforming gasification process.

[0039] Regarding the timing of mixing the metal source such as the metal-containing residue with the sewage sludge and the organic waste, a mixing step may be provided before the carbonization step, or the metal source and / or the metal-containing residue may be directly charged into the carbonization furnace. When the metal source is mixed before the carbonization step, for example, it may be charged into a dryer that dries the sewage sludge and the organic waste.

[0040] Methods for mixing metals with sewage sludge and organic waste include, for example, a method in which the sewage sludge and organic waste are immersed in a solution in which a metal source such as a metal-containing residue is dissolved in a solvent such as water, alcohol, ether, or hydrocarbon, and a method in which the solution is sprayed onto the sewage sludge and organic waste to support the metals on the sewage sludge and organic waste.

[0041] In the carbonization step of the present embodiment, the carbonization is promoted and the carbonization rate is increased by including the above-mentioned metals in the raw material. The content of the metal in the metal-containing residue is usually about 0.01 to 100 g, or about 0.1 to 50 g, per 1 kg of the metal-containing residue. The weight ratio of the metal-containing residue to the total of the sewage sludge and organic waste (metal-containing residue / sewage sludge+organic waste) may be in the range of 0.01 to 0.99, or 0.1 to 0.9, for example. When the metal element content of the metal-containing residue and the weight ratio of the metal-containing residue to the total of sewage sludge and organic waste are within the above ranges, the carbonization rate and tar removal rate in the carbonization process of the sewage sludge and organic waste tend to be better. By increasing the carbonization rate, it is possible to increase the production amount of carbonized products, the production amount of reformed gas, the production amount of olefins (described below), the production amount of isoparaffins, and the production amount of biojet fuel, which is the final product. In this embodiment, the content of the metal can be measured by ion chromatography, ICP emission spectrometry, and X-ray fluorescence analysis.

[0042] [Carbonization process] In the method of the present embodiment, a carbonization step is carried out in which sewage sludge and organic waste are carbonized to produce a carbonized product. In the carbonization step, the raw materials, sewage sludge and organic waste, are heated in a low-oxygen or oxygen-free state to cause pyrolysis. The pyrolysis of the raw materials produces a carbonized product and a dry distillation gas containing a low-molecular-weight fuel gas and heavy component fuel such as tar. The carbonization step of the present embodiment is carried out using a carbonization furnace.

[0043] The carbonization furnace can be appropriately selected from known carbonization furnaces, for example, a carbonization furnace equipped with an external or internal heating device, a carbonization furnace equipped with a device for transporting heated material such as a screw or a rotary, etc.

[0044] The carbonization conditions in the carbonization step of this embodiment are as follows. The heating temperature in the carbonization step is, for example, 200° C. or higher and 600° C. or lower, or 230° C. or higher and 500° C. or lower. The residence time in the carbonization step of this embodiment is, for example, from 5 minutes to 100 minutes, or from 10 minutes to 60 minutes. By pyrolyzing the raw materials, sewage sludge and organic waste, at the above heating temperature and heating time, carbonized materials can be efficiently obtained.

[0045] In the carbonization step of this embodiment, the raw material may be supplied to the carbonization furnace continuously or intermittently. The metal-containing residue may be supplied to the carbonization furnace continuously or intermittently.

[0046] [Dry distillation gas combustion process] In the manufacturing method of this embodiment, the dry distillation gas generated together with the carbonized material in the carbonization step may be separated from the carbonized material, recovered, and combusted to generate high-temperature combustion gas. Such combustion gas may be introduced into at least one of the carbonization step, the reforming gasification step described below, the olefin production step, the oligomerization reaction step, the hydrogenation step, or the step of heating water vapor by heat exchange, and used as exhaust gas for heating. Specifically, since the dry distillation gas usually contains heavy fuel components such as tar, it is transferred to an air combustion furnace or the like and burned in an air atmosphere at a temperature of 1000° C. to 1200° C., for example, to obtain high-temperature combustion gas from which the heavy fuel components have been removed. Since such combustion gas is at a high temperature, it can be transferred by various piping facilities or the like to each process of the manufacturing method of this embodiment, or to a heating process such as a dryer for sewage sludge and organic waste in an external system, and used as exhaust heat gas for heating each process.

[0047] By using the heat of the combustion gas as exhaust gas in a cascade manner for heating in each step of the manufacturing method of this embodiment, heating can be performed without heating with an external fuel (heavy oil, electricity, etc.), or by using less combustion gas than in the past by burning the external fuel with air. The steps of the manufacturing method of this embodiment that can use such exhaust gas include, for example, drying of sewage sludge and organic waste, a carbonization step (heating of the carbonization furnace), a reforming gasification step (heating of the reforming gasification furnace), a step of heat exchanging steam for heating (steam heat exchange step), a shift reaction hydrogen production step (heating of the shift reaction hydrogen production facility), an olefin production step (olefin production facility), an oligomerization reaction step (oligomerization reaction facility), and a hydrogenation step (hydrogenation facility). This will not only reduce the cost of gas production, but will also have the effect of curbing global warming by reducing CO2 emissions.

[0048] [Reformed gasification process] The method of this embodiment includes a reforming gasification process in which the carbonized material obtained in the carbonization process is gasified in the presence of 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). In the reforming gasification process of this embodiment, the following reactions occur. (1) Reaction of carbide with water vapor: C+H2O→H2+CO (2) Reaction of carbide with carbon dioxide: C+CO2→2CO (3) Shift reaction: CO + H2O → CO2 + H2 (4) Methanation reaction: C + 2H2 → CH4

[0049] In the gasification temperature range (600°C to 10,000°C) in the reformed gas process of this embodiment, the gasification reactions (1) and (2) between the carbide, steam, and carbon dioxide are particularly promoted. In addition, the reactions (3) and (4) occur concomitantly to produce the reformed gas. In this embodiment, when the gasification temperature is high, the proportion of hydrogen in the reformed gas increases relatively. In addition, by using carbon dioxide together with water vapor in the above-mentioned carbonized gasification reactions (1) and (2), it is possible to increase the amount of reformed gas produced, for example, by 1.2 to 2.5 times, compared with the case where reformed gas is produced using water vapor alone.

[0050] The water vapor used in the reforming gasification process of this embodiment can be obtained by heating water such as clean water to generate water vapor. Carbon dioxide used in the reforming gasification process of this embodiment can be introduced into the reforming gasification furnace from a system separate from the production method of this embodiment, or carbon dioxide discharged from a shift reaction hydrogen production process described later can be introduced into the reforming gasification furnace.

[0051] The amount of carbonized material supplied to the reforming gasification furnace in the reforming gasification process of this embodiment can be adjusted as appropriate to efficiently produce reformed gas, and may be, for example, 10 kg / h or more and 10,000 kg / h or less, or 50 kg / h or more and 5,000 kg / h or less. The amount of steam supplied to the reforming gasification furnace can be adjusted as appropriate, but for example, the amount of steam supplied per 1 kg / h of carbonized material may be 0.5 kg / h or more and 10 kg / h or less, or 2 kg / h or more and 5 kg / h or less. The amount of carbon dioxide supplied to the reforming gasification furnace can be adjusted as appropriate. For example, the amount of carbon dioxide supplied per 1 kg / h of carbonized material is set to 0.1 Nm 3 / h or more 10Nm 3 / h or less, or 0.5Nm 3 / h or more 5Nm 3 / h or less. In addition, the ratio of the carbon dioxide supply amount to the total of the water vapor supply amount and the carbon dioxide supply amount (CO2 supply amount ÷ (water vapor supply amount + carbon dioxide supply amount)) can be, for example, 1 vol.% or more and 85 vol.% or less, or 10 vol.% or more and 60 vol.% or less.

[0052] In the reforming gasification step of the embodiment, the temperature of the reforming gasification furnace can be appropriately adjusted so as to efficiently produce the reformed gas, and may be, for example, 600° C. or higher and 1000° C. or lower, or 800° C. or higher and 900° C. or lower. As a heating means for the reforming gasification furnace, for example, the combustion gas obtained by burning the above-mentioned dry distillation gas may be used as exhaust gas for heating.

[0053] The steam is heated, for example, in a heat exchanger that heats clean water to a range of 350°C to 800°C, and then supplied to the reforming gasification furnace. When the clean water is heated by heat exchange using a heat exchanger or the like, the exhaust heat gas from the reforming gasification furnace may be introduced into the heat exchanger for heating (steam heat exchange process). Furthermore, the exhaust heat gas from the heat exchanger that heated the clean water may be introduced into another process (for example, an olefin production process, an oligomerization reaction process, a shift reaction hydrogen production process, etc.) and used for heating. In the method for producing biojet fuel of this embodiment, by utilizing the exhaust gas for heating in other processes, in addition to the economic effect of reducing the production costs of reformed gas, olefins, and biojet fuel, it is possible to contribute to the suppression of global warming by reducing carbon dioxide emissions.

[0054] The pressure in the reforming gasification furnace in the reforming gasification step can be appropriately adjusted, and may be, for example, 0.05 MPa or more and 0.5 MPa or less.

[0055] The reformed gas obtained in the reformed gasification process of this embodiment contains hydrogen (H2) and carbon monoxide (CO), and typically contains hydrogen (H2), carbon monoxide (CO), methane (CH4) and carbon dioxide (CO2). The range of the hydrogen content in the reformed gas may be, for example, 25 vol. % or more and 75 vol. % or less, or 35 vol. % or more and 65 vol. % or less. The range of the carbon monoxide content in the reformed gas is, for example, 20 vol. % or more and 60 vol. % or less, or 25 vol. % or more and 50 vol. % or less. The total content of hydrogen and carbon monoxide in the reformed gas may be in the range of, for example, 60 vol. % or more and 100 vol. % or less, or 70 vol. % or more and 90 vol. % or less. The range of the methane content in the reformed gas is, for example, 0.1 vol % or more and 10 vol % or less, or 0.5 vol % or more and 5 vol % or less. The range of the carbon dioxide content in the reformed gas is, for example, 1 vol. % or more and 35 vol. % or less, or 10 vol. % or more and 25 vol. % or less. The content (volume %) of each component is the value at 25° C. (room temperature) and 1 atmospheric pressure.

[0056] [Separation and recovery process] In this embodiment, a separation and recovery process is provided in which a metal-containing residue generated together with the reformed gas in the reformed gasification process is separated and recovered from the reformed gas, and the recovered metal-containing residue is mixed with the biomass. That is, in the reforming gasification process, the metals contained in the charcoal remain as metal-containing residue, and the metal-containing residue is separated from the reformed gas and recovered. As a recovery method, for example, the reformed gas containing the metal-containing residue discharged from the reforming gasification furnace is separated into the reformed gas and the metal-containing residue using a separation device such as a cyclone dust collector, and the separated metal-containing residue is recovered. Such metal-containing residues can be recycled and supplied before being introduced into the carbonization process, for example, to a location that receives the biomass (receiving vessel, etc.), to a stage where the biomass is mixed and dried (mixing device, dryer, etc.), or simultaneously with the carbonization process (inside the carbonization furnace), and by being mixed with sewage sludge and organic waste as described above, emissions from within the system of the manufacturing method of this embodiment can be reduced.

[0057] The metal-containing residue is formed by recovering metals contained in sewage sludge and organic waste as residue, and therefore contains at least one element selected from the group consisting of metals contained in the raw materials, i.e., metals contained in the sewage sludge and organic waste described above, such as alkali metals and alkaline earth metals such as sodium, potassium, lithium, calcium, magnesium, and barium, boron, aluminum, iron, and nickel.

[0058] The reformed gas from which the metal-containing residue has been removed by the separation device may be used for the production of biojet fuel, and may also be used for other purposes, such as power generation and hydrogen production in a gasification power generation facility.

[0059] [Gas refining process] The manufacturing method of this embodiment may include a gas purification step for purifying the reformed gas obtained in the reformed gasification step. In the gas purification step, it is preferable to remove components such as sulfur-containing components contained in the reformed gas. The reformed gas may contain sulfur-containing components such as hydrogen sulfide and COS derived from biomass raw materials. These sulfur-containing components may act as catalyst poisons, and may cause a decrease in catalytic activity and a loss of stability in the olefin production step and oligomerization reaction step described below. Therefore, the stability of catalytic activity in each step may be improved by removing such sulfur-containing components.

[0060] For example, a known gas purifier can be used for gas purification. For example, a gas purification 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 is preferably used. By contacting the reformed gas with such a gas purification member, the sulfur-containing components are bonded to the metal and the porous carrier and are chemically removed from the reformed gas. The gas purifier is not limited to the above-mentioned type that uses chemical adsorption, but may be a gas purifier that includes a known gas adsorbent such as activated carbon or various zeolites. In addition to the sulfur-containing components, the gas purification may also remove nitrogen-containing components such as ammonia and NOx, and chlorine-containing components such as HCl.

[0061] [Olefin manufacturing process] The production method of this embodiment includes an olefin production step of contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms. In the olefin production process, the reformed gas obtained in the reforming gasification process (which may be a reformed gas purified through a gas purification process) is first contacted with a methanol synthesis catalyst to produce methanol from H2, CO, CO2, and CH4 contained in the reformed gas. The methanol is then contacted with a mesoporous catalyst to produce a mixed gas of ethylene (C2H4), propylene (C3H6), and butene (C4H8), i.e., a gas containing olefins with carbon numbers of 2 to 4 (hereinafter also referred to as C2 to C4 olefins).

[0062] As the methanol synthesis catalyst, a known methanol synthesis catalyst can be used, and examples thereof include a catalyst containing at least one element selected from the group consisting of copper, zinc, chromium, manganese, scandium, lithium, sodium, potassium, cesium, magnesium, barium, platinum, palladium, iridium, molybdenum, tungsten, vanadium, zirconium, hafnium, titanium, yttrium, cerium, and lanthanum (hereinafter also referred to as element (1)). These elements (1) may be supported on a carrier, for example, a porous carrier made of a porous oxide such as silica or alumina. By selecting an appropriate element from the above elements (1), or in some cases by selecting a plurality of elements, the amount and selectivity of methanol produced can be improved. When a methanol synthesis catalyst using a carrier is used, the amount of element (1) supported is, for example, 0.01 to 10 mass%, preferably 0.1 to 5 mass%, where the amount of element (1) supported is the ratio of the total mass of element (1) to the mass of the carrier.

[0063] The methanol synthesis catalyst can be produced by a known method. When producing a methanol synthesis catalyst in which element (1) is supported on a carrier, a solution containing element (1) may be supported on the carrier. The element (1) solution can be supported simultaneously or sequentially by a method such as immersion, dropping, coating, or spraying in a predetermined temperature range. A specific example of a method for producing a methanol synthesis catalyst includes a method in which a catalyst precursor containing element (1) is dissolved in a solvent, the solution is impregnated into a support, and the support is activated to produce a methanol synthesis catalyst. Examples of catalyst precursors include salts of element (1), such as the hydrochloride, nitrate, formate, acetate, oxalate, citrate, lactate, malate, and alkoxide salts. Solvents include, for example, ethanol, methanol, ethers, and water. Examples of the activation method include a method of gradually increasing the temperature in an oxygen-containing atmosphere in a temperature range of 250 to 600° C., and a method of gradually increasing the temperature in a hydrogen gas atmosphere in a temperature range of 100 to 450° C. In addition, the hydrogen activation treatment may be a reduction treatment using a reducing agent such as hydrazine or boron hydride. The selection of the catalyst precursor, the catalyst preparation process, and the activation treatment conditions are not limited to these.

[0064] As the mesoporous catalyst, known catalysts can be used, and examples thereof include mesoporous zeolites ZSM-5, ZSM-11, SAPO-34, and erionite, which are characterized by a pore diameter of 0.36 to 0.55 nm x 0.50 to 0.56 nm, and mesoporous catalysts containing mesointerlayer clay minerals, which are characterized by an interlayer distance of 0.35 to 0.56 nm. In this embodiment, the mesoporous catalyst is preferably treated with a salt of at least one element selected from phosphoric acid, boric acid, and alkali metals and alkaline earth metals such as lithium, sodium, potassium, rubidium, cesium, magnesium, calcium, strontium, barium, etc. This can improve the selectivity and production amount of olefins.

[0065] The mesoporous catalyst can be produced by a known method. A specific example of the production method is a method in which a catalyst precursor containing the above-mentioned elements is dissolved in a solvent, the obtained solution is impregnated into a support, and an activation process is performed to obtain an activated mesoporous catalyst. Catalyst precursors include salts of the above-mentioned elements, such as the hydrochlorides, nitrates, and organic acid salts of acetate, oxalate, citrate, lactate, and the like. Examples of the solvent include ethanol, methanol, and water. Examples of methods for catalyst activation and activation treatment include a method in which the temperature is raised stepwise in the temperature range of 250 to 600°C in an oxygen-containing atmosphere, and a method in which the temperature is raised stepwise in the temperature range of 100 to 450°C in a hydrogen gas atmosphere. The selection of the catalyst precursor, the process for producing the activated catalyst, and the activation and activation treatment conditions are not limited to those mentioned above.

[0066] The methanol synthesis catalyst and the mesoporous catalyst can be used separately or as a composite catalyst in which both are mixed. In this embodiment, in terms of olefin yield and selectivity, it is preferable to use a composite catalyst in which a methanol synthesis catalyst and a mesoporous catalyst are physically mixed. When a composite catalyst is used, the olefin production amount and olefin selectivity can be improved.

[0067] The volume ratio of the methanol synthesis catalyst to the mesoporous catalyst in the composite catalyst (methanol synthesis catalyst / mesoporous catalyst volume ratio) is, for example, 0.1 to 5, or 0.2 to 2, and the like. When the volume ratio of the methanol synthesis catalyst / mesoporous catalyst is within the above range, the methanol yield can be improved, and the olefin selectivity and the amount of olefin produced can be improved. The composite catalyst can be used in a fixed bed, fluidized bed, or slurry type catalytic reactor in which it is dispersed in an organic solvent such as hexane, heptane, or octane. In particular, when the catalyst is installed in a slurry type catalytic reactor, the uniformity of the reaction layer temperature is improved, and the olefin production activity is stabilized.

[0068] The reformed gas to be introduced into the olefin production process may be pressurized to a predetermined reaction pressure by a pressure booster or other pressure booster, and may be continuously circulated and supplied. The reaction pressure of the reformed gas in the olefin production process is, for example, 0.1 to 5 MPa, or 1 to 3.5 MPa. The reaction temperature is, for example, 200 to 500° C., or 250 to 450° C. The space velocity of the reformed gas (SV: synthesis gas velocity L / h / catalyst volume L) is, for example, 1000 to 35000 h -1 , or 3000~25000h -1 etc. In the olefin production process of this embodiment, for example, an olefin selectivity of 65 to 95% and an olefin yield (STY: kg / L-cat / h) of 0.25 to 1.5 kg / L-cat / h can be obtained. Under the typical reaction conditions of this embodiment, the production selectivities of olefins having 2 to 4 carbon atoms can be 25 to 50% ethylene (C2), 25 to 45% propylene (C3), and 10 to 20% butene (C4).

[0069] In the olefin production process, the reaction gas may be cooled by the internal cooling device 56 to condense and separate the moisture generated in the reaction, and then discharged outside the system. In this case, it is possible to improve the efficiency of olefin production and stabilize the catalytic activity.

[0070] The reaction gas generated in the olefin production process contains light gases (carbon monoxide, methane, carbon dioxide) in addition to the C2-C4 olefins. The light gases can be separated by the distillation separator 52, and the separated carbon monoxide and methane can be used in the shift reaction hydrogen production process.

[0071] [Oligomerization reaction process] The production method of this embodiment includes an oligomerization reaction step of oligomerizing the olefin to produce an iso-oligomer having 6 to 16 carbon atoms (hereinafter, also referred to as a C6 to C16 iso-oligomer). In the oligomerization reaction step, the olefins generated in the olefin production step are heated and pressurized in the presence of a metal complex catalyst to produce iso-oligomers having 6 to 16 carbon atoms. Specifically, C6 to C16 iso-oligomers are obtained by iso-oligomerizing ethylene (C2), propylene (C3), and butene (C4).

[0072] The catalyst and reaction conditions in the oligomerization reaction step of the present embodiment can be appropriately selected from known catalysts and reaction conditions within a range, and are not particularly limited. For example, the C6 to C16 iso-oligomers can be obtained in a reactor under heating and pressurizing conditions of 120 to 250° C. and 2 to 5 MPa, etc., in the presence of a metal complex catalyst containing a metal such as Co, Ti, Zr, Al, etc. In this embodiment, the light olefins having 2 to 5 carbon atoms generated simultaneously with the iso-oligomers in the oligomerization reaction step may be separated and recovered from the iso-oligomers by a separation and recovery means such as a distiller, and returned to the oligomerization reaction step. By recycling the recovered light olefins to the oligomerization reaction step, the production amount and yield of the target iso-oligomers having 6 to 16 carbon atoms can be improved.

[0073] [Hydrogenation process] The production method of this embodiment includes a hydrogenation step of hydrogenating the iso-oligomers to produce isoparaffins and producing a biojet fuel containing the isoparaffins. In the hydrogenation step, the iso-oligomers produced in the oligomerization reaction step are hydrogenated to produce isoparaffins having a carbon number of 6 to 16. The catalyst and reaction conditions in the hydrogenation step of this embodiment can be appropriately selected from known ones and ranges and are not particularly limited. For example, in the presence of a noble metal catalyst containing platinum, palladium, iridium, etc., in a reactor under reaction conditions of 250 to 350°C and 1 to 5 MPa, the C6 to C16 iso-oligomers are hydrogenated to produce C6 to C16 isoparaffins. Such isoparaffins are preferably produced at a conversion rate of 85 to 90%. Such C6 to C16 isoparaffins are used as biojet fuel.

[0074] [Biojet fuel] The biojet fuel produced by the production method of this embodiment is isoparaffin having 6 to 16 carbon atoms.

[0075] In the manufacturing method of this embodiment, the carbonization gas generated together with the carbonized material in the carbonization process may be combusted and introduced into at least one of the processes of the carbonization process, the reforming gasification process, the steam heat exchange process, the olefin production process, and the oligomerization reaction process. In this way, by recycling the heat and products generated within the system, such as by using the dry distillation gas as exhaust heat gas in each process and by mixing the metal-containing residue generated in the reforming gasification process with the raw material, it is possible to reduce emissions outside the system and lighten the environmental burden.

[0076] In the method for producing biojet fuel of this embodiment, the yield of the charred material can be increased by using a metal-containing residue in the carbonization step. In addition, the yield of the reformed gas can be increased by performing mixed reformed gasification of the charred material using carbon dioxide together with water vapor in the reformed gasification step. As a result, the yield of iso-oligomers having 6 to 16 carbon atoms obtained by oligomerization reaction of olefins having 2 to 4 carbon atoms for biojet fuel and isoparaffins obtained by hydrogenating the iso-oligomers increases, which results in a reduction in the production cost of the biojet fuel and an efficient production of the biojet fuel.

[0077] (Second embodiment: method for producing biojet fuel) The method for producing biojet fuel in this embodiment is similar to the method for producing biojet fuel shown in the first embodiment above, but further includes a shift reaction hydrogen production process in which carbon monoxide and methane in the reaction gas generated in the olefin production process are reacted with steam to produce hydrogen and carbon dioxide.

[0078] [Shift reaction hydrogen production process] The production method of this embodiment may include a shift reaction hydrogen production step in which carbon monoxide and methane in the reaction gas generated in the olefin production step are reacted with steam to produce hydrogen and carbon dioxide. In the shift reaction hydrogen production process, a shift reaction (reaction 5 below) and a methane reforming reaction (reaction 6 below) are carried out to generate a mixed gas containing hydrogen and carbon dioxide. (5) Shift reaction: CO+H2O→CO2+H2 (6) Methane reforming reaction: CH4 + 2H2O = 4H2 + CO2

[0079] In the production method of this embodiment, the light gases (carbon monoxide, methane and carbon dioxide) separated and recovered from the olefins generated in the olefin production step are introduced into a shift reaction hydrogen production step. Such light gas is brought into contact with a shift reaction hydrogen production catalyst in the coexistence of steam, whereby a mixed gas containing hydrogen and carbon dioxide is produced by the shift reaction and methane reforming reaction.

[0080] In the shift reaction hydrogen production process of this embodiment, a shift reaction and a methane reforming reaction are carried out in the presence of a shift reaction hydrogen production catalyst, so that a mixed gas consisting of hydrogen and carbon dioxide can be efficiently produced at a relatively low temperature.

[0081] Examples of the shift reaction hydrogen production catalyst include those containing at least one element selected from iron, ruthenium, nickel, copper, zinc, potassium, lithium, magnesium, chromium, cobalt, molybdenum, zirconia, titanium, cerium, lanthanum, and neodymium, and a porous oxide support. Any of these elements can be selected, and examples include composite catalysts containing at least one element serving as a catalyst for the shift reaction, such as lithium, magnesium, chromium, copper, zinc, potassium, etc., and at least one element serving as a catalyst for the methane reforming reaction, such as iron, ruthenium, nickel, cobalt, molybdenum, zirconia, titanium, cerium, lanthanum, neodymium, etc. The carrier can be appropriately selected from known catalyst carriers, and examples thereof include ceramics containing alumina, magnesium oxide, silicon oxide, etc., and porous oxides such as titanium oxide.

[0082] In the shift reaction hydrogen production process of this embodiment, the high-temperature combustion gas obtained in the above-mentioned combustion process of the dry distillation gas may be introduced and used as exhaust gas for heating.

[0083] The treatment conditions for the shift reaction in this embodiment are as follows. The heating temperature may be, for example, in the range of 250° C. or more and 600° C. or less, or 300° C. or more and 450° C. or less. The pressure in the shift reaction hydrogen production process of this embodiment may be, for example, 0.05 MPa to 5 MPa, or 0.09 MPa to 1 MPa. The residence time in the shift reaction hydrogen production process of this embodiment is, for example, from 1 minute to 100 minutes, or from 5 minutes to 50 minutes. The gas hourly space velocity (GHSV) of the reformed gas relative to the catalyst is, for example, 100 to 5000 h -1 , or 500~3000h -1 The following can be mentioned: By carrying out the shift reaction hydrogen production process under the above reaction conditions, a mixed gas containing hydrogen and carbon dioxide at high concentrations can be obtained more efficiently.

[0084] As described above, carbon dioxide is produced together with hydrogen in the shift reaction hydrogen production process. The produced carbon dioxide may be separated from the hydrogen and introduced into the reformed gasification process. The step of separating hydrogen and carbon dioxide can be carried out in a hydrogen separation step following the shift reaction hydrogen production step.

[0085] The hydrogen obtained may be compressed under high pressure to produce a compressed gas, or may be cooled to produce a liquefied gas. The separated carbon dioxide may be transported to the reforming gasification step by a transport facility and recycled as the carbon dioxide used in the reforming gasification.

[0086] [Hydrogen separation process] In this embodiment, a hydrogen separation step may be provided. In the hydrogen separation step of this embodiment, the mixed gas containing high concentrations of hydrogen and carbon dioxide obtained in the shift reaction hydrogen production step is separated into hydrogen and carbon dioxide using a gas separation and purification device or the like as a gas separation and purification means to obtain hydrogen. Such hydrogen may be stored in a hydrogen holder or the like. In addition, hydrogen may be mixed with reformed gas, the concentration of which is adjusted, and then supplied to the olefin production step. Examples of the gas separation and purification means include a PSA gas separation device and a ceramic membrane gas separation device. Either one of these gas separation devices may be used, or both may be used.

[0087] When the hydrogen obtained in the shift reaction hydrogen production process of the present embodiment is supplied as a mixed gas to an olefin production process, the H2 / CO volume ratio in the mixed gas is adjusted to, for example, 1 to 3 or 1.5 to 2.5, whereby the olefin production amount and olefin production selectivity in the olefin production process can be significantly improved.

[0088] In the production method of this embodiment, a water electrolysis step using water electrolysis equipment may be provided in order to obtain hydrogen necessary for adjusting the H2 / CO gas ratio of the reformed gas to be supplied to the olefin production step. Commercially available electricity can be used as the power for such water electrolysis equipment, but electricity obtained from renewable energy sources such as solar and wind power generation or nuclear reactor power generation energy may also be used in order to reduce CO2 emissions from the system in the production method for biojet fuel of this embodiment.

[0089] The production method of this embodiment provides all the same advantages as the production method of the first embodiment, and further provides the following advantages by including a shift reaction hydrogen production step. That is, by introducing the carbon dioxide generated in the shift reaction hydrogen production process into the reforming gasification process, the yield of the reformed gas generated in the reforming gasification process can be increased. As a result, the production cost of biojet fuel can be reduced, and biojet fuel can be produced efficiently.

[0090] Also, in the manufacturing method of this embodiment, the carbonization gas generated together with the carbonized material in the carbonization process may be combusted to generate combustion gas, and the combustion gas may be used as a heat source in at least one of the processes of the carbonization process, the reforming gasification process, the process of heat exchanging water vapor, the shift reaction hydrogen production process, the olefin production process, and the oligomerization reaction process. In this way, the yield of reformed gas can be improved by recycling the combustion gas and metal-containing residues generated in the system, such as using the dry distillation gas as an exhaust gas and a heat source in each process, and recycling and mixing the metal-containing residues generated in the reformed gasification process with the biomass raw material to improve the carbonization rate of the charcoal, etc. As a result, the production yield of biojet fuel can be increased and the production cost can be reduced.

[0091] (Third embodiment: biojet fuel production device) The biojet fuel production apparatus (hereinafter simply referred to as the production apparatus) of this embodiment will be described with reference to FIG. The production apparatus 100 of this embodiment includes a carbonization furnace 20 for introducing biomass 1 (sewage sludge and organic waste) and producing a carbonized material, a reforming gasification furnace 30 for introducing the carbonized material 2 obtained in the carbonization furnace 20 and carrying out a mixed gasification reaction with water vapor and carbon dioxide to produce a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide, an olefin production facility 50 for introducing the reformed gas obtained in the reforming gasification furnace 30 and bringing it into contact with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms, and an olefin production facility 51 for introducing the olefins and producing oligomers. The biojet fuel production system includes an oligomerization reaction system 42 that produces iso-oligomers by a merization reaction, a distillation purification system 43 that introduces the iso-oligomers and separates by distillation the iso-oligomers having 6 to 16 carbon atoms, a light olefin recycle pipe 45 that recycles and supplies the remaining light olefins (C2 to C5 olefins) to the oligomerization reaction system 42, and a hydrogenation system 44 that introduces the C6 to C16 iso-oligomers and hydrogenates them to produce biojet fuel 90 consisting of isoparylene having 6 to 16 carbon atoms.

[0092] (Renewable jet fuel production facility) A biojet fuel production apparatus 100 for producing biojet fuel according to this embodiment shown in FIG. 1 will be described. First, the manufacturing apparatus of this embodiment is equipped with a biomass receiver 11 that receives biomass 1 supplied from outside, and a rotary kiln dryer 12 (dryer) that dries the biomass 1 received by the biomass receiver 11, as equipment for carbonizing biomass. The biomass receiver 11 is equipped with a biomass supply facility 91 that supplies biomass 1 into the receiver 11, and a biomass supply amount adjustment means 80 that supplies biomass 1 from the receiver 11 to the dryer 12. The biomass supply amount adjustment means 80 is equipped with a means for adjusting the amount of biomass 1 supplied to the dryer 12 and for measuring the moisture content. The dryer 12 is connected to the carbonization furnace 20, and is configured so that the dried biomass 1 from the dryer 12 is transported to the carbonization furnace 20.

[0093] The carbonization furnace 20 is equipped with a transfer device such as a screw-type biomass transfer facility and a heating section (not shown) that uses combustion gas as a heat source via a combustion gas piping 72. The carbonization furnace 20 is equipped with a lower outlet for discharging the generated carbonized material 2 and an upper outlet for discharging the dry distillation gas generated in the carbonization furnace 20. The upper outlet is connected to the air combustion furnace 60 via a piping. A carbonized material supply piping is connected to the lower outlet, and the carbonized material can be fed into the reforming gasification furnace 30 via a carbonized material supply amount regulator 81 and a carbonized material supply device 92 provided on the carbonized material supply piping.

[0094] The air combustion furnace 60 is configured to combust the dry distillation gas 5 (containing tar) generated in the carbonization furnace 20 with an air blower 41 to generate high-temperature combustion gas 6.

[0095] Next, a description will be given of the reforming gasification furnace 30 which generates reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide by subjecting carbide to a gasification reaction with water vapor and carbon dioxide. The reforming gasification furnace 30 that performs the reforming gasification is configured to generate a reformed gas 8 (a mixed gas of H2, CO, CH4, and CO2) by gasifying the carbide 2 together with steam 7 and carbon dioxide 9. The reforming gasification furnace 30 includes an inner cylinder 30a and an outer cylinder 30b surrounding the inner cylinder. The carbide 2 is accommodated in the inner cylinder 30a. A combustion gas pipe (reforming gasification furnace) 73 from the air-fuel furnace 60 is connected to the gap between the inner cylinder 30a and the outer cylinder 30b, and a combustion gas for heating is supplied via the combustion gas pipe 73. The inner cylinder 30a is heated by the combustion gas, and the carbide, water vapor, and carbon dioxide are heated by the heat from the inner cylinder 30a, and reforming gasification proceeds.

[0096] A steam supply pipe 33 for supplying steam to the inside of the reforming gasification furnace 30 and a CO2 supply pipe 32 for supplying carbon dioxide are connected to the reforming gasification furnace 30. A CO2 supply regulator 83 is provided in the CO2 supply pipe 32 to regulate the amount of CO2 supplied to the reforming gasification furnace 30. The steam supply pipe is provided with a steam heat exchanger 31 and a steam supply amount regulator 84 to regulate the temperature and amount of steam supplied to the reforming gasification furnace 30 .

[0097] The manufacturing apparatus 100 of this embodiment is equipped with a separation and recovery means for separating and recovering the metal-containing residue generated together with the reformed gas in the reforming gasification furnace 30 from the reformed gas, and an introduction means for introducing the metal-containing residue recovered by the separation and recovery means into the biomass introduced into the carbonization furnace 20. Specifically, a reformed gas pipe 35 is connected to the upper part of the reforming gasification furnace 30, which discharges the reformed gas generated through a reformed gas supply device 93, and is configured to transport the reformed gas to a dust collector 34. The dust collector 34 is connected via piping to a gas purifier 36, a reformed gas supply regulator 86, a gas mixture preparer 89, and a pressurized gas circulation system 88, and is configured to introduce the reformed gas into the olefin production system 50. The gas purifier 36 is configured to be capable of removing sulfur- and chlorine-containing components from the reformed gas, and uses a known gas adsorbent or the like as described above. The reformed gas discharged from the dust collector 34 is pressurized by a pressurized gas circulation system 88 such as a booster to a reaction pressure required in the olefin production facility 50 .

[0098] The dust collector 34 is equipped with a metal-containing residue separation and recovery equipment 94 that separates and recovers the metal-containing residue contained in the reformed gas from the reformed gas. A metal-containing residue receiver 38 that stores the metal-containing residue after separation and recovery in the dust collector 34 is connected via a metal-containing residue discharge pipe 39. A metal-containing residue supply equipment 37 that transfers the recovered metal-containing residue to the biomass receiver 11 is connected to the metal-containing residue receiver 38. A metal-containing residue supply amount adjuster 82 is connected to the metal-containing residue supply equipment 37 and is configured to adjust the amount of metal-containing residue supplied to the biomass receiver 11.

[0099] Next, a C2-C4 olefin production facility 50 for producing olefins having 2 to 4 carbon atoms from the reformed gas (hereinafter, also referred to as olefin production facility) will be described. The above-mentioned composite catalyst 63 is disposed inside the olefin production facility 50 so as to be in contact with the reformed gas introduced inside. The olefin production facility 50 is also provided with an internal cooling device 56 for adjusting the inside to a temperature suitable for the reaction. The composite catalyst 63 is supplied from a catalyst mixture preparer 57 that prepares the composite catalyst 63 by mixing a methanol synthesis catalyst 58 and a mesoporous catalyst 59 to an olefin production facility 50 via a catalyst mixture amount adjuster 95 and a composite catalyst supply pipe 62 .

[0100] The olefin production facility 50 is configured to transfer the olefins produced as a result of the reaction therein to the oligomerization reaction facility 42 via a distillation separator 52 which separates the olefins produced. The distillation separator 52 is connected to a reaction gas pipe 77 for transferring the gas containing carbon monoxide and methane separated from the olefins to a shift reaction hydrogen production facility 53 .

[0101] Next, an oligomerization reaction facility for producing an iso-oligomer having 6 to 16 carbon atoms by oligomerization reaction of olefins having 2 to 4 carbon atoms will be described. The oligomerization reaction equipment 42 as an oligomerization reaction equipment is configured to carry out an oligomerization reaction of olefins introduced into the inside via a C2-C4 olefin piping 47 to produce iso-oligomers having 6 to 16 carbon atoms. The oligomerization reaction equipment 42 contains the oligomerization catalyst as described above, and is equipped with a heating and pressurizing device capable of adjusting the temperature, pressure, etc. to values ​​appropriate for the oligomerization reaction. The oligomerization reaction equipment 42 is connected to a C6 to C16 iso-oligomer pipe 48 that transfers the iso-oligomers produced by the reaction to a hydrogenation equipment 44 via a distillation purification equipment 43.

[0102] Next, the hydrogenation equipment 44 that hydrogenates the iso-oligomers to produce isoparaffins and then produces a biojet fuel containing the isoparaffins will be described. The hydrogenation equipment 44 contains the hydrogenation catalyst as described above, and is equipped with a heating and pressurizing device capable of adjusting the temperature, pressure, etc. to the levels appropriate for the hydrogenation reaction. In the hydrogenation equipment 44, biojet fuel 90 consisting of C6 to C16 isoparaffins is obtained and discharged from a C6 to C16 isoparaffin piping 49.

[0103] (Hydrogen and carbon dioxide circulation equipment) Of the production apparatus of this embodiment, a facility for circulating hydrogen and carbon dioxide generated during the production of biojet fuel will be described. The biojet fuel production apparatus 100 of this embodiment further includes a shift reaction hydrogen production facility 53 that produces hydrogen and carbon dioxide by reacting carbon monoxide and methane in the reaction gas generated in the olefin production facility 50 with water vapor. The provision of such a shift reaction hydrogen production facility 53 is optional. The shift reaction hydrogen production equipment 53 is configured to introduce light gas containing carbon monoxide and methane, which has been separated from the C2-C4 olefins in the distillation separator 52 from the reaction gas discharged from the olefin production equipment 50, into the shift reaction hydrogen production equipment 53 via the distillation separator 52. A shift reaction hydrogen production facility 53 is provided inside the facility, and is configured to generate a mixed gas containing hydrogen and carbon dioxide by the shift reaction described above. The shift reaction hydrogen production facility 53 is connected to an H2 / CO2 gas pipe 64 for transporting the generated mixed gas to a gas separation and purification facility 54.

[0104] The gas separation and purification equipment 54 is provided with a CO2 supply pipe 32 so as to separate CO2 from the mixed gas generated in the shift reaction hydrogen production equipment 53 and introduce the CO2 into the reforming gasification furnace 30 via a CO2 supply regulator 83. As the gas separation and purification equipment 54, a separation device such as a PSA (Pressure Swing Adsorption) type gas separation device or a ceramic membrane type gas separation device is used.

[0105] The hydrogen separated in the gas separation and purification equipment 54 is transferred to the hydrogen holder 55 via a hydrogen supply pipe 79 . The hydrogen holder 55 is connected to the gas mixture preparer 89 and the water electrolysis equipment 40 . The water electrolysis equipment 40 electrolyzes the clean water 4 to generate hydrogen, and the hydrogen generated in the water electrolysis equipment 40 is transferred to the hydrogen holder 55 via the hydrogen supply pipe 51 and the water electrolysis hydrogen supply regulator 87, and is supplied to the gas mixture adjuster 89 via the hydrogen supply pipe 78 to adjust the H2 / CO gas ratio in the reformed gas. This is configured to increase the H2 / CO volume ratio in the reformed gas.

[0106] (Equipment for circulating exhaust gas) Next, a description will be given of an exhaust gas circulation facility provided to utilize the heat generated in the manufacturing apparatus of this embodiment in each process. The biojet fuel production apparatus 100 of this embodiment is provided with multiple combustion gas pipes so that the heat generated in each process can be used for heating within the apparatus as exhaust gas. The multiple combustion gas pipes in this embodiment are composed of pipes that transport the combustion gas 6 generated by the air fuel furnace 60 that burns the dry distillation gas discharged from the carbonization furnace 20 to each device. Such multiple combustion gas pipes include a combustion gas pipe 70 connected to an air fuel furnace 60 and a combustion gas flow regulator 61, and through the combustion gas pipe 71 that supplies combustion gas to the 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 gasification furnace 30, a combustion gas pipe 75 that supplies combustion gas to the olefin production equipment 50, a combustion gas pipe 96 that supplies combustion gas to the oligomerization reaction equipment, a combustion gas pipe 97 that supplies combustion gas to the hydrogenation reaction equipment, and a combustion gas pipe 76 that supplies combustion gas to the shift reaction hydrogen production equipment 53. Also included is a combustion gas pipe 74 that supplies the combustion gas generated in the reforming gasifier 30 to the steam heat exchanger 31 . By adopting such a configuration for transferring the combustion gas to each device, the high-temperature gas generated in the device 100 of this embodiment can be recycled for heating in each device.

[0107] The method of producing biojet fuel using the biojet fuel production apparatus 100 of this embodiment may be a method as shown in the production methods of the first and second embodiments above. Also, the production method may use all or some of the functions of the production apparatus 100 of this embodiment. That is, the embodiment of the production method and the embodiment of the production apparatus are shown as independent and separate embodiments.

[0108] The method and device for producing biojet fuel according to the present embodiment are as described above, but the embodiment disclosed herein should be considered to be illustrative and not restrictive in all respects. The scope of the present invention is indicated by the claims rather than the above description, and is intended to include all modifications within the meaning and scope of the claims. EXAMPLES

[0109] Next, examples of the present invention will be described together with comparative examples. Note that the present invention is not limited to the following examples.

[0110] (Test 1) A test was conducted to produce jet fuel using the jet biofuel production equipment configured as shown in Figure 1. In this test, sewage sludge and organic waste as biomass were fed into a dryer and a carbonization furnace, and carbonization was carried out in the carbonization furnace, the reforming gasification reaction in the reforming gasification furnace, the shift reaction and methane reforming reaction in the shift reaction hydrogen production equipment, and gas separation and purification in the PSA gas separation and purification unit. The recovered hydrogen was supplied to the reformed gas to adjust the reformed gas composition to H2 / CO = 2.5 (volume ratio). The carbon dioxide separated in the gas separation device was recycled and supplied to the reforming gasification furnace. The metal-containing residue separated and recovered in the cyclone dust collector was recycled and supplied to the dryer for sewage sludge and organic waste. Experimental results of the carbonization rate, reformed gas production amount, gas composition (volume %), and biojet fuel production amount in the cases where the metal-containing residue was recycled and not supplied to the sewage sludge and organic waste are shown in Example 1 and Comparative Example 1.

[0111] The specific test method is as follows. Sewage sludge (80% by mass moisture content) was fed at 30 kg per hour. Construction waste chips were fed as organic waste at 10 kg per hour. Carbonization was performed at a carbonization furnace temperature of 250 to 450°C. Reformed gasification was performed at a steam / carbide (mass ratio) of 1.5, CO2 / carbide (molar ratio) of 0.5, and a temperature of 860°C. The shift reaction hydrogen production process was performed at a temperature of 450°C and a pressure of 3.5 MPa under a shift reaction hydrogen production catalyst prepared by supporting Fe, Ru, Ni, Cu, Zn, Mg, Zr, Ti, and Ce on porous oxides. Metal-containing residues separated and collected by a cyclone dust collector were fed at 3 kg per hour into a kiln-type dryer that mixed and processed sewage sludge and construction waste chips. In this test, the olefin production process using reformed gas was carried out using a composite catalyst prepared by mixing a methanol synthesis catalyst (Cu / ZnO) and a mesoporous catalyst (SAPO-34). The reaction conditions were 380°C and 2.5 MPa. The olefin oligomerization reaction was carried out under reaction conditions of 120-250°C and 2.5-5 MPa. Hydrogenation after the oligomerization reaction was carried out under reaction conditions of 0.1 to 2.5 MPa and 250 to 450°C. The reformed gas component composition and the concentrations of CO, hydrogen, CO2, CH4 and other components in the outlet gas of the shift reaction hydrogen production unit were measured using a thermal conductivity type gas chromatograph analyzer (Shimadzu Corporation GC-14B) filled with Gaskuropack and molecular sieve 13X, and an FID gas chromatograph analyzer (Shimadzu Corporation GC-8A). The flow rate of the exhaust gas was measured using a wet gas flowmeter. The metal element contents of the metal-containing residue were measured using an ICP emission spectrometer (Shimadzu Corporation ICPS-8100) and an X-ray fluorescence analyzer (Hitachi High-Tech Corporation EA1400). The metal contents of the metal-containing residue obtained in this test were Na 35g / kg, K 85g / kg, Ca 46g / kg, Mg 27g / kg, Ba 5g / kg, Fe 7.5g / kg, and Ni 3.8g / kg. The yield of biojet fuel in the table indicates the weight (per hour) of liquid oil consisting of C6 to C16 isoparaffins obtained after hydrogenation. The results are shown in Table 1.

[0112] [Table 1] Note 1) Reformed gasification process: steam / carbide = 1.5 (weight ratio), CO2 / carbide = 0.5 (mole ratio), reaction temperature 860℃

[0113] From these results, the production volume of reformed gas (Nm 3 It was shown that the production rate (kg / h) of biojet fuel consisting of C6 to C16 isoparaffins and the production rate (kg / h) of biojet fuel consisting of C6 to C16 isoparaffins were significantly improved when the metal-containing residue was recycled (Example 1) compared to when it was not recycled (Comparative Example 1).

[0114] (Test 2) As biomass, sewage sludge and rice straw from agricultural waste were used, and tests of carbonization, reformed gasification, and biojet fuel production were conducted in the same manner as in Test 1. Sewage sludge (80% moisture content) was fed at 45 kg per hour. Rice straw was fed as organic waste at 20 kg per hour. Carbonization was performed at a carbonization furnace temperature of 250 to 420°C. The reformed gas production amount, reformed gas component composition, and biojet fuel production amount measured in Example 2, in which the reformed gasification process of the carbonized material was performed at a temperature of 900°C under mixed steam and CO2 supply conditions of steam / carbonized material (mass ratio) = 1.7 and CO2 / carbonized material (molar ratio) = 0.35, and in Comparative Example 2, in which only steam was supplied under the condition of steam / carbonized material = 1.7, are shown in Table 2.

[0115] The shift reaction hydrogen production process was carried out under the conditions of temperature 350°C and pressure 0.3MPa using a composite catalyst of Ru, Cu, Cr, K, Li, La and Nd supported on a porous oxide. In the olefin production process using the reformed gas in this test, the reaction conditions were 380°C and 2.5MPa using a composite catalyst consisting of a methanol synthesis catalyst (Cu-Pd / ZnO) and a mesoporous catalyst (ZMS-11). The olefin oligomerization reaction was carried out under reaction conditions of 120-250°C and 2.5-5MPa. Hydrogenation after the oligomerization reaction was carried out under reaction conditions of 0.1-2.5MPa and 250-450°C. The metal-containing residue separated and collected by the cyclone dust collector was mixed and fed into a dryer for sewage sludge and rice straw raw materials at a rate of 5kg per hour and carbonized. The metal contents of the metal-containing residue obtained in this test are 23g / kg Na, 65g / kg K, 50g / kg Ca, 15g / kg Mg, 2.5g / kg Ba, 0.5g / kg Li, 8.2g / kg Fe and 2.5g / kg Ni. The results are shown in Table 2.

[0116] [Table 2]

[0117] From these results, it is clear that the reformed gas (Nm 3 / h) and the production amount of biojet fuel (kg / h) were shown to be significantly increased compared to the condition where only steam was supplied (Comparative Example 2). [Industrial Applicability]

[0118] In the present invention, in the carbonization step using biomass, the manufacturing method and apparatus for manufacturing reformed gas and biojet fuel, the manufacturing efficiency of reformed gas and biojet fuel can be improved by recycling the metal-containing residue in the reformed gasification step to the biomass and recycling the carbon dioxide discharged in the shift reaction hydrogen production step to the reformed gasification furnace, thereby reducing the manufacturing cost of biojet fuel and the environmental load due to the reduction in carbon dioxide emissions. [Explanation of symbols]

[0119] 1. Biomass (sewage sludge, organic waste) 2. Carbide 3 Metal-containing residue 4 Water supply 5. Dry distillation gas (including tar) 6 Combustion gas 7. Water Vapor 8. Reformed gas 9 CO2 10 Hydrogen 11 Biomass receiver 12 Rotary kiln dryer 20 Carbonization furnace 30 Reformer gasifier 31 Steam heat exchanger 32 CO2 supply pipe 33 Steam supply pipe 34 Dust collector (cyclone) 35 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 Oligomerization Reaction Facility 43 Distillation and purification equipment 44 Hydrogenation facility 45 Light olefin recycling piping 46 C2~C4 Olefins 47 C2~C4 Olefin Piping 48 C6~C16 iso-oligomer piping 49 C6~C16 Isoparaffin Piping 50 C2~C4 olefin production facility 51 Hydrogen supply piping (water electrolysis hydrogen) 52 Distillation separator 53 Shift reaction hydrogen production facility 54 Gas separation and purification equipment (ceramic membrane separator, PSA) 55 Hydrogen Holder 56 Internal cooling system 57 Catalyst Mixing Preparator 58 Methanol synthesis catalyst 59 Mesoporous Catalysts 60 Air-fired furnace 61 Combustion gas flow regulator 62 Composite catalyst supply piping 63 Composite Catalysts 64 H2 / CO2 gas piping 70 Combustion gas piping 71 Combustion gas piping (dryer) 72 Combustion gas piping (carbonization furnace) 73 Combustion gas piping (reforming gasification furnace) 74 Combustion gas piping (water vapor heat exchanger) 75 Combustion gas piping (C2~C4 olefin production facility) 76 Combustion gas piping (shift reaction hydrogen production facility) 77 Reaction gas piping 78 Hydrogen supply piping (gas separator / purifier) 79 Hydrogen supply pipe (hydrogen holder) 80 Biomass supply adjustment measures 81 Carbide feed rate regulator 82 Metal-containing residue supply amount regulator 83 CO2 supply amount regulator 84 Steam supply regulator 85 Hydrogen supply regulator 86 Reformed gas supply regulator 87 Water electrolysis hydrogen supply amount regulator 88 Pressurized gas circulation equipment 89 Gas Mixture Adjuster 90 Biojet fuel (C6~C16 isoparaffin) 91 Biomass supply facility 92 Carbide supply device 93 Reformed gas supply equipment 94 Metal-containing residue separation and recovery equipment 95 Catalyst mixture amount regulator 96 Combustion gas piping (oligomerization reaction equipment) 97 Combustion gas piping (hydrogenation reactor) 100 Jet fuel production equipment

Claims

1. a carbonization step of carbonizing the biomass to generate a carbonized material; a reforming / gasification step of gasifying the carbide, steam, and carbon dioxide to generate a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide; an olefin production step of contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms; an oligomerization reaction step of producing an iso-oligomer having 6 to 16 carbon atoms by oligomerization of the olefin; A hydrogenation step of hydrogenating the iso-oligomers to produce isoparaffins and producing a biojet fuel containing the isoparaffins; a separation and recovery step of separating and recovering a metal-containing residue generated together with the reformed gas in the reformed gasification step from the reformed gas, and mixing the recovered metal-containing residue with the biomass.

2. 2. The method for producing a biojet fuel according to claim 1, wherein the metal-containing residue contains at least one element selected from the group consisting of alkali metals and alkaline earth metals including sodium, potassium, lithium, calcium, magnesium, and barium, boron, aluminum, iron, and nickel.

3. 3. The method for producing a biojet fuel according to claim 1 or 2, wherein the olefin production step includes a separation step of separating a reaction gas generated by contacting the reformed gas with a methanol synthesis catalyst and a mesoporous catalyst into a mixed gas containing carbon monoxide and methane and olefins having 2 to 4 carbon atoms.

4. 3. The method for producing a biojet fuel according to claim 1 or 2, further comprising a shift reaction hydrogen production process in which carbon monoxide and methane in the reaction gas generated in the olefin production process are reacted with steam to produce hydrogen and carbon dioxide.

5. 5. The method for producing a biojet fuel according to claim 4, wherein carbon dioxide generated in the shift reaction hydrogen production process is introduced into the reformed gasification process, and hydrogen generated in the shift reaction hydrogen production process is mixed with the reformed gas obtained from the reformed gasification process.

6. 5. The method for producing a biojet fuel according to claim 4, wherein the shift reaction hydrogen production step uses a shift reaction catalyst containing at least one element selected from the group consisting of iron, ruthenium, nickel, copper, zinc, potassium, lithium, magnesium, chromium, cobalt, molybdenum, zirconia, titanium, cerium, lanthanum, and neodymium, and a porous oxide support.

7. 3. The method for producing a biojet fuel according to claim 1 or 2, wherein the dry distillation gas generated together with the carbonized material in the carbonization process is combusted and introduced into at least one of the carbonization process, the reformed gasification process, the steam heat exchange process, the olefin production process, and the oligomerization reaction process.

8. 5. The method for producing a biojet fuel according to claim 4, wherein the dry distillation gas generated together with the carbonized material in the carbonization process is combusted and introduced into at least one of the carbonization process, the reformed gasification process, the steam heat exchange process, the shift reaction hydrogen production process, the olefin production process, and the oligomerization reaction process.

9. 3. The method for producing a biojet fuel according to claim 1 or 2, wherein the methanol synthesis catalyst comprises at least one element selected from the group consisting of copper, zinc, chromium, manganese, scandium, lithium, sodium, potassium, cesium, magnesium, barium, platinum, palladium, iridium, molybdenum, tungsten, vanadium, zirconium, hafnium, titanium, yttrium, cerium, and lanthanum, and a porous support.

10. The method for producing a biojet fuel according to claim 1 or 2, wherein the mesoporous catalyst comprises a porous support made of a mesoporous zeolite and a mesoporous clay mineral.

11. 3. The method for producing a biojet fuel according to claim 1 or 2, wherein the olefin production step uses a composite catalyst prepared by mixing the methanol synthesis catalyst and the mesoporous catalyst, and a mixing volume ratio of the methanol synthesis catalyst to the mesoporous catalyst in the composite catalyst is 0.1 to 5.

12. a carbonization furnace into which biomass is introduced to generate carbonized material; a reforming gasification furnace into which the carbonized material obtained in the carbonization furnace is introduced and gasified with water vapor and carbon dioxide to generate a reformed gas containing hydrogen, carbon monoxide, methane, and carbon dioxide; an olefin production facility into which the reformed gas obtained in the reforming gasification furnace is introduced and brought into contact with a methanol synthesis catalyst and a mesoporous catalyst to produce olefins having 2 to 4 carbon atoms; an oligomerization reaction facility for introducing the olefin and carrying out an oligomerization reaction to produce an iso-oligomer having 6 to 16 carbon atoms; and a hydrogenation facility for introducing the iso-oligomer obtained in the oligomerization reaction facility and hydrogenating it to obtain a biojet fuel containing isoparaffin, a separation and recovery means for separating and recovering a metal-containing residue generated together with the reformed gas in the reforming gasification furnace from the reformed gas; and a means for introducing the metal-containing residue recovered by the separation and recovery means into the biomass.

13. The biojet fuel production apparatus according to claim 12, further comprising a shift reaction facility that reacts carbon monoxide and methane in the reaction gas generated in the olefin production facility with steam to produce hydrogen and carbon dioxide.

14. The biojet fuel production apparatus according to claim 12 or 13, wherein the olefin production facility is provided with a separation means for separating the generated reaction gas into olefins having 2 to 4 carbon atoms and a gas containing carbon monoxide and methane.

15. The biojet fuel production apparatus according to claim 13 , wherein the shift reaction facility is provided with a transfer means for transferring the generated carbon dioxide to the reformer-gasifier.

16. A combustion device is provided for combusting the dry distillation gas discharged from the carbonization furnace, The biojet fuel production apparatus according to claim 12, wherein the combustion device is provided with a supply means for supplying combusted gas as a heating gas to at least one of the carbonization furnace, the reforming gasification furnace, the olefin production facility, the oligomerization reaction facility, and the hydrogenation facility.

17. A combustion device is provided for combusting the dry distillation gas discharged from the carbonization furnace, The biojet fuel production apparatus according to claim 13, wherein the combustion device is provided with a supply means for supplying combusted gas as a heating gas to at least one of the carbonization furnace, the reforming gasification furnace, the olefin production facility, the oligomerization reaction facility, the hydrogenation facility, and the shift reaction facility.

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