WO2018147281A1 - Hydrocarbon production method, production apparatus therefor, production system therefor, and biocrude production method - Google Patents

Abstract

[Problem] To provide: a hydrocarbon production method with which it is possible to efficiently manufacture a hydrocarbon by using biomass, thus suppressing a carbon resource loss; a production apparatus therefor; a production system therefor; and a biocrude production method. [Solution] The present invention is characterized by being provided with: a pre-processing step for obtaining a biocrude by performing solvolysis by mixing at least a biomass and a solvent; and a fluid catalytic cracking step for performing fluid catalytic cracking by using the biocrude obtained in the pre-processing step and a hydrogen donor as raw materials.

Description

METHOD FOR PRODUCING HYDROCARBON, DEVICE FOR PRODUCING THE SAME, SYSTEM FOR PRODUCING THE SAME, AND METHOD FOR PRODUCING BIOCRUDE

The present invention relates to a method for producing hydrocarbon, an apparatus for producing the same, a system for producing the same, and a method for producing a biocrude.

In recent years, development of alternative resources has been sought against the background of concern over depletion of fossil resources such as petroleum and the increase in energy demand. For example, using biomass such as plants as a raw material Various methods for synthesizing transportation fuels have been proposed to replace.

As a synthesis method of fuel replacing petroleum, a method of producing liquid fuel using biomass such as plants as a raw material has been researched and developed (see, for example, Patent Document 1). In the method for producing liquid fuel described in Patent Document 1, woody biomass and an organic solvent are mixed and subjected to a liquefaction process by thermal decomposition at 250 ° C. to 400 ° C., and this decomposition product is separated to obtain a liquid fuel It is what you get.

JP, 2006-063310, A

However, when producing hydrocarbons from biomass using the conventional thermal decomposition process described in Patent Document 1, a subcritical water treatment process, or a critical water treatment process, the biomass has a high oxygen content, and the biomass Due to the high temperature treatment, many inorganic gases such as carbon monoxide (CO) and carbon dioxide (CO ₂ ) are generated, and there is a problem that the loss of carbon resources contained in biomass is large.

Therefore, the present invention focuses on the problems as described above, and a method for producing hydrocarbons that can efficiently produce hydrocarbons by using biomass and suppressing loss of carbon resources, a production apparatus thereof, An object of the present invention is to provide a manufacturing system and a method of manufacturing a biocrude.

The method for producing a hydrocarbon according to the present invention comprises a pretreatment step of obtaining biocrude by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound and performing solvolysis, and the pretreatment step obtained by the pretreatment step. And a fluid catalytic cracking step of performing fluid catalytic cracking using the biocrude and the hydrogen donor as raw materials.

In the method for producing a hydrocarbon of the present invention, the solvent in the pretreatment step preferably contains an organic acid.

In the method for producing a hydrocarbon according to the present invention, the biomass may be woody biomass, and the solvent in the pretreatment step may contain the biocrude.

In the method for producing a hydrocarbon according to the present invention, the biocrude and the hydrogen donor may be separately supplied in the fluid catalytic cracking step.

The method for producing a biocrude according to the present invention is characterized in that the biocrude is obtained by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound and subjecting them to solvolysis.

An apparatus for producing a hydrocarbon according to the present invention is an apparatus for producing a hydrocarbon used in the fluid catalytic cracking step of the process for producing a hydrocarbon according to the present invention, the reactor in which the fluid catalytic cracking is performed;
A raw material supply means for supplying the raw material to the reactor, wherein the raw material supply means supplies a biocrude supply unit for supplying the biocrude; and a hydrogen donor supply unit for supplying the hydrogen donor. It is characterized by having separately.

The system for producing hydrocarbon according to the present invention uses the method for producing hydrocarbon according to the present invention, wherein the pretreatment step and the fluid catalytic cracking step are performed at places separated from each other, The biocrude obtained by the treatment process is transported and supplied to the fluid catalytic cracking process.

In the hydrocarbon production system of the present invention, the biomass may be woody biomass, and the pretreatment step may be performed at a raw wood core of the woody biomass material.

According to the method for producing hydrocarbon and the method for producing biocrude according to the present invention, biomass is pretreated by solvolysis from thermal decomposition, subcritical water treatment or supercritical water treatment which is a conventional pretreatment method. Also, when biomass is liquefied at a low temperature and it is catalytically cracked with a hydrogen donor in the subsequent fluid catalytic cracking step, deoxygenation is performed by hydrodeoxygenation to remove much oxygen as water, The production of carbon monoxide and carbon dioxide is suppressed, and the loss of carbon resources can be reduced. Thereby, hydrocarbons can be efficiently produced from biomass.

Careless mixing of the biocrude and the hydrogen donor may result in part of the biomass being precipitated as a solid. According to the hydrocarbon production apparatus of the present invention, since the biocrude and the hydrogen donor are supplied to the reactor by separate feeding units, the biocrude and the hydrogen donor are not mixed in the feeding unit. It can prevent the precipitation of biomass.

According to the hydrocarbon production system of the present invention, the pretreatment step and the fluid catalytic cracking step are performed at locations separated from each other, and the biocrude obtained by the pretreatment step is transported to the fluid catalytic cracking step. From the supply, transporting the biocrude to a facility that performs a fluid catalytic cracking process can lower the cost of transportation compared to transporting solid, bulky biomass than liquid biocrude.

It is a figure which shows the process flow of the pre-processing process concerning one Embodiment of this invention. BRIEF DESCRIPTION OF THE DRAWINGS It is a figure which shows typically the manufacturing apparatus of the hydrocarbon concerning the 1st Embodiment of this invention. It is a figure which shows typically the manufacturing apparatus of the hydrocarbon concerning the 2nd Embodiment of this invention. It is a figure which shows typically the manufacturing apparatus of the hydrocarbon concerning the 3rd Embodiment of this invention. It is a figure which shows the result of the thermogravimetric analysis in the Example of this invention. It is a figure which shows the result of the GPC measurement in the Example of this invention.

[Method for Producing Hydrocarbon, Method for Producing Biocrude, and Device for Producing Hydrocarbon]
The process for producing hydrocarbon and the apparatus for producing hydrocarbon according to the present invention will be described.

The method for producing a hydrocarbon according to the present invention comprises a pretreatment step of obtaining a biocrude by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound and performing solvolysis, and a bio obtained by the pretreatment step. The method is characterized by comprising a fluid catalytic cracking step of performing fluid catalytic cracking using crude and hydrogen donors as raw materials. Further, the method for producing biocrude according to the present invention is characterized in that the biocrude is obtained by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound and performing solvolysis. In the present invention, biocrude refers to a liquid product obtained by solvolysis in the pretreatment step. For example, the biocrude obtained by subjecting woody biomass to the pretreatment step includes methoxyphenols derived from lignin, alkylphenols such as alkylphenol, and oxygen-containing aromatic compounds such as furan derived from cellulose or hemicellulose, About 80) copolymerized high molecular compounds etc. are included.

As the hydrocarbon in the present invention, for example, an oxygen-free Drop-in fuel (a fuel which can use an existing engine or infrastructure), an aromatic compound such as benzene, toluene or xylene, ethylene, propylene or butadiene etc. So-called petrochemical products such as olefins are mentioned. However, hydrocarbons in the present invention are not limited to these.

Biomass is an organic source of biological origin excluding fossil resources. As biomass in the present invention, forest resources such as woody biomass, agricultural products processing residues and the like can be used. In the present invention, particularly, woody biomass can be suitably used.

In the pretreatment step, biomass and a solvent are mixed to perform solvolysis. For example, after biomass and a solvent are mixed in a reactor and the reactor is heated to a predetermined reaction temperature, solvolysis is allowed to proceed for a predetermined time. After the solvolysis reaction, the liquid product is recovered and made biocrude. The resulting biocrude is subjected to a fluid catalytic cracking step. In the pretreatment process, any apparatus may be used as long as it can heat the mixture of biomass and solvent at the set temperature and time to perform solvolysis. For example, an autoclave or a tubular reactor may be used. Can. Further, in the pretreatment step, in order to suppress the vaporization of the liquid during the reaction, it is preferable to pressurize and make the reaction. In addition, in the pretreatment step, the biomass and the solvent can be mixed to form a mixture, and then the mixture can be supplied into the reactor.

The solvent in the pretreatment step promotes the solvolysis reaction of biomass, and contains an oxygen-containing aromatic compound. The oxygen-containing aromatic compounds used for the solvent are substances soluble in cellulose, hemicellulose, lignin and their decomposition products, and specifically, methoxyphenols such as guaiacol (2-methoxyphenol), alkylphenols , Vegetable oil or fat and the like can be used.

In addition, the solvent in the pretreatment step preferably further contains an organic acid. The organic acid used for the solvent is an organic acid which exhibits acidity in an aqueous solution, such as a carboxylic acid, an organic acid having 1 to 6 carbon atoms, etc. Specifically, formic acid, acetic acid, propionic acid or butyric acid may be used. it can. When using woody biomass as biomass, what is by-produced in a pretreatment process is preferred, and especially acetic acid can be used conveniently.

As the solvent contains an oxygen-containing aromatic compound or an organic acid, the solvolysis of the biomass is promoted, so the biomass is decomposed even at a lower temperature than thermal decomposition, subcritical water treatment or supercritical water treatment, and it is liquefied Is possible. In addition, by containing an oxygen-containing aromatic compound in the solvent, the biomass and the decomposition product thereof can be dissolved with high solubility in the solvent, so that the radical is diluted and dispersed in the solvent to suppress repolymerization, The liquefaction reaction (solvolysis) can be promoted. Furthermore, when an organic acid is contained in the solvent, it acts as an acid catalyst on solvolysis, so that the liquefaction reaction of biomass can be further promoted.

Further, as the solvent in the pretreatment step, biocrude obtained by the pretreatment step can be used in addition to or instead of the oxygen-containing aromatic compound or the organic acid. That is, a part of the biocrude obtained by the pretreatment process may be stored and then used as a solvent when the biomass-derived material is subjected to the pretreatment process. In addition, even when biocrude is added to a solvent and the pretreatment step is performed, the obtained biocrude can be added to the solvent and used in the next pretreatment step.

For example, when woody biomass is used as a raw material, the biocrude obtained by the pretreatment step of the present invention contains, as an oxygen-containing aromatic compound, methoxyphenols such as guaiacol, alkylphenols, and organic acids such as acetic acid. It is done. Thereby, even if it does not add an oxygen-containing aromatic compound and an organic acid separately, a biocrude can be added and a liquefaction reaction of biomass can be promoted.

Moreover, FIG. 1 is a figure which shows an example of the process flow of a pre-processing process in the case of collect | recovering a solvent and using for a pre-processing process again. As shown in FIG. 1, the biomass, if necessary, water, an organic acid, or a solvent (an oxygen-containing aromatic compound and an organic acid) are mixed and provided to a reactor to carry out a solvolysis reaction. The reaction product is supplied to a distillation column, and it is fractionated into gas and water, a solvent (oxygen-containing aromatic compound and organic acid), and biocrude, and the solvent is subjected again to the solvolysis reaction. That is, when the biocrude is added to the solvent in the next pretreatment step, the oxygen-containing aromatic compound and the organic acid may be recovered from the reaction product by distillation and used again as the solvent in the pretreatment step. Thereby, a substance that accelerates the solvolysis reaction can be used again as a solvent, and the solvolysis reaction can be advanced more efficiently, and more substances serving as hydrocarbon raw materials can be used in the fluid catalytic decomposition step. Can be supplied. At this time, gas, light oil and water may be recovered and used for other applications. Thereby, resources contained in biomass can be used more effectively. Further, by recovering water, even if the water content is too high to be subjected to the pretreatment step again as a solvent, the water content of the reaction system can be adjusted to an appropriate amount.

In addition, when the biomass contains an appropriate amount of water, the hydrolysis reaction can be advanced by the water contained in the biomass without adding water to the reaction system, so in the pretreatment process of the present invention, at least the biomass and the solvent And solvolysis, and may not add water. That is, in the pretreatment process of the present invention, the solvolysis reaction can be advanced without requiring a large amount of water. Moreover, as water, it is preferable that 5% or more is contained in the reaction system. By containing water of 5% or more in the reaction system, the liquefaction reaction of biomass can be efficiently advanced in the pretreatment step. In addition, when the water content in the reaction system is increased, the dissociation of the acid catalyst proceeds to accelerate the solvolysis reaction, and depending on the raw material, the effect can be enjoyed. In addition, when biocrude is repeatedly used in addition to or in place of the oxygen-containing aromatic compound or organic acid, there is no water accumulated in the reaction system at the start of the operation, the type of biomass, Water may be added to the solvent of the pretreatment step depending on the condition and the like. By containing water, it is possible to advance the hydrolysis of the biomass and to promote the acid dissociation of the organic acid. In addition, for example, in a material containing a sufficient amount of water, or in a humidity control wood chip, water may not be added to the solvent of the pretreatment process. When water is not added to the reaction system, the oxygen-containing aromatic compound itself can be used as a solvent.

The pretreatment step is preferably performed at 160 ° C. or higher. If the temperature is too low, the solvolysis reaction may not proceed and the carbon yield of the liquid product (biocrude) may be low. Moreover, it is preferable to perform a pre-processing process at 290 degrees C or less. If the temperature is too high, the thermal decomposition reaction proceeds to form carbon monoxide (CO) and carbon dioxide (CO ₂ ), and coking also proceeds, which may cause loss of carbon as a gas or solid. From this, by appropriately setting the temperature conditions of the pretreatment process, the solvolysis reaction can be advanced, and the formation of carbon monoxide and carbon dioxide can be suppressed.

The biomass to be subjected to the pretreatment step is preferably pre-crushed. Since the specific surface area of the solid particles is increased by being crushed, the solvolysis reaction proceeds more efficiently even in the same treatment time in the pretreatment step, and the yield of the biocrude obtained by the pretreatment step is improved. be able to. The degree of pulverization may be appropriately set in consideration of the cost of pulverization and the cost of solvolysis.

In the fluid catalytic cracking step, hydrocarbon is produced by performing fluid catalytic cracking using biocrude and a hydrogen donor as raw materials.

The hydrogen donor in the fluid catalytic cracking process of the present invention includes substances capable of donating hydrogen in the fluid catalytic cracking process, and such materials. Organic hydrogen donors have high H / C (the ratio of hydrogen to carbon in the compound), and the decomposition reaction proceeds easily in the fluid catalytic cracking reaction, and an organic that can donate hydrogen due to the progressing hydrogen transfer reaction at the same time It is a compound and, for example, heavy oil represented by vacuum gas oil and atmospheric residual oil can be used. These have a structure in which a linear alkane substituent is developed in a polycyclic aromatic such as alkyl tetralin or alkyl naphthalene (for example, the following compound 1), or a linear alkane structure represented by hexadecane or eicosane (for example, Of the compound 2), and includes such substances, and those substances.

In the fluid catalytic cracking process of the present invention, a zeolite or amorphous silica-alumina having appropriate acid properties can be used as a catalyst, and in the case of zeolite, particularly large pores among zeolites in consideration of the molecular size of the raw material The FAU type zeolite which has is preferably used. In addition, since FAU type zeolite has high hydrogen transfer reaction activity, hydrogen contained in a hydrogen donor is hydroxyl group (-OH), ether bond (-O-), or carboxyl group (Bio-crude). It is delivered to an oxygen-containing component having a structure such as —COOH), and hydrodeoxygenation proceeds to produce water. As a result, the loss of carbon resources in the biomass as carbon monoxide (CO) or carbon dioxide (CO ₂ ) can be suppressed to efficiently convert them into hydrocarbons. Furthermore, it is speculated that a single ring aromatic compound is produced by hydrogenolysis of polycyclic aromatics produced in the biocrude.

Next, with reference to FIG. 2, an apparatus for producing hydrocarbon according to a first embodiment of the present invention will be described.

The hydrocarbon production apparatus 100 is used in a fluid catalytic cracking process, and comprises a raw material storage tank 10 for storing raw materials, and a raw material supply pipe 20 serving as a raw material supply means for supplying raw materials to a riser reaction pipe 30 described later. , Distillation of the hydrocarbon obtained in the riser reaction tube 30, which is a reactor in which fluid catalytic cracking is performed, the regeneration tower 40 for regenerating the catalyst to which coke is attached, and the riser reaction tube 30, and fractionated to each component And a distillation column 50.

Further, a valve 21 for adjusting the supply amount of the raw material is provided between the raw material supply pipe 20 and the riser reaction pipe 30. In the present embodiment, the raw material biocrude and the hydrogen donor are mixed in advance and stored in the raw material storage tank 10 as a raw material slurry.

Fluid catalytic cracking is one of the petroleum refining techniques, and is also referred to as a FCC (Fluid Catalytic Cracking) process. The fluid catalytic cracking reaction is roughly divided into a reaction system (cracking of raw materials and catalyst regeneration) and a separation and purification system of cracked products. In the reaction system, the raw material and the vapor are supplied to the riser reaction tube 30, and the raw material is made into fine powder of zeolite or amorphous silica-alumina having an appropriate acid property at a temperature of about 450 ° C. to 650 ° C. It is decomposed in contact with a finely powdered solid acid catalyst (indicated by white circles (() in FIG. 2).

First, a heavy oil which is a hydrogen donor is decomposed at an acid point which is an active point dispersed in micropores or mesopores of a solid acid catalyst, and an olefin is produced via an intermediate carbenium ion. Furthermore, as a cyclization reaction or a hydrogen transfer reaction proceeds, the oxygen in the compound contained in the biocrude is removed as water and the decomposition proceeds. Since coke is formed on the catalyst in the decomposition reaction of the raw material, the catalyst on which coke has adhered after the reaction (indicated by black circles (●) in FIG. 2, the caulking catalyst) is 600 ° C. to 800 ° C. in the regenerator 40. The catalyst is burned at a high temperature to remove coke and is regenerated and supplied again to the riser reaction tube 30 as a regenerated catalyst (indicated by white circles (() in FIG. 2). At this time, air is sent from the lower part of the regeneration tower 40, and carbon monoxide, carbon dioxide and water are released from the upper part of the regeneration tower 40 along with the combustion of coke. Also, to keep the activity of the catalyst constant, part of the regenerated catalyst is withdrawn and fresh catalyst is replenished. As described above, the reaction system of the fluid catalytic cracking reaction proceeds.

The reactant obtained in the riser reaction tube 30 is sent to the distillation column 50 and fractionated for each component. Light fraction such as propylene, butene or gasoline from the top of distillation column 50, light cycle oil (LCO) from middle, middle fraction such as light oil from middle, heavy cycle oil (HCO) from bottom, or Heavy fractions such as slurry oil (CSO) are obtained.

By such a catalytic cracking reaction, the deoxygenation reaction and the cracking reaction of the biocrude proceed by redistribution of hydrogen in the raw material, and a high energy fuel can be obtained. Moreover, since the fluid catalytic cracking process is not a reaction process in a fixed bed but a reaction process composed of a dilute fluidized bed, even if a small amount of solid remains in the pretreatment process, the reactor is clogged, etc. The operation can be continued without causing any defect.

Next, a hydrocarbon production apparatus according to a second embodiment of the present invention will be described with reference to FIG. In addition, about the same structure as embodiment mentioned above, description is abbreviate | omitted using the same code | symbol.

The hydrocarbon manufacturing apparatus 200 includes a raw material storage tank 210 for storing raw materials, a raw material supply pipe 220 serving as a raw material supply means for supplying raw materials to a riser reaction pipe 30 described later, and a riser reaction pipe 30 for performing fluid catalytic cracking. And a regeneration tower 40 for regenerating the catalyst to which coke has been attached, and a distillation tower 50 for distilling the hydrocarbon obtained in the riser reaction tube 30 and fractionating the components into components.

The raw material storage tank 210 is configured to have a biocrude storage tank 211 and a hydrogen donor storage tank 212. In the hydrocarbon production apparatus 200 of the present embodiment, the biocrude and the hydrogen donor are combined. Are stored in separate storage tanks. Also, the raw material supply pipe 220 includes a biocrude supply pipe 222 connected to the biocrude storage tank 211, a hydrogen donor supply pipe 223 connected to the hydrogen donor storage tank 212, a biocrude supply pipe 222, and hydrogen donating. And a mixed supply pipe 224 joined to the body supply pipe 223 and connected to the riser reaction pipe 30. That is, in the hydrocarbon production apparatus 200 of the present embodiment, the biocrude and the hydrogen donor are separately stored, mixed in the feed pipe, and supplied to the riser reaction pipe 30. In addition, a valve 221 is provided between the mixing supply pipe 224 and the riser reaction pipe 30 to adjust the supply amount of the raw material. In the present embodiment, the biocrude storage tank 211 is provided upstream of the hydrogen donor storage tank 212, but the hydrogen donor storage tank 212 may be provided upstream.

Next, a hydrocarbon production apparatus according to a third embodiment of the present invention will be described with reference to FIG. In addition, about the same structure as embodiment mentioned above, description is abbreviate | omitted using the same code | symbol.

The hydrocarbon manufacturing apparatus 300 is a reactor in which fluid catalytic cracking is performed, and a raw material storage tank 310 for storing raw materials, a raw material supply pipe 320 which is a raw material supply means for supplying raw materials to a riser reaction pipe 30 described later. A riser reaction pipe 30, a regeneration tower 40 for regenerating a catalyst to which coke is attached, and a distillation tower 50 for distilling hydrocarbons obtained in the riser reaction pipe 30 to fractionate each component.

The raw material storage tank 310 is configured to include a biocrude storage tank 311 and a hydrogen donor storage tank 312. In the hydrocarbon production apparatus 300 of the present embodiment, the biocrude and the hydrogen donor are combined. Are stored in separate storage tanks. The raw material supply pipe 320 is a biocrude supply pipe 322 (biocrude supply part) connected to the biocrude storage tank 311, and a hydrogen donor supply pipe 323 (hydrogen donor connected to the hydrogen donor storage tank 312). A supply unit). That is, in the hydrocarbon production apparatus 300 of the present embodiment, the biocrude and the hydrogen donor are separately stored, and are supplied to the riser reaction pipe 30 by the separate supply pipes. In addition, a valve 321 a for adjusting the supply amount of biocrude is provided between the biocrude supply pipe 322 and the riser reaction pipe 30, and hydrogen is provided between the hydrogen donor supply pipe 323 and the riser reaction pipe 30. A valve 321 b is provided to adjust the amount of donor supply.

As in the hydrocarbon production apparatus of the present embodiment, in the fluid catalytic cracking step of the present invention, biocrude and hydrogen donor may be separately supplied. In addition, the production apparatus used in the fluid catalytic cracking step of the present invention separately has a biocrude supply unit for supplying biocrude and a hydrogen donor supply unit for supplying a hydrogen donor as raw material supply means. It may be

When using a biocrude and a hydrogen donor such as heavy oil as a material in a fluid catalytic cracking step, if the biocrude and the hydrogen donor hardly dissolve each other, the biomass is stabilized in the hydrogen donor slurry. In order to disperse it, it can be configured as the hydrocarbon production apparatus 100 of the first embodiment or the hydrocarbon production apparatus 200 of the second embodiment. That is, as in the hydrocarbon production apparatus 100 shown in FIG. 2, the raw material slurry obtained by mixing the biocrude and the hydrogen donor is supplied to the lower part of the riser reaction tube 30 where the fluid catalytic cracking reaction is performed. Alternatively, as in the hydrocarbon production apparatus 200 shown in FIG. 3, the biocrude and the hydrogen donor are stored in separate tanks and mixed in the raw material supply pipe 220 (mixing supply pipe 224). The raw material can be configured to be supplied to the riser reaction tube 30.

On the other hand, when a portion of the biocrude and the hydrogen donor are mutually dissolved, the solvent in the biocrude in which the biomass is dispersed may be back-extracted to the hydrogen donor to precipitate the biomass. The supply nozzle may be clogged. In such a case, as in the hydrocarbon production apparatus 300 shown in FIG. 4, the biocrude and the hydrogen donor are stored in separate tanks, and separate supply pipes up to the riser reaction pipe 30 (biocrude (biocrude) It is preferable to be configured to be supplied through the supply pipe 322 and the hydrogen donor supply pipe 323). By separately supplying the biocrude and the hydrogen donor, the biomass can be prevented from being precipitated since the biocrude and the hydrogen donor are not mixed in the supply pipe. Thereby, the clogging of the raw material supply pipe and the supply nozzle can be prevented. In the riser reaction tube 30, the catalyst, which is solid particles, flows at a high flow rate, and clogging does not occur.

As described above, how to configure a hydrocarbon production apparatus can be selected according to the properties of the raw material crude crude and the hydrogen donor.

According to the method for producing hydrocarbon and the method for producing biocrude according to the present invention as described above, the biomass is pretreated by solvolysis at a lower temperature than thermal decomposition, subcritical water treatment or supercritical water treatment. As the decomposition reaction proceeds, when it is catalytically decomposed with a hydrogen donor in the subsequent fluid catalytic cracking step, deoxygenation is carried out by hydrodeoxygenation reaction, and a large amount of oxygen is removed as water, so that monooxidation The formation of carbon and carbon dioxide is suppressed, and the loss of carbon resources can be reduced. Thereby, hydrocarbons can be efficiently produced from biomass. Moreover, it is speculated that a monocyclic aromatic compound is produced by hydrogenolysis of a polycyclic aromatic compound that constitutes biomass.

In addition, when the biocrude and the hydrogen donor are mixed, part of the biomass may be precipitated as a solid. According to the hydrocarbon production apparatus of the present invention, since the biocrude and the hydrogen donor are separately supplied, the deposition of the biomass is prevented without the biocrude and the hydrogen donor being mixed in the feed pipe. be able to.

[Hydrocarbon production system]
Next, the hydrocarbon production system of the present invention will be described.

The hydrocarbon production system of the present invention uses the above-mentioned hydrocarbon production method, and may be carried out in a place where the pretreatment step and the fluid catalytic cracking step are in proximity, or each other The biocrude obtained by the pretreatment step may be transported at a remote place and supplied to the fluid catalytic cracking step. Whether the pretreatment step and the fluid catalytic cracking step are performed in close proximity to each other or in locations separated from each other can be appropriately selected depending on the biomass production site, the location conditions of equipment, and the like.

For example, when the production area of biomass is in a forest area and the equipment used for the fluid catalytic cracking process is in a bay area, the equipment used for the pretreatment process is provided in the forest area, and the pretreatment process and the fluid catalytic cracking process Can be done at a distance from each other. At this time, the biocrude obtained in the pretreatment process can be transported by a tank lorry, a truck or the like. In addition, for transportation from the middle to the bottom of a mountain where forest roads can not be used so that tanker trucks, trucks, etc. can not pass, the biocrude may be transported by a transport pipe. The transport of the biocrude may be performed not only by the vehicle transport but also by other transport means in consideration of the transport cost.

In the present invention, “a place separated from each other” refers to a batch such as a tank lorry or a truck instead of transporting the reactant by directly connecting the facility used in the pretreatment process and the facility used in the fluid catalytic cracking process with piping or the like. It indicates that they are separated to the extent of being transported via transport. If the equipment used for the pretreatment process is provided in a place where tank lorries, trucks, etc. can not pass, as described above, transport the reactant through transport pipes etc. to the passable place, The reactants may then be transported by batch transport to the site where equipment is used for the fluid catalytic cracking process.

If the pretreatment step and the fluid catalytic cracking step are performed at locations separated from each other, transporting the biocrude to a facility that performs the fluid catalytic cracking step is more than transporting the bulkier biomass than the biocrude. Transportation costs can be reduced.

The pretreatment step may be performed at the biomass production site. For example, when the biomass is a woody biomass, the operation of the pretreatment process may be performed at a site near mountain where a raw wood as a material of the woody biomass is present.

When the operation of the fluid catalytic cracking process is performed using the equipment of a refinery, the production site of woody biomass and the refinery are often separated from each other. Since woody biomass is bulkier than biocrude, transportation of woody biomass from a production area to a hydrocarbon production facility (a facility equipped with equipment used in the pretreatment process and fluid catalytic cracking process) increases transportation costs. By performing the pretreatment step at the biomass production site, woody biomass that is bulkier than biocrude becomes liquid biocrude, and can be transported by a tank lorry or the like. From this, the transportation cost can be lower than that for transporting woody biomass that is bulkier than biocrude as it is.

Besides, the best configuration, method and the like for carrying out the present invention are disclosed in the above description, but the present invention is not limited to this. That is, although the present invention has been described with particular reference to a particular embodiment, it is to be understood that shapes, materials, quantities, etc. may be added to the embodiments described above without departing from the scope of the technical idea and purpose of the present invention. Various modifications can be made by one skilled in the art in other detailed configurations.

Therefore, the descriptions of the above-described disclosure of the shapes, materials and the like are merely illustrative for ease of understanding of the present invention, and are not intended to limit the present invention. The description in the name of a member from which some or all of the limitations of the material and the like have been removed is included in the present invention.

Hereinafter, the present invention will be more specifically described by way of examples. However, the present invention is not limited by the following examples. In addition, a ratio shows a mass ratio unless there is particular notice.

[Examination of model materials]
In the present example, woody biomass was used as a raw material. At first, simulated cedar was examined as a model material of cedar. The “simulated cedar” in the present example is a composition in which cellulose and lignin are mixed in a ratio of 6: 4 to simulate the composition of cedar. Here, the composition of lignin is about 30% in general cedar (Harokuchi, et al. (1993) “Chemistry of wood” by Bunneijido), but it is easy to understand the decomposition of lignin in fluid catalytic decomposition. The composition was increased to 40%. Moreover, since it is assumed that cellulose and hemicellulose do not differ greatly in decomposition characteristics structurally (cellulose + hemicellulose), the composition was replaced with cellulose to make 60%.

First, in order to compare the thermal behavior of cedar and simulated cedar, thermogravimetric analysis was performed. Sugi chip and simulated Japanese cedar were used as materials. For measurement, the temperature was raised from room temperature to 800 ° C. at 10 K / min under a nitrogen atmosphere (50 ml / min) using a thermogravimetric analyzer (manufactured by Shimadzu Corporation, TGA-51). The results of thermogravimetric analysis are shown in FIG. The ordinate represents the residual ratio (%, a value obtained by calculating the weight ratio of the residue to the weight of the sample subjected to thermogravimetric analysis), and the abscissa represents the temperature. The broken line in the figure indicates the cedar chip, and the solid line indicates the analysis result of simulated cedar. As a result, while it has been known that cellulose and lignin constituting cedar and simulated cedar show thermal decomposition behavior which is largely different from that of cypress, cedar and simulated cedar show similar thermal decomposition behavior. The In addition, it has been confirmed that the constituents of cedar have a complex higher order structure due to hydrogen bonds and the like, but the presence or absence of such a bond between constituents does not substantially affect the thermal decomposition behavior. From the above, it is considered that the decomposition behavior of simulated cedar is similar to that of general woody biomass. In addition, from the results of FIG. 5, it was found that when the temperature of the cedar and the simulated cedar exceeds 290 ° C., the thermal decomposition reaction proceeds.

[Pretreatment step (hydrocrude production) in hydrocarbon production method]
(Examples 1 and 2)
Next, cedar and simulated cedar were subjected to the pretreatment process, respectively, and the liquid, gas and solid after the process were recovered to compare the carbon yield. The cedar and the simulated cedar were subjected to the pretreatment step, and the liquid, gas and solid after the pretreatment step were recovered to calculate the carbon yield.

The following materials were used. In addition, the mass ratio shown below shall show preparation density | concentration.
Sugi chip (Example 1) or simulated Japanese cedar (Example 2) 10%
Guiaiacol 84%
Water 5%
Acetic acid 1%

The cedar chips used in Example 1 were ground beforehand using cedar chips having an average particle diameter of 100 μm or more using a planetary ball mill (Fritchu Japan, model number P-7), and then sieved to 75 μm and 106 μm. It is a Sugi chip which entered between the sieves. That is, a cedar chip having an average particle diameter of about 80 μm was used as a raw material. The same sieving was performed on the simulated Japanese cedar used in Example 2, and the simulated Japanese cedar inserted between 75 μm and 106 μm sieves was used as the valve amount.

The above materials were mixed and subjected to an autoclave (MM Labotech, MMJ-500, internal volume 430 ml). The reaction conditions were 200 ° C., 1 hour, and then natural cooling. The generated gas product (gas) was collected by a gas bag and analyzed using gas chromatography (manufactured by Shimadzu Corporation, GC-8A). The detection was performed by a thermal conductivity detector.

Also, liquid products and solid products are described in no. Separation by vacuum filtration using 5 C filter paper. After filtration, the liquid product remaining in the solid product or in the reaction vessel was washed with acetone and extracted. The acetone extract was evaporated at a temperature of 60 ° C. to evaporate acetone, and the residue also became a liquid product. Further, the solid product after acetone washing was subjected to vacuum drying at room temperature overnight using a desiccator and an aspirator (manufactured by Tokyo Rika Kikai, model number A-3S), and then the mass was measured. The carbon fraction in the dried solid product was measured using an NC analyzer (manufactured by Sumika Analysis Center, SUMIGRAPH NC-1000).

The carbon mass in Japanese cedar or simulated Japanese cedar was measured by an NC analyzer (manufactured by Sumika Analysis Center, model number SUMIGRAPH NC-1000). In addition, it was assumed that carbon contained in the produced gas and carbon in the solid were all derived from cedar or simulated cedar. Therefore, the carbon mass in the gaseous product with respect to the carbon mass in the raw material cedar or simulated cedar as the gaseous carbon yield, and the carbon mass in the solid product with respect to the carbon mass in the raw cedar or simulated cedar as the solid carbon yield Calculated. Furthermore, the liquid carbon yield was calculated by subtracting the gaseous carbon yield and the solid carbon yield from 100%. That is, the gaseous carbon yield, liquid carbon yield, and solid carbon yield shown below are based on carbon in the raw material cedar or simulated cedar, and the conversion from solvents (guaiacol, water, acetic acid) is low. In this example, the conversion from the solvent is not considered because it is considered that the carbon yield is not greatly affected.

(Example 3)
The following were used as materials.
Sugi chip 10%
Guaiacol 85%
Water 5%
The same operation as in Example 1 was performed except that acetic acid was changed to 0% (no addition).

(Examples 4 to 6)
The following were used as materials.
Simulated cedar 10%
Guaial 75-85%
Water 5%
Acetic acid 0-10%
Acetic acid is respectively 0% (Example 4, no addition), 5% (Example 5), 10% (Example 6), and guaiacol is 85% (Example 4), 80% (Example 5), respectively. The same operation as in Example 2 was performed except that 75% (Example 6) was used.

(Examples 7 to 9)
The following were used as materials.
Simulated cedar 10%
Guaiacol 85%
Water 5%
In addition, the same operation as in Example 2 was performed except that the reaction temperature was 150 ° C. (Example 7), 250 ° C. (Example 8), and 300 ° C. (Example 9) as the reaction conditions.

(Examples 10 to 12)
The following were used as materials.
Simulated cedar 10%
Guaia call 74 to 89%
Water 0 to 15%
Acetic acid 1%
Using simulated Japanese cedar as the material, the moisture content is made 0% (Example 10, no addition), 10% (Example 11), 15% (Example 12), 89% (Example 10), 79% of guaiacol (Example 11) The same operation as in Example 2 was performed except that 74% (Example 12) was used.

(Example 13)
Using the liquid product (biocrude) obtained in Example 2 as a solvent, a second pretreatment step was performed under the same conditions as in Example 2 with the following composition.
Simulated cedar 10%
Liquid product obtained in the pretreatment reaction of Example 2 84%
Water 5%
Acetic acid 1%

The liquid product obtained in the above second pre-treatment step is used as a solvent, and the above composition (10% simulated cedar, 84% liquid product obtained in the second pre-treatment step, 5% water, acetic acid 1 The third pretreatment step was performed under the same conditions as in Example 2 in%). Furthermore, the liquid product obtained in the third pretreatment step is used as a solvent, and the above composition (10% simulated cedar, 84% liquid product obtained in the third pretreatment step, 5% water, acetic acid 1 The fourth pretreatment step was performed under the same conditions as in Example 2 in%). The liquid, gas and solid after the fourth pretreatment step were recovered by the same method as in Example 2 to calculate the carbon yield.

(Example 14)
The same operation as in Example 1 was carried out except that the cedar chips of the material were not crushed by a planetary ball mill.

(Comparative example 1)
The conditions were the same as in Example 1 except that 10% of cedar chip was used as the material, guaiacol was 0% (no addition), acetic acid was 1%, and water was 89%. As a result, a large amount of solid remained, and almost no liquid product was obtained. From this, it is difficult to obtain sufficient biocrude under the condition that no solvent containing oxygenated aromatic compound is added, and the obtained product contains a large amount of solid matter, and therefore fluid contact It has been shown to be difficult to provide for the degradation step.

(Result and Consideration of Examples 1 to 14)
The treatment conditions of Examples 1 to 14 are shown in Table 1, and the carbon yield (C%) of the solvolysis products (liquid product, gaseous product, solid product) of Examples 1 to 14 is shown in Table 2 Show.

As shown in Table 2, carbon resources are recovered in a liquid product (Biocrude) in Examples 1 to 14 in which Japanese cedar and simulated Japanese cedar are subjected to solvolysis, and a pretreatment step is carried out. It has been shown that carbon resources can be efficiently recovered to biocrude.

As shown in Table 2, in Example 1 using Sugi and Example 2 using simulated Sugi, the carbon yields of the liquid product, the gas product, and the solid product were almost the same. . From the results of thermogravimetric analysis and the results of Examples 1 and 2, it was shown that simulated cedar is useful as a model substance of cedar.

Further, as shown in Table 2, in Examples 1 and 2 in which acetic acid was added, the carbon yield of the liquid product was higher than in Examples 3 and 4 in which acetic acid was not added. From this, it was shown that the addition of acetic acid in the pretreatment step accelerates the decomposition reaction and carbon can be efficiently recovered by the liquid product (biocrude). The amount of acetic acid added was as high as 1% (Example 2) even at 5% (Example 5), and showed a high carbon yield. In addition, when the addition amount of acetic acid is 10% (Example 6), the carbon yield of the liquid product is higher than that in the case where no acetic acid is added, but in comparison with the cases of 1% and 5%. The carbon yield of the liquid product decreased.

Also, comparing Examples 2 and 7 to 9, the reaction temperature of 200 ° C. (Example 2) has a higher carbon yield of the liquid product and the higher temperature than the reaction temperature of 150 ° C. (Example 7). When (at 250 ° C. (Example 8) or 300 ° C. (Example 9)), the carbon yield of the liquid product decreased. At the reaction temperature of 200 ° C., the carbon yield of the liquid product was the highest. Comparing the carbon yields of non-liquid products, the carbon yield of solid products is the highest at a reaction temperature of 150 ° C, and the carbon yield of gaseous products is that of reaction temperatures of 250 ° C and 300 ° C. It got higher. This is considered to be because the higher the temperature, the easier the solvolysis reaction proceeds, and the more the temperature is, the more the thermal decomposition reaction proceeds, as shown in the result of the thermogravimetric analysis described above. In addition, the carbon contents of the solid products obtained in the simulated sugi, Examples 2, 8 and 9 before the reaction were calculated to be 46.6%, 45.7%, 69.0% and The solid product obtained in Example 2 has the same carbon content as that of simulated cedar, and the solid product obtained in Examples 8 and 9 has a carbon content higher than that of simulated cedar. Was high. It was shown that part of the raw material is carbonized under the condition of higher reaction temperature.

In addition, comparing Examples 2 and 10 to 12, the carbon yield of the liquid product is higher when the added amount of water is 5% (Example 2) than when no water is added (Example 10), and the added amount of water is 10% Also in (Example 11) and 15% (Example 12), the carbon yield of the liquid product was almost the same and showed a high value. That is, it was confirmed that the carbon yield in the liquid product is higher when water is added to the reaction system. This is considered to be because the addition of water to the reaction system facilitates the progress of the hydrolysis reaction. Further, it was also confirmed from Examples 2 and 10 to 12 that a small amount of water of about 15% or less is sufficient for the reaction system. Generally, considering the amount of water contained in biomass, when using about 10% of the reaction system as the material of the pretreatment process, the water contained in the reaction system will be about 5% or more. Was considered to proceed even if water was not further added to the reaction system.

The carbon yield in the liquid product (Biocrude) became a high value of 91.5% in Example 2 where the liquid product (biocrude) was repeatedly subjected to the pretreatment step of Example 2 and the liquid product being reused as a solvent. . From this, it was shown that carbon can be efficiently recovered to the solvolysis liquid product of biomass even if the liquid product is added as a solvent.

Further, from the results of Example 1 and Example 14, it was confirmed that most of carbon was recovered as a liquid product under both conditions. Furthermore, since the carbon yield of the liquid product was higher in Example 1 in which the sugi chip was crushed than in Example 14 in which the sugi chip was not crushed, the biomass was finely ground to form a liquid even at the same treatment time. It has been shown that carbon can be efficiently recovered by waste.

<Composition Analysis of Biocrude>
(Example 15)
Next, composition analysis of the biocrude obtained by the pretreatment process was performed. The following materials were used. In addition, the mass ratio shown below shall show preparation density | concentration.
Simulated cedar 30%
Guaia call 64%
Water 5%
Acetic acid 1%
The above materials were mixed and reacted under the same conditions as in Example 1 to obtain a liquid product. The obtained liquid product was subjected to GPC measurement. Tetrahydrofuran was used as the solvent, and the column was TSKgel G2500Hxl (manufactured by Tosoh Corporation). The results of the GPC measurement are shown in FIG. In FIG. 6, the result of Example 15 is indicated by a solid line. The liquid product was also subjected to GC-MS analysis to confirm the compounds contained in the liquid product. GC-MS analysis was performed with Rxi-1 ms (Restec), a vaporization chamber temperature of 300 ° C., an interface temperature of 330 ° C., and a column temperature of 35-330 ° C.

(Example 16)
The same operation as in Example 15 was performed except that acetic acid was 0% (no addition) and guaiacol was 65%. The results of the GPC measurement are shown in FIG. In FIG. 6, the result of Example 16 is indicated by a broken line.

(Results and discussion)
As shown in FIG. 6, a peak attributed to guaiacol and a compound modified with guaiacol and a broad peak having a molecular weight of about 200 to 10,000 were observed around a molecular weight of 150. The peak in the vicinity of the molecular weight 150 was the same peak in Example 15 and Example 16. It is considered that the peak with a molecular weight of about 200 to 10000 becomes larger under the condition (Example 15) in which acetic acid is added than the condition (Example 16) in which acetic acid is not added (Example 15), and this peak is derived from the decomposition product of simulated cedar. It was done. Further, as a result of gas chromatography analysis, the liquid products of Examples 15 and 16 mainly contain guaiacol as a single ring oxygen-containing aromatic compound, and in addition, catechol, cresol, dimethylphenol, methoxyphenol And benzenediol, etc., and the content of the single ring oxygen-containing aromatic compound was 63% by mass.

From the results of the above Examples 1 to 16, it was shown that biomass can be decomposed in the pretreatment step of the present invention to efficiently recover a carbon product as a liquid product, ie, a biocrude.

[Fluid catalytic cracking process of biocrude in hydrocarbon production method]
(Example 17)
The biocrude obtained in Example 1 was subjected to a fluid catalytic cracking step. Industrial RFCC equilibrium catalyst (UCS value (unit lattice constant) 24.27 Å (2.427 nm) containing FAU type zeolite as a catalyst, using a fixed bed flow reactor according to ASTM D3907-92 as the reactor The ratio of the catalyst to the total mass of the biocrude and the hydrogen donor was Cat / Oil = 3, WHSV = 16 ^-1 , and the reaction temperature of the fluid catalytic cracking reaction was 500 ° C. The experimental method was as follows. It was carried out according to the method defined in ASTM D 5154-10 In Example 17, eicosane was used as a hydrogen donor.

The resulting product was analyzed as follows. The reaction products passed through the catalyst bath were cooled in an ice bath and separated after gas-liquid separation. Gas recovery was carried out by water replacement. Hydrogen, carbon monoxide and carbon dioxide contained in the gaseous product are analyzed by gas chromatography with thermal conductivity detector (GC-8A, manufactured by Shimadzu Corporation), and hydrocarbon is with hydrogen flame ionization detector. Gas chromatography (manufactured by Shimadzu Corporation, GC-2014) was analyzed. Hydrocarbons and oxygenated compounds in the liquid product can be detected using a gas chromatography with hydrogen flame ionization detector (GC-2014, manufactured by Shimadzu Corporation) and a gas chromatograph mass spectrometer (GCMS-QP2010 Plus, manufactured by Shimadzu Corporation) analyzed. The amount of coke produced was determined from the weight change of the catalyst tank before and after the reaction, and the components were analyzed using an NC analyzer (Sumigraph NC-1000, manufactured by Sumika Chemical Analysis Center). The components that could not be detected by gas chromatography were taken as others. In addition, although it was confirmed visually that water is contained in a liquid product, since it was difficult to quantify by gas chromatography, it was decided to include water in others. Furthermore, it is considered that other non-degraded high molecular weight oxygen-containing components are also contained.

(Examples 18 to 20)
The same operation as in Example 17 was performed except that a catalyst having a different UCS value from the industrial RFCC equilibrium catalyst of Example 17 was used. The catalyst had a UCS value of 24.30 Å (2.430 nm, Example 18), 24.35 Å (2.435 nm, Example 19), 24.40 Å (2.440 nm, Example 20).

(Comparative example 2)
The same procedure as in Example 17 was performed, except that no hydrogen donor was added, that is, only biocrude was subjected to fluid catalytic cracking. As a result, the tube was clogged, and a large amount of coke was formed to precipitate carbon, and a small amount of hydrocarbon was formed. In addition, since only a biocrude does not form carbenium ions and there is no hydrogen donor, hydrodeoxygenation reaction and hydrogenolysis do not proceed by hydrogen transfer reaction, and therefore, almost no hydrocarbons are formed. it is conceivable that.

(Results and discussion)
The composition of the reaction product in the fluid catalytic cracking step of Examples 17 to 20 is as shown in Table 3.

As shown in Table 3, the reaction products (Examples 17 to 20) in the fluid catalytic cracking step contain gaseous hydrocarbons, and paraffins, olefins, aromatic hydrocarbons as liquid hydrocarbons, and contain oxygen As a compound, methylphenols were included. Therefore, it has been confirmed that hydrocarbons can be produced by subjecting a cedar-derived biocrude and a hydrogen donor, eicosane, to fluid catalytic cracking. In addition, the higher the UCS value, that is, the higher the catalytic activity, the higher the amount of hydrocarbons produced. However, in Example 20, which has the highest catalytic activity, not only the hydrocarbons but also the amount of coke are high. It was confirmed that

Moreover, oxygen contained in the biocrude subjected to the fluid catalytic cracking step is contained in the reaction product as an oxygen-containing compound, carbon monoxide (CO), carbon dioxide (CO ₂ ), or water. When the products of Examples 17 to 20 are compared, it can be said that as the catalytic activity increases, the amounts of oxygenated compounds, carbon monoxide, and carbon dioxide are decreased, and thus the amount of water produced is increased. Conceivable. That is, it is considered that the hydrodeoxygenation reaction proceeds in which hydrogen is transferred from the hydrogen donor, eicosane, to the oxygen-containing compound contained in the biocrude to form water. Therefore, it is presumed that the production of hydrocarbons by subjecting the biocrude and the hydrogen donor to the fluid catalytic cracking step is due to the hydrodeoxygenation reaction of the oxygen-containing compound contained in the biocrude.

From the above evaluation results, in Examples 1 to 20, which is an exemplary embodiment of the present invention, most of carbon resources are recovered from biomass into biocrude, and loss of carbon resources is reduced, and fluid catalytic cracking is performed. It has been shown that hydrocarbons can be produced.

DESCRIPTION OF SYMBOLS 100 Hydrocarbon production apparatus 10 Raw material storage tank 20 Raw material supply pipe 21 Valve 30 Riser reaction pipe 40 Regenerative tower 50 Distillation column 200 Hydrocarbon production apparatus 210 Raw material storage tank 211 Biocrude storage tank 212 Hydrogen donor storage tank 220 Raw material supply Pipe 221 valve 222 biocrude supply pipe 223 hydrogen donor supply pipe 224 mixing supply pipe 300 hydrocarbon manufacturing apparatus 310 raw material storage tank 311 biocrude storage tank 312 hydrogen donor storage tank 320 raw material supply pipe 321a, 321b valve 322 biocrude Supply tube 323 hydrogen donor supply tube

Claims (8)

A pretreatment step of obtaining biocrude by solvolysis by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound;
A method for producing hydrocarbon, comprising: a fluid catalytic cracking step of performing fluid catalytic cracking using the biocrude obtained in the pre-treatment step and a hydrogen donor as raw materials. The method for producing hydrocarbon according to claim 1, wherein the solvent in the pretreatment step contains an organic acid. The biomass is woody biomass,
The method for producing a hydrocarbon according to claim 1 or 2, wherein the solvent in the pretreatment step contains the biocrude. The method for producing a hydrocarbon according to any one of claims 1 to 3, wherein the biocrude and the hydrogen donor are separately supplied in the fluid catalytic cracking step. A process for producing a biocrude comprising obtaining a biocrude by mixing at least biomass and a solvent containing an oxygen-containing aromatic compound and subjecting the mixture to solvolysis. An apparatus for producing hydrocarbons used in the fluid catalytic cracking step of the process for producing hydrocarbons according to any one of claims 1 to 4, wherein
A reactor in which the fluid catalytic cracking is performed;
A raw material supply means for supplying the raw material to the reactor;
The apparatus for producing hydrocarbon, wherein the raw material supply means separately comprises a biocrude supply unit for supplying the biocrude and a hydrogen donor supply unit for supplying the hydrogen donor. A hydrocarbon production system using the hydrocarbon production method according to any one of claims 1 to 4,
The pre-treatment step and the fluid catalytic cracking step being performed at locations remote from one another,
A hydrocarbon production system, which transports the biocrude obtained by the pre-treatment process and supplies it to the fluid catalytic cracking process. The biomass is woody biomass,
8. The hydrocarbon production system according to claim 7, wherein the pretreatment step is performed at the base of a raw wood that is a material of the woody biomass.

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