Method for producing biofuel, apparatus for producing biofuel, and bio-oil

Abstract

Provided is a method for producing a biofuel, which is economical and exhibits both carbon reduction and resource recycling effects. According to an aspect, a method for producing a biofuel is provided comprising the steps of: (S1) preparing a raw material including at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks; and (S2) pyrolyzing the raw material through pyrolysis to obtain sub-gas, bio-char, and bio-oil.

Description

Method for producing biofuel, biofuel production device and biooil

[0001] The present invention relates to a method for producing biofuel, and more specifically, to a method for producing biofuel, a biofuel production device, and bio-oil.

[0002] Recently, with the renewed recognition of the superiority of biomass fuel as a renewable energy source, research on biomass energy conversion technologies is actively being conducted around the world, and technological development is currently progressing at a rapid pace. Among these biomass energy conversion technologies, one that has recently attracted attention is bio-oil production technology. Bio-oil is oil produced from woody and herbaceous biomass and can be used as a raw material for chemical products, similar to crude oil, which is a raw material for petroleum fuels and petrochemicals. Moreover, compared to solid feedstocks, it has a higher energy density, resulting in lower transportation and storage costs. Furthermore, its liquid form makes it easy to handle, making it highly valuable as a fuel for heating and power generation.

[0003] Meanwhile, cashews, a raw material for biofuel production, are a popular nut used in various dishes, snacks, and as an accompaniment to alcohol in both the East and the West. Cashews grow on cashew trees, and the nut is encased in a shell at the base of the cashew apple.

[0004] After producing cashew nuts from cashew trees, shells are produced as a byproduct, and cashew shells contain about 30 to 35% of cashew oil (cashew nut shell liquid).

[0005] Cashew oil can be extracted from cashew nut shells using mechanical extraction (pressing), heat treatment (roasting), distillation, supercritical fluid extraction, and solvent extraction. The composition of the main components and yield of the oil vary depending on the extraction method. Currently, the commercially available cashew oil extraction method in Vietnam and other regions uses mechanical pressing. Anacardic acid, a phenolic lipid, accounts for 60-70% of the oil produced. Anacardic acid is an organic compound with alkyl and carboxyl groups chemically bonded to a phenol group. It can cause dermatitis and rashes upon contact with the skin, causing significant inconvenience to local cashew nut farmers. While this mechanical pressing method is quick and easy to extract, the cashew shells still contain excessive amounts of cashew oil and a large amount of impurities, including ash. Using cashew oil, which contains a high level of ash, as fuel can cause various problems, including corrosion, fouling, and slagging in engines and power plants. It can also reduce the reactivity of high-value-added products, such as curing agents, surfactants, and resins.

[0006] Furthermore, anacadic acid, the main component of pressed cashew oil, is responsible for increasing the total acid value and viscosity. The total acid value is measured by measuring the content of free fatty acids in the oil, and the higher the content of anacadic acid, which is the free fatty acid form of cardanol, the higher the measured total acid value. Viscosity is somewhat related to the freezing point of a liquid. Anacadic acid has a melting point of 34℃ and cardanol has a melting point of -20℃, so anacadic acid has a high viscosity at room temperature. Since anacadic acid causes dermatitis and rashes when in contact with the skin, a separate process is required to convert it to cardanol, and there is the problem of simultaneously removing impurities. Therefore, in order to utilize cashew oil produced by the mechanical extraction method as fuel or a high value-added material, there is the problem of converting the main component anacadic acid to cardanol and simultaneously removing impurities.

[0007] The purpose of the present invention is to provide a method for producing biofuel that is economical and has both carbon reduction and resource recycling effects.

[0008] Another object of the present invention is to provide a method for producing a biofuel having a high calorific value through a simple process.

[0009] Another object of the present invention is to provide a method for producing biofuel, which can reduce process efficiency and manufacturing costs by reusing gas generated during the method for producing biofuel as a heat source for thermal decomposition of raw materials.

[0010] Another object of the present invention is to provide a biofuel production device capable of implementing the above-described biofuel production method.

[0011] The purposes of the present invention are not limited to those mentioned above, and other unmentioned purposes and advantages of the present invention can be understood through the following description and will be more clearly understood through the embodiments of the present invention. Furthermore, it will be readily apparent that the purposes and advantages of the present invention can be realized by the means and combinations thereof set forth in the claims.

[0012] According to a first aspect of the present invention for achieving the above object, a method for producing biofuel is provided, comprising the steps of (S1) preparing a raw material including at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks; and (S2) pyrolyzing the raw material using a pyrolysis method to obtain sub-gas, biochar, and bio-oil.

[0013] According to a second aspect of the present invention, the vegetable oil of the vegetable oil residue in the first aspect may include at least one of palm oil, soybean oil, coconut oil, rapeseed oil, olive oil, corn oil, and peanut oil.

[0014] According to a third aspect of the present invention, in the first or second aspect, the husk may include at least one of coffee husk, palm oil husk (Palm kernel shell, PKS), and grain husk.

[0015] According to a fourth aspect of the present invention, in any one of the first to third aspects, the pyrolysis method may include at least one of rotary kiln pyrolysis, fluidized bed pyrolysis, batch pyrolysis, and screw pyrolysis.

[0016] According to a fifth aspect of the present invention, in any one of the first to fourth aspects, the sub-gas can be reused as a heat source for the pyrolysis method. Specifically, the sub-gas is transferred to a combustion device via a heat exchanger, heated in the combustion device, and then transferred to the pyrolysis reactor, where it can be reused as a heat source for pyrolyzing raw materials.

[0017] According to a sixth aspect of the present invention, in any one of the first to fifth aspects, the bio-oil may include a phenol derivative.

[0018] According to the seventh aspect of the present invention, in the sixth aspect, the phenol derivative may include at least one of the compounds represented by the following chemical formulas 1 to 3.

[0019] [Chemical Formula 1]

[0020]

[0021] [Chemical Formula 2]

[0022]

[0023] [Chemical Formula 3]

[0024]

[0025] In the above chemical formulas 1 to 3, R1 to R3 are each independently a carbon chain functional group having 15 carbon atoms and including at least one of an unsaturated bond and a saturated bond.

[0026] According to an eighth aspect of the present invention, a method for producing a biofuel may be provided, further comprising at least one of the steps of (S3a) forming the biochar into pellets to produce a first biofuel; and (S3b) trans-esterifying the bio-oil to produce a second biofuel.

[0027] According to a ninth aspect of the present invention, a biofuel production device is provided, comprising: a raw material injection unit into which raw materials are injected; a pyrolysis reactor connected to the raw material injection unit; a cooler connected to the pyrolysis reactor; a heat exchanger connected to the pyrolysis reactor; a first recovery unit connected to the cooler and for recovering biochar; and a second recovery unit connected to the heat exchanger and for recovering bio-oil; wherein the raw material includes at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks.

[0028] According to a tenth aspect of the present invention, in the ninth aspect, the pyrolysis reactor may include at least one of a rotary kiln reactor, a fluidized bed reactor, a batch pyrolysis reactor, and a screw pyrolysis reactor.

[0029] According to an eleventh aspect of the present invention, in the ninth or tenth aspect, the biofuel production device may further include a combustion device connected to the heat exchanger and the pyrolysis reactor.

[0030] According to a twelfth aspect of the present invention, a bio-oil is provided, which is derived from cashew oil (Cashew nut shell liquid; CNSL) containing anacardic acids, wherein the bio-oil comprises a phenol derivative derived from the anacardic acids. Here, the bio-oil according to the twelfth aspect may be produced by at least one method for producing a biofuel among the first to eighth aspects. In addition, the bio-oil according to the twelfth aspect may be produced by at least one apparatus for producing a biofuel among the ninth to eleventh aspects.

[0031] According to the 13th aspect of the present invention, in the 12th aspect, the content of the anacardic acid may be 60 to 70 wt% based on the total weight of the cashew oil.

[0032] According to the fourteenth aspect of the present invention, in the twelfth or thirteenth aspect, the phenol derivative may include at least one of the compounds represented by the following chemical formulas 1 to 3.

[0033] [Chemical Formula 1]

[0034]

[0035] [Chemical Formula 2]

[0036]

[0037] [Chemical Formula 3]

[0038]

[0039] In the above chemical formulas 1 to 3, R1 to R3 are each independently a carbon chain functional group having 15 carbon atoms and including at least one of an unsaturated bond and a saturated bond.

[0040] According to the fifteenth aspect of the present invention, in the fourteenth aspect, the bio-oil may include 70 to 80 wt% of the compound represented by the chemical formula 1 and 10 to 20 wt% of the compound represented by the chemical formula 2.

[0041] According to the 16th aspect of the present invention, in the 14th or 15th aspect, the bio-oil may further include more than 0 and less than 10 wt% of the compound represented by the chemical formula 3.

[0042] The above solutions to the problem do not enumerate all features of the present invention. The various features of the present invention, along with their corresponding advantages and effects, can be understood in more detail by referring to the specific examples below.

[0043] According to one aspect of the present invention, a method for producing a biofuel having a high calorific value can be implemented through a simple process.

[0044] According to another aspect of the present invention, a method for producing biofuel that is economical and simultaneously has carbon reduction and resource recycling effects can be implemented.

[0045] According to another aspect of the present invention, a method for producing biofuels having various applications, such as biodiesel, can be implemented.

[0046] In addition to the effects described above, specific effects of the present invention are described below while explaining specific details for carrying out the invention.

[0047] Figure 1a is a flow chart showing a method for producing biofuel according to one embodiment of the present invention.

[0048] Figure 1b illustrates a biofuel production device according to one embodiment of the present invention.

[0049] Figure 2 is a flow chart showing a method for producing biofuel according to one embodiment of the present invention.

[0050] Figure 3 is a DSC (Differential Scanning Calorimetry) graph of cashew nut shells according to the method of Example 1.

[0051] Figure 4 is a DSC graph of cashew oil according to the method of Example 1.

[0052] Figure 5a is a DSC graph of oil made from cornstalks. Figure 5b is a DSC graph of oil made from wood pellets. Figure 5c is a DSC graph of oil made from coffee grounds.

[0053] Figure 6a is a DSC graph and a calculation formula for confirming the exothermic characteristics of the cashew nut shell according to Example 1 at 200 to 300°C.

[0054] Figure 6b is a DSC graph and a calculation formula for confirming the exothermic characteristics of cashew oil according to Example 1 at 200 to 300°C.

[0055] Figure 7 is a graph showing the specific heat (Cp) according to each temperature for cashew nut shells (CNS), cashew oil (CNSL), corn stover, wood pellets, and coffee husks.

[0056] In this specification, singular expressions include plural expressions unless the context clearly indicates otherwise.

[0057] The term “connection” as used herein refers not only to the direct connection of certain elements, but also includes an indirect connection where another element is interposed between the elements.

[0058] If multiple embodiments are described in this specification, the embodiments may be combined unless specifically stated otherwise. In this case, the effects of the present invention may be defined as including the effects derived from each embodiment and the effects resulting from the organic combination of the embodiments. For example, even if Embodiments 1 and 2 are described independently in this specification, Embodiments 1 and 2 may be organically combined with each other, unless the context clearly indicates otherwise, and the effects of the present invention may include the effects resulting from the combination of Embodiments 1 and 2.

[0059] The numerical range indicated by the term "to" in this specification refers to a numerical range that includes the values ​​described before and after the term as the lower limit and the upper limit, respectively. When multiple numerical values ​​are disclosed as the upper and lower limits of an arbitrary numerical range, the numerical range disclosed in this specification can be understood as any numerical range that has any one of the multiple lower limit values ​​and any one of the multiple upper limit values ​​as the lower limit and the upper limit, respectively. For example, when a to b, or c to d is described in the specification, it can be understood that a or more and b or less, a or more and d or less, c or more and d or less, or c or more and b or less is described.

[0060] In this specification, “comprising at least one of a, b and c” may include a, b or c alone, or a combination of two or more selected from the group consisting of ab and c.

[0061] As used herein, terms such as "about" or "substantially" refer to a reasonable amount of variation from the modified term that does not significantly alter the final result. These terms may be interpreted to include a variation of at least ±5% or at least ±10%, provided that such variation does not alter the meaning of the term and render it invalid.

[0062] 1. Method for producing biofuel

[0063] Previously, mechanical extraction methods, primarily used to convert cashew oil (CNSL) obtained from cashew nut shells into biofuel, resulted in the extraction of cashew oil containing a large amount of impurities, including ash. Using cashew oil containing such a large amount of ash as fuel can cause various problems, including corrosion, fouling, and slagging in engines or power plants. It can also reduce the reactivity of high-value-added products, such as curing agents, surfactants, and resins. Furthermore, anacardic acid, the main component of cashew oil, causes dermatitis and rashes upon contact with skin, necessitating its conversion to cardanol while simultaneously removing the impurities. From another perspective, when producing cashew shell oil by mechanical pressing of cashew shells, additional processes such as a heat treatment process to convert anacardic acid to cardanol, a reaction to esterify free fatty acids, and a separation process to remove impurities were required to produce bio-heavy oil from the cashew shell oil. In other words, the requirement of additional processes led to increased manufacturing costs and excessive requirement of processing equipment.

[0064] According to one aspect of the present invention, a method for producing a biofuel is provided, comprising the steps of (S1) preparing a raw material including at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks; and (S2) pyrolyzing the raw material using a pyrolysis method to obtain a sub-gas, biochar, and bio-oil. According to one aspect of the present invention, by including the steps of (S1) preparing a raw material including at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks; and (S2) pyrolyzing the raw material using a pyrolysis method to obtain a sub-gas, biochar, and bio-oil, a method for producing a biofuel can be implemented by a simple process to realize bio-oil having a high calorific value, while being economical and having carbon reduction and resource recycling effects at the same time. Through this, a biofuel with various applications such as biodiesel can be implemented. According to another aspect of the present invention, the manufacturing cost is significantly reduced compared to a mechanical oil extraction method, separate equipment for producing bio-heavy oil is not required, and the yield of bio-heavy oil is increased, so that economic feasibility can be further improved.

[0065] (S1) A step of preparing a raw material including at least one of cashew nut shell, cashew nut shell cake, vegetable oil residue and husk;

[0066] A method for producing biofuel according to the present invention comprises a step of preparing a raw material comprising at least one of cashew nut shells (CNS), cashew nut shell cakes (CNSC), vegetable oil residues, and husks. Specifically, the raw material may be a biomass that is subject to pyrolysis and may be an easily available and environmentally friendly material.

[0067] In some examples, the vegetable oil residue may be residue generated from a plant producing the vegetable oil. Specifically, the vegetable oil in the vegetable oil residue may include at least one of palm oil, soybean oil, coconut oil, rapeseed oil, olive oil, corn oil, and peanut oil, and more specifically, palm oil.

[0068] In some examples, the husk may refer to the shell or by-product of the husk raw material, and may specifically include at least one of coffee husk, palm kernel shell (PKS), and grain husk, and more specifically may include coffee husk. Here, the coffee husk may refer to the shell surrounding green coffee beans; or the shell that occurs before the green coffee beans are harvested and the coffee beans are extracted. In some examples, the palm oil husk may be the shell surrounding the edible seeds of the oil palm fruit. In some examples, the grains that are the raw material of the grain husk may be rice, hulled barley, rice barley, wheat, oats, rye, corn, millet, barley, sorghum, buckwheat, etc.

[0069] In some examples, when two or more kinds of the raw materials are included, the contents of the cashew nut shell, the cashew nut shell cake, the vegetable oil residue, and the husk may each independently be 15 wt% or more, 20 wt% or more, 25 wt% or more, 30 wt% or more, 35 wt% or more, and specifically 20 to 40 wt%, based on the total weight of the raw materials.

[0070] In some examples, the content of the vegetable oil residue may be 15 to 25 wt%, 16 to 24 wt%, 17 to 23 wt%, 18 to 22 wt%, 19 to 21 wt%, or 20 to 21 wt% based on the total weight of the raw material.

[0071] In some examples, the content of the husk may be 15 to 25 wt%, 16 to 24 wt%, 17 to 23 wt%, 18 to 22 wt%, 19 to 21 wt%, or 20 to 21 wt%, based on the total weight of the raw material.

[0072] (S2) A step of pyrolyzing the above raw material using a pyrolysis method to obtain sub-gas, biochar, and bio-oil.

[0073] The method for producing biofuel according to the present invention includes a step of pyrolyzing the raw material using a pyrolysis method (S2) without generating toxic gases, hazardous wastes and wastewater to obtain sub-gas, biochar and bio-oil.

[0074] Specifically, the pyrolysis method is not particularly limited and may be a method of applying heat to the raw material by various heat treatment means. In some examples, the pyrolysis method may include at least one of rotary kiln pyrolysis, fluidized bed pyrolysis, batch pyrolysis, and screw pyrolysis, and specifically may include a rotary kiln pyrolysis method. According to some embodiments of the present invention, when the rotary kiln pyrolysis method is used as the pyrolysis method, the raw material can flow due to mixing and blending motion caused by the rotation of the kiln body compared to other pyrolysis methods, so that the pyrolysis time can be shortened, and at the same time, the heat required for pyrolysis can be supplied to the solid raw material as quickly as possible, thereby further increasing the yield of biofuel.

[0075] In some examples, the rotary kiln pyrolysis method can be performed through a general rotary kiln reactor commercially available in the art. Specifically, the rotary kiln pyrolysis method can be performed at a temperature of 300 to 600°C under atmospheric pressure for 1 to 60 minutes, preferably at a temperature of 350 to 550°C under atmospheric pressure for 10 to 50 minutes, and most preferably at a temperature of 450 to 490°C under atmospheric pressure for 20 to 30 minutes. At this time, if any one of the pressure, temperature, and time conditions of the pyrolysis does not satisfy the above range, the production yield of biochar and bio-oil from the cashew nut shell may be significantly low, or a large amount of impurities and anacardic acid may be included, resulting in low purity and causing dermatitis and rash upon contact with the skin.

[0076] In some examples, the fluidized bed pyrolysis method can be performed using various fluidized bed reactors commonly used in the art. Fluidized bed reactors are typically used under rapid pyrolysis conditions and can have a short residence time. Specifically, the fluidized bed pyrolysis method can be performed at a temperature of 480 to 500°C under atmospheric pressure for 1 to 5 minutes.

[0077] In some examples, the batch pyrolysis process may be performed using a typical batch pyrolysis reactor commonly used in the art. Specifically, the batch pyrolysis process may be performed at a temperature of 480 to 500°C under atmospheric pressure for 90 to 120 minutes.

[0078] In some examples, the screw pyrolysis method may be performed using a typical screw pyrolysis reactor commonly used in the relevant technical field. Specifically, the screw pyrolysis method may be performed at a temperature of 480 to 500°C under atmospheric pressure for 60 to 80 minutes. At this time, the rotation speed of the screw is not particularly limited, but may be specifically controlled to 15 to 20 rpm.

[0079] The sub-gas according to the present invention may be a gas generated in the process of pyrolyzing the raw material. In this case, if the sub-gas is simply discharged, a separate treatment facility for discharging the sub-gas may be required. In some embodiments of the present invention, the sub-gas may be reused as a heat source for the pyrolysis method. Here, the sub-gas may be supplied to a reactor performing the pyrolysis method through a gas path and reused as a heat source for pyrolyzing the raw material. According to some embodiments of the present invention, by reusing the sub-gas as a heat source for the pyrolysis method, the efficiency of the manufacturing cost and heat treatment process can be further improved by using the sub-gas as a heat source without a separate treatment facility, thereby further increasing the yield of bio-oil. The principle of reusing the sub-gas as a heat source for the pyrolysis method is described in detail in the description of FIG. 1B.

[0080] In some examples, the sub-gas may include at least one of a light hydrocarbon gas having less than 4 carbon atoms, a light aliphatic hydrocarbon gas having 4 to 5 carbon atoms, and a light naphtha hydrocarbon gas having 5 to 6 carbon atoms. Here, based on the total volume of the sub-gas, the content of the light hydrocarbon gas having less than 4 carbon atoms may be 75 to 80% (v / v), the content of the light aliphatic hydrocarbon gas having 4 to 5 carbon atoms may be 10 to 15% (v / v), and the content of the light naphtha hydrocarbon gas having 5 to 6 carbon atoms may be 10 to 15% (v / v).

[0081] In some embodiments of the present invention, the bio-oil may include a phenol derivative, and specifically, the phenol derivative may include at least one of the compounds represented by the following chemical formulae 1 to 3.

[0082] [Chemical Formula 1]

[0083]

[0084] [Chemical Formula 2]

[0085]

[0086] [Chemical Formula 3]

[0087]

[0088] In the above chemical formulas 1 to 3, R1 to R3 are each independently a carbon chain functional group having 15 carbon atoms and including at least one of an unsaturated bond and a saturated bond.

[0089] In some embodiments of the present invention, the bio-oil can be used directly as a biofuel. If necessary, an additional step of concentrating the bio-oil to produce biofuel may be provided, and a commercially available vacuum concentrator may be used as a means for concentrating the bio-oil.

[0090] In some embodiments of the present invention, a method for producing a biofuel may be provided, comprising at least one of: (S3a) forming the biochar into pellets to produce a first biofuel; and (S3b) trans-esterifying the bio-oil to produce a second biofuel. Specifically, steps (S3a) and (S3b) may be performed independently. In some examples, steps (S3a) and (S3b) may be performed simultaneously, or steps (S3a) and (S3b) may be performed in that order, or steps (S3b) and (S3a) may be performed in that order.

[0091] Specifically, in the step (S3a), a ring die, a vertical ring die, a flat die, or a gear-type forming device may be used as a device for forming the biochar into pellets. At this time, the process conditions for forming into pellets may be adjusted such that the moisture content factor is 12 to 15% and the particle size is 450 to 600 μm.

[0092] Specifically, in the step (S3b), a batch heat treatment mixing device may be used as a device for inducing a trans-esterification reaction of the bio-oil. At this time, the process conditions for inducing the trans-esterification reaction of the bio-oil may be controlled by heat treatment conditions of 70 to 80°C using an acid catalyst and alcohol. For example, the content of the acid catalyst may be 1 wt% based on the total weight of the reaction solution, and the volume ratio of the acid catalyst (e.g., sulfuric acid) and alcohol may be 1:3. Here, the reaction solution may be a mixture containing bio-oil, an acid catalyst, and alcohol.

[0093] Hereinafter, the configuration of the present invention will be described in more detail with reference to Fig. 1a.

[0094] Figure 1a is a flow chart showing a method for producing biofuel according to one embodiment of the present invention.

[0095] Referring to FIG. 1a, a method for producing a biofuel according to one embodiment of the present invention may include the steps of (S10) preparing a raw material including at least one of cashew nut shells, cashew nut shell cakes, palm oil residues, and coffee husks; and (S20) pyrolyzing the raw material using a pyrolysis method to obtain a sub-gas, biochar, and bio-oil. In this case, the steps of (S30a) forming the biochar into pellets to produce a first biofuel; and (S30b) trans-esterifying the bio-oil to produce a second biofuel may each be performed independently.

[0096] 2. Biofuel production facility

[0097] According to another aspect of the present invention, a biofuel production device is provided, comprising: a raw material injection unit into which raw materials are injected; a pyrolysis reactor connected to the raw material injection unit; a cooler connected to the pyrolysis reactor; a heat exchanger connected to the pyrolysis reactor; a first recovery unit connected to the cooler and for recovering biochar; and a second recovery unit connected to the heat exchanger and for recovering bio-oil; wherein the raw material includes at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks.

[0098] Hereinafter, the configuration of the present invention will be described in more detail with reference to FIG. 1b. Parts described above and repeated descriptions will be briefly explained or omitted.

[0099] Figure 1b illustrates a biofuel production device according to one embodiment of the present invention.

[0100] Referring to FIG. 1b, a biofuel production device (1000) according to the present invention includes a raw material injection unit (100), a pyrolysis reactor (200), a cooler (400), a heat exchanger (500), a first recovery unit (P1), and a second recovery unit (P2).

[0101] Raw material injection unit (100)

[0102] The raw material injection unit (100) according to the present invention may be a device that receives raw materials and homogeneously mixes the received raw materials.

[0103] In some examples, the raw material injection unit (100) may include a sub-injection unit (10) and a mixing unit (20) connected to the sub-injection unit (10). For example, the raw material may be injected into the raw material injection unit (100) through a hole provided in the sub-injection unit (10) and then homogeneously mixed through the mixing unit (20). For example, the mixing unit (20) may be a single-screw or twin-screw device.

[0104] The raw material according to the present invention includes at least one of cashew nut shells, cashew nut shell cakes, vegetable oil residues, and husks.

[0105] Pyrolysis reactor (200)

[0106] The pyrolysis reactor (200) according to the present invention can produce sub-gas, preliminary biochar, and preliminary bio-oil by pyrolyzing the raw material injected through the raw material injection unit (100). Here, preliminary biochar may refer to a solid substance that is a previous state of biochar, and preliminary bio-oil may refer to a previous state of bio-oil, specifically, a state before passing through a heat exchanger.

[0107] The pyrolysis reactor (200) according to the present invention is connected to the raw material injection unit (100), and specifically, the pyrolysis reactor (200) can be directly connected to the raw material injection unit (100).

[0108] In some embodiments of the present invention, the pyrolysis reactor (200) may include at least one of a rotary kiln reactor, a fluidized bed reactor, a batch pyrolysis reactor, and a screw pyrolysis reactor, and specifically, may include a rotary kiln reactor. According to some embodiments of the present invention, when the rotary kiln reactor is used, the raw material can flow through a mixing and blending motion by the rotation of the kiln body compared to other reactors, so that the pyrolysis time can be shortened, and at the same time, the heat required for pyrolysis can be supplied to the solid raw material as quickly as possible, thereby further increasing the yield of biofuel.

[0109] Cooler (400)

[0110] The cooler (400) according to the present invention can cool or cool the preliminary biochar obtained in the thermal decomposition process.

[0111] In some examples, the cooler (400) is not particularly limited and may include various means for cooling the preliminary biochar. Specifically, an indirect rotary kiln type may be used to cool the preliminary biochar. Specifically, the preliminary biochar may be cooled using air or cooling water on the outer wall of the kiln. Here, the cooling water may be supplied through a cooling tower (410) described below.

[0112] Heat exchanger (500)

[0113] The heat exchanger (500) according to the present invention is a device that efficiently transfers heat by utilizing different temperature differences between fluids, and may be a device that transfers the heat of the reserve bio-oil obtained in the thermal decomposition process. Specifically, the temperature of the reserve bio-oil can be indirectly lowered through cooling water supplied through a cooling tower (410) described later. By lowering the temperature of the reserve bio-oil through the cooling method, the bio-oil can be recovered in a liquid phase through a first recovery unit (P1) described later.

[0114] The heat exchanger (500) according to the present invention can produce bio-oil by transferring the heat of the preliminary bio-oil. Specifically, the heat exchanger (500) can be connected to the pyrolysis reactor (200), and more specifically, can be indirectly connected. At this time, a dust collector (300) can be interposed between the heat exchanger (500) and the pyrolysis reactor (200). Here, the dust collector (300) can separate the solid or liquid dust generated during the pyrolysis process from the sub-gas by rotating the sub-gas by centrifugal force. For example, the dust collector (300) can be a dry cyclone.

[0115] For example, the sub-gas may be generated during the thermal decomposition process of the thermal decomposition reactor (200) and may be entirely transferred to the dust collector (300) described later without moving to the cooler (400).

[0116] First recovery unit (P1) and second recovery unit (P2)

[0117] The first recovery unit (P1) according to the present invention is connected to the heat exchanger (500) and can recover bio-oil.

[0118] The second recovery unit (P2) according to the present invention is connected to the cooler (400) and can recover biochar.

[0119] Specifically, the first and second recovery units (P1, P2) can be indirectly connected to each other.

[0120] Other components

[0121] The biofuel production device (1000) according to the present invention may further include a blower (700) connected to the heat exchanger (500). For example, the blower (700) may serve to transport the sub-gas discharged from the heat exchanger (500) to a combustion device (800) to be described later.

[0122] The biofuel production device (1000) according to the present invention may further include a cooling tower (410) connected to the heat exchanger (500) and the cooler (400). For example, the cooling tower (410) lowers the temperature of cooling water whose temperature has increased for heat exchange, and supplies the cooling water whose temperature has decreased back to the heat exchanger (500) and / or the cooler (400). In relation to the heat exchanger (500), the cooling tower (410) may lower the temperature of the sub-gas generated during the pyrolysis process and contribute to the recovery of bio-oil, and in relation to the cooler (400), may lower the temperature of the reserve biochar to prevent fire during biochar recovery.

[0123] The biofuel production device (1000) according to the present invention may further include a combustion device (800) connected to the blower (700). Specifically, the combustion device (800) may be connected to the pyrolysis reactor (200) and the heat exchanger (500), and more specifically, may be directly connected to the pyrolysis reactor (200) or indirectly connected to the heat exchanger (500). For example, the combustion device (800) may perform a role of recovering and combusting a sub-gas (uncondensed gas) discharged from the heat exchanger (500) to supply it as a heat source to the pyrolysis reactor (200), and CO2, CO, NOx (x is 1 or 2), etc. may be generated through the combustion device (800).

[0124] Although not specifically shown in Fig. 1b, a gas transport device (not shown) may be additionally provided between the combustion device (800) and the pyrolysis reactor (200) to transport the sub-gas combusted in the combustion device (800) to the pyrolysis reactor (200).

[0125] In some examples, the temperature of the sub-gas combusted through the combustion device (800) is not particularly limited and may be a temperature capable of pyrolyzing the raw material in the pyrolysis reactor (200), and specifically may be 300 to 600°C, 400 to 500°C, or 450 to 490°C.

[0126] 3. Bio-oil

[0127] According to another aspect of the present invention, a bio-oil is provided derived from cashew nut shell liquid (CNSL) containing anacardic acid, wherein the bio-oil comprises a phenol derivative derived from the anacardic acid. In some examples, the anacardic acid can be thermally decomposed into one or more phenol derivatives. Specifically, the phenol derivatives can be defined as compounds containing a phenol structure as a parent (ballast).

[0128] According to another embodiment of the present invention, the raw material of the bio-oil may be any one selected from the group consisting of cashew nut shell (CNS), cashew nut shell cake (CNSC), and combinations thereof, as a raw material to be thermally decomposed.

[0129] The anacadic acid according to the present invention may be a benzoic acid derivative having a carboxyl group bonded to a benzene ring as a phenolic lipid. Specifically, the anacadic acid can be converted into a phenol derivative, which will be described later, under certain thermal conditions. At this time, the carboxyl group bonded to the benzene ring can be removed through decarboxylation under the thermal conditions.

[0130] In some embodiments of the present invention, the content of the anacardic acid may be 60 to 70 wt%, 61 to 69 wt%, 62 to 68 wt%, 63 to 67 wt%, 64 to 67 wt%, 65 to 67 wt%, or 66 to 67 wt% based on the total weight of the cashew oil. According to some embodiments of the present invention, when the content of the anacardic acid is less than the numerical range, the content of the phenol derivative included in the bio-oil may decrease, which may cause a problem of lowering the production yield of the bio-oil, and when the content of the anacardic acid remaining in the bio-oil exceeds the numerical range, the content of the anacardic acid remaining in the bio-oil may increase, which may cause a problem of lowering the yield of the bio-oil or increasing the content of impurities.

[0131] The phenol derivative according to the present invention may be a product of the conversion of the anacardic acid through a chemical reaction. In some examples, the anacardic acid may be converted into the phenol derivative through a decarboxylation reaction under thermal conditions.

[0132] In some embodiments of the present invention, the phenol derivative may include at least one of the compounds represented by the following chemical formulas 1 to 3.

[0133] [Chemical Formula 1]

[0134]

[0135] [Chemical Formula 2]

[0136]

[0137] [Chemical Formula 3]

[0138]

[0139] In the above chemical formulae 1 to 3, R1 to R3 may each independently be a carbon chain functional group having 15 carbon atoms that includes at least one of an unsaturated bond and a saturated bond. Here, the unsaturated bond may include at least one of a carbon-carbon double bond and a carbon-carbon triple bond, and specifically, may include a carbon-carbon double bond. In some examples, the carbon chain functional group may be a straight-chain or branched alkyl group having 15 carbon atoms; or a substituent in which at least one carbon-carbon single bond bonded to the alkyl group is replaced with a double bond.

[0140] In some examples, R1 to R3 are each the same substituent, and may be any one or more of the following chemical formulas 4a to 4d, specifically 4a. Here, “*” may indicate a point of connection to another part in the molecule.

[0141] [Chemical Formula 4a]

[0142]

[0143] [Chemical Formula 4b]

[0144]

[0145] [Chemical formula 4c]

[0146]

[0147] [Chemical formula 4d]

[0148]

[0149] In some embodiments of the present invention, the bio-oil may comprise 70 to 80 wt% of the compound represented by the chemical formula 1 and 10 to 20 wt% of the compound represented by the chemical formula 2, based on the total weight of the bio-oil. In some examples, the content of the compound represented by the chemical formula 1 may be 71 to 79 wt%, 72 to 78 wt%, 73 to 77 wt%, 74 to 76 wt%, or 75 to 76 wt%, based on the total weight of the bio-oil. In some examples, the content of the compound represented by the chemical formula 2 may be 11 to 19 wt%, 12 to 18 wt%, 13 to 17 wt%, 14 to 16 wt%, or 15 to 16 wt%, based on the total weight of the bio-oil. According to some embodiments of the present invention, if the content of the compounds represented by the above chemical formulas 1 and 2 does not satisfy the above numerical range, a problem of not satisfying the bio-heavy oil standard may occur.

[0150] In some embodiments of the present invention, the bio-oil may further include more than 0 and less than 10 wt% of the compound represented by the chemical formula 3. In some examples, the content of the compound represented by the chemical formula 3 may be 1 to 10 wt%, 2 to 9 wt%, 3 to 8 wt%, 4 to 7 wt%, or 5 to 6 wt%. According to some embodiments of the present invention, if the content of the compound represented by the chemical formula 3 does not satisfy the numerical range or exceeds the numerical range, a problem of not satisfying the bio-heavy oil standard may occur.

[0151] For example, the content of the compounds represented by the above-described chemical formulas 1 to 3 can be analyzed through a GC-MS (Gas chromatography mass spectrometry) analysis method commonly used in the relevant technical field.

[0152] In some embodiments of the present invention, the content of the phenol derivative may be 70 to 100 wt%, 71 to 79 wt%, 72 to 78 wt%, 73 to 77 wt%, 74 to 76 wt%, or 75 to 76 wt% based on the total weight of the bio-oil. According to some embodiments of the present invention, when the content of the phenol derivative satisfies the numerical range, the yield and purity of the bio-oil are further increased, and the biofuel properties can be excellently expressed. For example, the content of the phenol derivative described above can be analyzed through a GC-MS analysis method commonly used in the relevant technical field.

[0153] In some embodiments of the present invention, the cashew oil can have exothermic properties at 150 to 500°C, specifically at 200 to 350°C, and more specifically at 200 to 300°C. In some examples, the specific heat (Cp) of the cashew oil at 200°C or higher can be 20 W / g·°C or higher. Specifically, the specific heat (Cp) of the cashew oil can be 20 to 50 W / g·°C, 25 to 45 W / g·°C, or 30 to 45 W / g·°C at 250 to 300°C. For example, the exothermic properties of the cashew oil can be analyzed using a Differential Scanning Calorimetry (DSC) analysis method under analysis conditions of a nitrogen flow rate of 50 ml / min, a temperature increase rate of 20°C / min, and a temperature increase rate of 25 to 500°C.

[0154] According to another aspect of the present invention, a biofuel manufactured from bio-oil according to certain embodiments may be provided. In some examples, the biofuel may be, without limitation, biodiesel, and may specifically be a transportation fuel. In still other examples, the biofuel may be any one selected from the group consisting of a land improver, a pyrolysis heat source, and a wood pellet boiler fuel.

[0155] In some examples, the bio-oil can undergo an esterification reaction by reacting with an acid compound containing a carboxyl group. Subsequently, bio-heavy oil can be obtained through an esterification reaction and an ash removal reaction and an impurity removal reaction at temperatures above approximately 80°C.

[0156] Figure 2 is a flow chart showing a method for producing biofuel according to one embodiment of the present invention.

[0157] Referring to FIG. 2, a method for producing biofuel according to one embodiment of the present invention may include a step of separating cashew nuts and cashew nut shells from cashews obtained from a cashew tree; and a step of pyrolyzing the cashew nut shells to obtain biochar and bio oil.

[0158] In some examples, the pyrolysis can recover almost all of the oil contained in the cashew nut shell, thereby significantly improving productivity compared to the existing mechanical extraction process. The pyrolysis can be performed at a temperature of 300 to 600°C under atmospheric pressure for 1 to 60 minutes, preferably at a temperature of 350 to 550°C under atmospheric pressure for 10 to 50 minutes, and most preferably at a temperature of 450 to 490°C under atmospheric pressure for 20 to 30 minutes. In this case, if any one of the pressure, temperature, and time conditions of the pyrolysis does not satisfy the above range, the production yield of biochar and bio-oil from the cashew nut shell is significantly low, or there is a problem that the purity is low due to the inclusion of a large amount of impurities and anacardic acid, and dermatitis and rash are induced when in contact with the skin.

[0159] In some examples, the biochar may have a calorific value of 5,000 to 8,000 kcal / kg, a moisture content of 1 to 8 wt%, and an ash content of 1 to 7 wt%, preferably a calorific value of 5,700 to 7,300 kcal / kg, a moisture content of 2 to 7 wt%, and an ash content of 4 to 6.8 wt%, and most preferably a calorific value of 6,400 to 7,290 kcal / kg, a moisture content of 2 to 5 wt%, and an ash content of 5.5 to 6.5 wt%.

[0160] The above biochar has a low moisture content and high calorific value, so it can be used as a heat source for the pyrolysis process, and has the advantage of being applicable as a land improvement agent that can improve plant growth along with a carbon sequestration effect.

[0161] In some examples, the bio-oil may be a bio-heavy oil containing 1 to 20 ppm of potassium (K), preferably 2 to 17 ppm, and 1 to 5 ppm of sodium (Na), preferably 1 to 4 ppm, based on the total bio-oil content. The bio-oil has very low contents of calcium and sodium, which are ash-inducing components, so that a high-purity bio-oil can be obtained, and the bio-oil can be used directly as bio-heavy oil without a separate refining process. The bio-heavy oil can be used as fuel for power generation or ships.

[0162] In some examples, the bio-oil may have a calorific value of 8,000 to 9,800 kcal / kg, a total acid value of 5 to 20 mgKOH / g, and an oil production yield of 30% or more, preferably 8,200 to 9,100 kcal / kg, a total acid value of 7 to 13 mgKOH / g, and an oil production yield of 35% or more, and most preferably, the bio-oil may have a calorific value of 9,000 to 9,700 kcal / kg, a total acid value of 10 to 12 mgKOH / g, and an oil production yield of 40% or more.

[0163] Hereinafter, embodiments of the present invention will be described in detail so that those skilled in the art can easily implement the present invention. However, this is merely an example, and the scope of the present invention is not limited by the following contents.

[0164] [Manufacturing Example 1: Biofuel Production]

[0165] <Comparative Example 1: Method for Obtaining Cashew Shell Cake and Cashew Oil Using a Mechanical Extraction Method>

[0166] Cashews obtained from a cashew tree were separated into cashew nuts and cashew nut shells by a mechanical stripping method. Here, the content of cashew oil (cashew nut shell liquid) contained in the cashew nut shell was 20 wt%, and the content of anacardic acids contained in the cashew oil was 67 wt%.

[0167] The above 10 kg of cashew nut shells were mechanically extracted using a press at a pressure of 0.25 MPa and room temperature for 10 minutes to obtain 8 kg of cashew nut shell cake and 2 kg of cashew oil.

[0168] <Example 1: Method for obtaining biochar and bio-oil using a pyrolysis method>

[0169] Steps to separate cashews from their shells:

[0170] Cashew nuts and cashew nut shells were separated from cashews using the same method as in Comparative Example 1. Here, the content of cashew oil (cashew nut shell liquid) contained in the cashew nut shell was 30 wt%, and the content of anacardic acid contained in the cashew oil was 67 wt%. The content of anacardic acid contained in the cashew oil was measured using a GC-MS analysis method.

[0171] Steps to pyrolyze cashew shells:

[0172] After 1,000 kg of the above cashew nut shells were placed in a rotary-kiln type pyrolysis reactor, pyrolysis was performed at a temperature of 470°C for 30 minutes under conditions of atmospheric pressure and an oxygen concentration of 5% inside the reactor, thereby obtaining 350 kg of biochar and 400 kg of bio-oil.

[0173] <Example 2: Unlike Example 1, cashew shell cake was used instead of cashew shell>

[0174] Bio-oil was obtained in the same manner as in Example 1, but instead of the cashew nut shells, 1,000 kg of cashew nut shell cake prepared in the manner described in Comparative Example 1 was introduced into a rotary kiln-type pyrolysis reactor. As a result, 300 kg of biochar and 350 kg of bio-oil were obtained.

[0175] [Experimental Example 1: Characteristic Analysis of Cashew Oil]

[0176] The exothermic temperature and specific heat of cashew oil according to Example 1 were measured under the analysis method and analysis conditions described in Table 1 below.

[0177] Cashew oil exothermic temperature of Example 1 of the analysis method and analysis conditions ( oC)DSC nitrogen flow rate 50ml / min, temperature increase 20℃ / min, temperature increase 25 ~ 500℃, heat generation temperature 200~300℃, specific heat (W / g℃)DSC nitrogen flow rate 50ml / min, temperature increase 20℃ / min, temperature increase 25 ~ 500℃, 20 W / g℃ or more (condition of 200℃ or more)

[0178] Figure 3 is a DSC graph of cashew nut shells prepared according to the method of Example 1. Figure 4 is a DSC graph of cashew oil prepared according to the method of Example 1. Figure 5a is a DSC graph of oil prepared using corn stalks as a raw material. Figure 5b is a DSC graph of oil prepared using wood pellets as a raw material. Figure 5c is a DSC graph of oil prepared using coffee grounds as a raw material.

[0179] Figure 6a is a DSC graph and a calculation formula for confirming the exothermic characteristics of cashew nut shells according to Example 1 at 200 to 300°C. Figure 6b is a DSC graph and a calculation formula for confirming the exothermic characteristics of cashew oil according to Example 1 at 200 to 300°C. Figure 7 is a graph showing the specific heat (Cp) according to each temperature for cashew nut shells (CNS), cashew oil (CNSL), corn stover, wood pellets, and coffee husks.

[0180] Referring to FIGS. 3 to 7, it can be confirmed that, in the method according to Example 1, cashew nut shells and cashew oil undergo an exothermic reaction at about 200 to 300°C, unlike other raw materials. Specifically, the exothermic characteristics in FIGS. 6a and 6b can be calculated using the following equations 1 and 2.

[0181] [Formula 1]

[0182] y = 5E-09x 6 - 8E-06x 5 + 0.0053x 4 - 1.8253x 3 + 350.5x 2 - 35773x + 2E+06

[0183] [Formula 2]

[0184] y = -1E-10x 6 + 2E-07x 5 - 1E-04x 4 + 0.033x 3 - 6.0981x 2 + 596.35x - 24123

[0185] In the above equations 1 and 2, x is temperature (℃) and y is heat flow (W / g).

[0186] [Experimental Example 2: Analysis of Biochar and Bio-Oil]

[0187] For the biochar and bio-oil obtained in Examples 1 and 2 and Comparative Example 1, the calorific value of the biochar, the moisture and ash contents of the biochar, and the calorific value (LHV), K content, Na content, total acid value, and oil production yield of the bio-oil were measured, and the results are shown in Tables 2 and 3 below.

[0188] Comparative example of classification analysis method Example 1 Example 1 Example 2 Bio heavy oil required properties Calorific value (LHV) of biochar (kcal / kg) Calorific value meter (Ministry of Environment Notice No. 2020-219) 7,000 7,290 7,020 - K content of bio oil (ppm) ICP-OES 9,000 31750 or less Na content of bio oil (ppm) ICP-OES 1,000 3450 or less Total acid number of bio oil (mg KOH / g) Total acid number measurement (color indicator titration method, KS M ISO 6618:1997) 321 110.9725 or less Oil production yield (%) (Output / Input) X 100 640 35 -

[0189] Comparative example of classification analysis method Example 1 Example 1 Example 2 Moisture (weight%) Moisture measurement (Ministry of Environment Notice No. 2020-219) 10 or more 24.4 ash (weight%) Ash measurement (Ministry of Environment Notice No. 2020-219) 1.96.26.2

[0190] In addition, the components in the biochar (Table 4) and bio-oil (Table 5) obtained in Example 1 were analyzed using a fuel properties analysis method (KS M 0010:2016, KS M ISO 6245:2001, KS M 2057:2006, KS M ISO 10370:2014, Ministry of Environment Notice No. 2020-219, ASTM D7582-15, ICP-OES), and the results are shown in Tables 4 and 5 below.

[0191] Biochar industrial analysis wt% Biochar elemental analysis wt% (ash free) Chlorine wt% Calorific value kcal / kg Moisture Ash Volatile matter Fixed carbon CHNOSCl High Low 2.006.2012.6079.2086.253.231.309.210.010.0372907120

[0192] Bio-oil industrial analysis wt% Bio-oil elemental analysis wt% (ash free) Calorific value kcal / kg Alkali metal ppm Moisture Ash Volatile matter Residual carbon CHNOS High Low NaK 0.10 0.20 9 8.8 8 0.8 2 8 3.0 2 10.4 8 0.3 16.1 8 0.0 1 9 6 10 9 0 3 0 3.0 0 3.0 0

[0193] [Experimental Example 3: Contents of anacardic acid in cashew oil and phenol derivatives in bio-oil]

[0194] In the method according to the above Example 1 or 2, the content of anacardic acid contained in cashew oil was measured using GC-MS analysis, and the content of a phenol derivative derived from anacardic acid was measured using GC-MS analysis. Specifically, the phenol derivative may be composed of cardanol, cardol, and 2-methyl cardol. In each of cardanol, cardol, and 2-methyl cardol, R1 to R3 bonded to a benzene ring are functional groups represented by the following chemical formula 4a.

[0195] [Chemical Formula 4a]

[0196]

[0197] Example 1 Example 2 Raw material Cashew nut shell (CNS) Cashew nut shell cake (CNSC) Anacardic acid content (% by weight) 0.00.0 Cardanol (% by weight) 95.4 94.7 Cardol (% by weight) 4.6 5.3 2-methyl cardol (% by weight) 0.00.0

[0198] Although the preferred embodiments of the present invention have been described in detail above, the scope of the present invention is not limited thereto, and various modifications and improvements made by those skilled in the art using the basic concept of the present invention defined in the following claims also fall within the scope of the present invention.

[0199] <Explanation of symbols>

[0200] 1000: Biofuel production facility 100: Raw material injection unit

[0201] 200: Pyrolysis reactor 300: Dust collector

[0202] 400: Cooler 500: Heat Exchanger

[0203] 410: Cooling tower 700: Blower

[0204] 800: Combustion device P1: First recovery unit

[0205] P2: Second Recovery Unit

Claims

1. (S1) A step of preparing a raw material including at least one of cashew nut shell, cashew nut shell cake, vegetable oil residue and husk; and (S2) a step of thermally decomposing the above raw material by a thermal decomposition method to obtain sub-gas, biochar and bio-oil; including; Method for producing biofuel.

2. In paragraph 1, The vegetable oil of the above vegetable oil residue is, Containing at least one of palm oil, soybean oil, coconut oil, rapeseed oil, olive oil, corn oil, and peanut oil, Method for producing biofuel.

3. In paragraph 1, The above husk, Containing at least one of coffee husk, palm oil husk (Palm kernel shell, PKS) and grain husk, Method for producing biofuel.

4. In paragraph 1, The above thermal decomposition method is, Comprising at least one method of rotary kiln pyrolysis, fluidized bed pyrolysis, batch pyrolysis, and screw pyrolysis. Method for producing biofuel.

5. In paragraph 1, The above sub-gas is reused as a heat source for the above thermal decomposition method. Method for producing biofuel.

6. In paragraph 1, The above bio-oil contains a phenol derivative. Method for producing biofuel.

7. In paragraph 6, The above phenol derivatives are, Comprising at least one compound represented by the following chemical formulas 1 to 3, Method for producing biofuel: [Chemical Formula 1] [Chemical formula 2] [Chemical Formula 3] In the above chemical formulas 1 to 3, R 1 Inland R 3 is a carbon chain functional group having 15 carbon atoms and containing at least one unsaturated bond and one or more saturated bonds.

8. In paragraph 1, (S3a) a step of manufacturing a first biofuel by forming the biochar into a pellet; and (S3b) a step of producing a second biofuel by trans-esterifying the bio-oil; further comprising at least one of: Method for producing biofuel.

9. Raw material injection section where raw materials are injected; A pyrolysis reactor connected to the above raw material injection unit; A cooler connected to the above pyrolysis reactor; A heat exchanger connected to the above pyrolysis reactor; A first recovery unit connected to the above cooler and recovering biochar; and A second recovery unit connected to the above heat exchanger and recovering bio-oil; The above raw materials are, Containing at least one of cashew nut shell, cashew nut shell cake, vegetable oil residue and husk, Biofuel production facility.

10. In paragraph 9, The above pyrolysis reactor is, Comprising at least one of a rotary kiln reactor, a fluidized bed reactor, a batch pyrolysis reactor, and a screw pyrolysis reactor, Biofuel production facility.

11. In paragraph 9, Further comprising a combustion device connected to the heat exchanger and the pyrolysis reactor; Biofuel production facility.

12. A bio-oil derived from cashew oil (Cashew nut shell liquid; CNSL) containing anacardic acids, The above bio-oil is, Comprising a phenol derivative derived from the above anacardic acid, Bio-oil.

13. In paragraph 12, The content of the above anacardic acid is 60 to 70 wt% based on the total weight of the cashew oil. Bio-oil.

14. In paragraph 12, The above phenol derivatives are, Comprising at least one compound represented by the following chemical formulas 1 to 3, Bio-oil: [Chemical Formula 1] [Chemical formula 2] [Chemical Formula 3] In the above chemical formulas 1 to 3, R 1 Inland R 3 are each independently a carbon chain functional group having 15 carbon atoms, each of which contains at least one unsaturated bond and one or more saturated bonds.

15. In paragraph 14, The above bio-oil is, 70 to 80 wt% of the compound represented by the chemical formula 1 and Comprising 10 to 20 wt% of a compound represented by the chemical formula 2 above, Bio-oil.

16. In paragraph 15, The above bio-oil is, Further comprising 0 to 10 wt% of a compound represented by the chemical formula 3, Bio-oil.

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