Preparation method for aviation fuel component, system, and aviation fuel component

Abstract

The present invention relates to a preparation method for an aviation fuel component, a system therefor, and an aviation fuel component obtained by means of the preparation method of the present invention. More specifically, the present invention relates to a preparation method for preparing an aviation fuel component by using biological feedstock oil, a system for implementing the method, and an aviation fuel component obtained by means of the preparation method of the present invention. In the present invention, by subjecting the biological feedstock oil to a reconstruction reaction, the biological feedstock oil can be converted into an aviation fuel component, and a high yield can be achieved. Additionally, the obtained aviation fuel component has high energy density and a low freezing point, and exhibits excellent performance when used as an aviation fuel component.

Description

Preparation methods and systems for aviation fuel components, and aviation fuel components Technical Field

[0001] This invention belongs to the field of renewable energy, specifically relating to a method and system for preparing aviation fuel components, and aviation fuel components obtained by the preparation method of this invention. More specifically, it relates to a method for preparing aviation fuel components using bio-based oil, a system for implementing the method, and aviation fuel components obtained by the preparation method of this invention. Background Technology

[0002] Aviation fuel kerosene is a crucial component of sustainable aviation fuel and holds immense potential in meeting the vast market demand. Currently, the main technologies for producing aviation fuel kerosene include direct hydrotreating of biomass feedstocks, the biomass FT-SPK synthesis process, and biomass pyrolysis.

[0003] In the aforementioned technologies, the hydroprocessed esters and fatty acids (HEFA) synthesis process involves hydrogenating and deoxygenating vegetable oils or waste oils to convert bio-based feedstocks into C64. 15 ~C 18 Alkanes, including straight-chain alkanes, are selectively hydrocrackinged to obtain products such as bio-aviation kerosene. CN117229804A discloses a method for preparing bio-aviation kerosene by hydrogenating waste oil. This process employs a two-stage hydrogenation process, which deoxygenates and isomerizes the waste oil to obtain aviation fuel components. CN118995260A discloses a method for producing bio-aviation kerosene by hydrogenating waste catering oil. This method utilizes a ZnO-supported Cu-Rh-phosphotungstic acid catalyst to catalyze the hydrogenation, deoxygenation, and isomerization of waste catering oil to produce bio-aviation kerosene.

[0004] The biomass Fischer-Tropsch synthesis of paraffinic kerosene (FT-SPK) process is similar to the traditional FT synthesis of hydrocarbons after coal gasification. This process first gasifies biomass under Fischer-Tropsch synthesis conditions to obtain a mixed gas component containing H2, CO, CO2, CH4, etc. The mixed gas component is then separated and purified. The resulting synthesis gas, mainly composed of H2 and CO, is then contacted with a catalyst to undergo a Fischer-Tropsch synthesis reaction, yielding n-alkanes with a broad carbon chain distribution. The liquid-phase product contains over 90% n-alkanes. However, the aviation kerosene component synthesized by FT (C7-C4)... 17 It has a low energy density, a relatively high freezing point, and poor fluidity at low temperatures, so it can only be used as a blending component.

[0005] The intermediate liquid phase product of bio-oil obtained by biomass pyrolysis has high viscosity, complex composition and high oxygen content. Therefore, the obtained bio-oil needs to be hydrodeoxygenated and hydroisomerized again to obtain aviation fuel components.

[0006] However, bio-aviation kerosene produced by existing technologies contains fewer cycloalkanes and aromatics, and has a higher freezing point. Summary of the Invention

[0007] In response to the technical problems in the prior art, the inventors of this invention conducted in-depth research and discovered that by adopting the specific method of this invention, the yield of aviation fuel prepared from biomass raw materials can be significantly improved. At the same time, the resulting aviation fuel oil has high energy density, low freezing point, and excellent product performance.

[0008] To achieve the above objectives, the present invention provides a method for preparing aviation fuel components, characterized by comprising the following steps:

[0009] S1. Reconstruction step, wherein the bio-based oil and the reconstruction catalyst are brought into contact under reconstruction reaction conditions to carry out a reconstruction reaction, thereby obtaining reactive oil and gas and the catalyst to be generated. The reconstruction reaction conditions include: a reaction temperature of 100-350°C, preferably 200-330°C; and a reaction time of 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds.

[0010] S2, separation step, wherein the reaction oil and gas are separated to obtain a first aviation fuel component and heavy oil.

[0011] The present invention further provides a system for preparing aviation fuel components, characterized in that it comprises the following units:

[0012] The remodeling unit is equipped with a bio-based oil inlet and a catalyst inlet, wherein the bio-based oil and the remodeling catalyst are brought into contact under remodeling reaction conditions to carry out a remodeling reaction, and the resulting reaction oil and gas and the catalyst to be generated are obtained.

[0013] A separation unit, connected downstream of the remodeling unit, separates the reacted oil and gas to obtain a first aviation fuel component and heavy oil.

[0014] Furthermore, the present invention also provides an aviation fuel component, wherein, based on the weight of the component, it comprises 30-70% (preferably 40-50%) of alkanes, 20-50% (preferably 29-45%) of total cycloalkanes and 10-25% (preferably 15-25%) of total aromatics, and has a freezing point below -40°C, preferably below -65°C, wherein, based on the weight of the total cycloalkanes, the total cycloalkanes comprise 60-83% (preferably 65-83%) of monocyclic cycloalkanes, 16-35% (preferably 16-30%) of dicyclic cycloalkanes and 1-10% (preferably 2-8%) of tricyclic cycloalkanes.

[0015] In this invention, by reconstructing biomass feedstock oil, its components can be converted into aviation fuel components, achieving a high yield. Simultaneously, the resulting aviation fuel components exhibit high energy density and low freezing point, demonstrating excellent performance when used as aviation fuel components.

[0016] Furthermore, in this invention, the reconstruction reaction and the hydrogenation reaction are coupled, thereby allowing the further extraction of aviation fuel components from the hydrogenation products. The aviation fuel components obtained through hydrogenation treatment exhibit higher energy density and a lower freezing point. Moreover, this further reduces the energy consumption costs in the aviation fuel component production process.

[0017] Furthermore, in this invention, by returning the heavy hydrogenated distillate oil after the hydrogenation reaction to the reconstitution reaction, on the one hand, the utilization rate of bio-based feedstock oil can be further improved, and on the other hand, mild reaction conditions can be provided for the reconstitution reaction of bio-based feedstock oil, thereby further improving the yield of bio-based feedstock oil converted into aviation fuel components.

[0018] In this invention, by introducing oxygen-containing organic compounds into the remodeling reaction, the composition of aviation fuel components can be adjusted, and low-carbon olefins can also be produced. Thus, the product composition can be flexibly adjusted as needed.

[0019] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0020] The accompanying drawings are provided to further illustrate the invention and form part of the specification. They are used together with the following detailed description to explain the invention, but do not constitute a limitation thereof. In the drawings:

[0021] Figure 1 is a schematic flowchart of one embodiment of the method for preparing aviation fuel components provided by the present invention.

[0022] Explanation of reference numerals in the attached drawings: Ⅰ-Pre-reconstruction zone; Ⅱ-Reconstruction zone; 1-Pipeline; 2-Pipeline; 3-Pipeline; 4-Stripping section; 5-Settler; 6-Gas collection chamber; 7-Inclined tube; 8-Regenerator; 9-Pipeline; 10-Pipeline; 11-Pipeline; 12-Pipeline; 13-Separation unit; 14-Pipeline; 15-Pipeline; 16-Pipeline; 17-Pipeline; 18-Pipeline; 19-Hydrogenation unit; 20-Pipeline; 21-Pipeline; 22-Pipeline. Detailed Implementation

[0023] The present invention will be described in detail with reference to specific embodiments. However, it should be noted that the scope of protection of the present invention is not limited to these specific embodiments, but is determined by the claims in the appendix.

[0024] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0025] All publications, patent applications, patents, and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings commonly understood by those skilled in the art. In case of conflict, the definitions in this specification shall prevail.

[0026] When this specification uses the prefixes "known to those skilled in the art," "prior art," or similar terms to derive materials, substances, methods, steps, apparatus, or components, the objects derived from such prefixes cover those commonly used in the art at the time of this application's filing, but also include those that are not currently commonly used but will become generally recognized in the art as suitable for similar purposes.

[0027] In the context of this specification, except where expressly stated, any matters or issues not mentioned herein shall apply directly to those known in the art without any modification. Furthermore, any implementation described herein may be freely combined with one or more other implementations described herein, and any resulting technical solutions or concepts shall be considered part of the original disclosure or original record of this invention, and should not be regarded as new content not disclosed or anticipated herein, unless those skilled in the art consider such combination to be clearly unreasonable.

[0028] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight, unless being based on weight would not be in accordance with the common understanding of those skilled in the art.

[0029] In the context of this invention, unless otherwise specified, the physical properties of substances (such as boiling point) are measured at room temperature (25°C) and normal pressure (101325 Pa).

[0030] [Preparation methods for aviation fuel components]

[0031] This invention provides a method for preparing aviation fuel components, characterized by comprising the following steps:

[0032] S1. Reconstruction step, wherein the bio-based oil and the reconstruction catalyst are brought into contact under reconstruction reaction conditions to carry out a reconstruction reaction, thereby obtaining reactive oil and gas and the catalyst to be generated. The reconstruction reaction conditions include: a reaction temperature of 100-350°C, preferably 200-330°C; and a reaction time of 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds.

[0033] S2, separation step, wherein the reaction oil and gas are separated to obtain a first aviation fuel component and heavy oil.

[0034] In this invention, aviation fuel components are sometimes also referred to as aviation kerosene or jet fuel.

[0035] In one embodiment of the present invention, there is no limitation on the bio-based oil, and examples include vegetable oils, animal oils, microbial oils, waste cooking oils, and oil refinery by-products. In one embodiment of the present invention, the vegetable oils may include soybean oil, rapeseed oil, palm oil, sunflower seed oil, corn oil, peanut oil, cottonseed oil, flaxseed oil, castor oil, coconut oil, olive oil, jatropha oil, tung oil, jatropha oil, rice bran oil, etc. In one embodiment of the present invention, the animal oils may include tallow, lard, mutton fat, chicken fat, fish oil, etc. In one embodiment of the present invention, the microbial oils may include algae oil (microalgae oil), yeast oil, fungal oil, etc. In one embodiment of the present invention, the waste cooking oils may include gutter oil, acidified oil, and waste frying oil, etc. In one embodiment of the present invention, the oil refinery by-products may include acidified oil, etc. In one embodiment of the present invention, the oil refinery by-products refer to by-products generated during the refining of vegetable oils and animal oils. The method of the present invention can convert more bio-based oils into aviation fuel components, improving the high-value-added utilization of biomass raw materials. Furthermore, less coke is produced due to the deoxygenation of fatty acid esters and the generation of a small amount of hydrogen during catalytic conversion.

[0036] In one embodiment of the present invention, the bio-based feedstock oil is selected from fatty acid esters with 14 to 20 carbon atoms, such as, but not limited to, palmitate (C16), stearate (C18), oleate (C18), and linoleate (C18). In another embodiment of the present invention, the content of unsaturated fatty acid esters in the bio-based feedstock oil is 10% to 80% by weight. In the present invention, biomass feedstock with an unsaturated fatty acid ester content of 10% to 80% by weight undergoes catalytic conversion at the acidic sites of a molecular sieve catalyst, which is beneficial for obtaining aviation fuel components with high energy density and low freezing point.

[0037] In one embodiment of the present invention, the bio-based oil can be at least one selected from triglycerides, diglycerides, monoglycerides, fatty acid esters, phospholipids, and fatty acid derivatives. For example, methyl esters, ethyl esters, monoglycerides, and triglycerides of various fatty acids can be listed.

[0038] In one embodiment of the invention, the reconstitution catalyst comprises zeolite, inorganic oxide, and optionally clay, wherein the zeolite comprises mesoporous zeolite and optionally macroporous zeolite. In another embodiment of the invention, the mesoporous zeolite content is 51% to 100% by weight, and the macroporous zeolite content is 0% to 49% by weight, based on the weight of the zeolite.

[0039] In one embodiment of the present invention, the catalyst comprises 1% to 50% by weight of zeolite, 5% to 99% by weight of inorganic oxides, and 0% to 70% by weight of clay, based on the weight of the catalyst.

[0040] In one embodiment of the present invention, the molar ratio of SiO2 to Al2O3 in the mesoporous zeolite is 50 or more, preferably 80 or more, and the molar ratio of SiO2 to Al2O3 does not exceed 300, preferably not more than 280.

[0041] In this invention, bio-based feedstock oil is deoxygenated under the action of a remodeling catalyst and undergoes a remodeling reaction under suitable conditions, thereby reducing the content of straight-chain alkanes in aviation fuel components and increasing the content of cycloalkanes and aromatics.

[0042] In this invention, due to the limitation of the pore structure of the molecular sieve catalyst, the long-chain molecules in the bio-based oil undergo deoxygenation and cracking simultaneously or sequentially on the molecular sieve catalyst, and undergo isomerization, cyclization and addition reactions under the acidic action of the molecular sieve catalyst, promoting the generation of aviation fuel components.

[0043] In one embodiment of the present invention, the reconstruction reaction conditions include: a reaction temperature of 100–350°C, preferably 200–330°C.

[0044] In one embodiment of the present invention, the reconstruction reaction conditions include: a reaction time of 0.01 to 200 seconds, preferably 0.1 to 80 seconds, and more preferably 1 to 20 seconds.

[0045] In one embodiment of the present invention, the reconstruction reaction conditions include: a reaction temperature of 100–300°C, preferably 200–280°C.

[0046] In one embodiment of the present invention, the reaction temperature of the reconstruction reaction is 150°C, 160°C, 170°C, 180°C, 190°C, 200°C, 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C, 300°C, 310°C, 320°C, 330°C, 340°C, or 350°C.

[0047] In one embodiment of the present invention, the reconstruction reaction conditions include: a heavy hourly space velocity of 1–95 h⁻¹. -1 Preferably 5-85h -1 .

[0048] In one embodiment of the present invention, the reconstructive reaction conditions include a catalyst to bio-based oil weight ratio of 3 to 25, preferably 5 to 20.

[0049] In one embodiment of the present invention, in step S1, the reaction stream after the reconstruction reaction is fed into the settling section for separation of the catalyst to be generated and the reaction oil and gas.

[0050] In one embodiment of the present invention, in step S1, the catalyst to be generated is stripped to recover the residual reaction oil and gas. The separated reaction oil and gas is then collected in a gas collection chamber, exited, and subjected to the separation step in step S2.

[0051] In step S2 of the present invention, the reaction oil and gas from the remodeling step are separated to obtain a first aviation fuel component and heavy oil products. In one embodiment of the present invention, the reaction oil and gas from the remodeling step are separated to obtain dry gas, liquefied petroleum gas, naphtha, the first aviation fuel component, and heavy oil products.

[0052] In one embodiment of the present invention, the cutting point between the first aviation fuel component and the heavy oil is any temperature selected between 130 and 300°C, preferably any temperature selected between 150 and 280°C.

[0053] In one embodiment of the present invention, the cutting point between the first aviation fuel component and the heavy oil is 130°C, 140°C, 150°C, 160°C, 170°C, 180°C, 190°C, 200°C, 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C, or 300°C.

[0054] In one embodiment of the present invention, the initial boiling point of the first aviation fuel component is any temperature between 100 and 180°C.

[0055] In one embodiment of the present invention, the initial boiling point of the first aviation fuel component is 100°C, 110°C, 120°C, 130°C, 140°C, 150°C, 160°C, 170°C, or 180°C.

[0056] As described above, through the S1 reconstruction step of the present invention, bio-based feedstock oil can be converted into reactive oil gas containing a first aviation fuel component. Then, through the S2 separation step, the first aviation fuel component of the present invention can be separated from the reactive oil gas. This first aviation fuel component is the aviation fuel component of the present invention, and its freezing point and other physical properties meet the requirements of aviation fuel.

[0057] In one embodiment of the present invention, heavy oil products can also be obtained from the reaction oil and gas, and the heavy oil products can be further processed.

[0058] In one embodiment of the present invention, in order to provide milder reconstitution reaction conditions for bio-based oils, in addition to the specific reconstitution reaction conditions of the present invention, a pre-reconstitution step may also be set before the reconstitution step.

[0059] In one embodiment of the present invention, the method for preparing the aviation fuel component further includes a pre-SO remodeling step, wherein,

[0060] S0, Pre-reconstruction step, wherein fossil feedstock oil is contacted with a reconstruction catalyst under pre-reconstruction conditions to perform a first reconstruction treatment, yielding a first reconstruction reaction stream, and

[0061] S1. In the reconstruction step, the first reconstruction reaction stream and the bio-based oil are subjected to a second reconstruction treatment under reconstruction reaction conditions to obtain reaction oil and gas and the catalyst to be generated.

[0062] That is, in this invention, when a pre-reconstruction step is present, the reconstruction catalyst is fed into the pre-reconstruction step and first undergoes a pre-reconstruction reaction with the fossil feedstock oil (first reconstruction treatment). Then, the reaction stream obtained from the pre-reconstruction reaction is directly fed into the reconstruction step, where bio-feedstock oil is introduced, and a reconstruction reaction is carried out under reconstruction reaction conditions (second reconstruction treatment). At this time, in the reconstruction reaction, the bio-feedstock oil undergoes a reconstruction reaction by contacting the catalyst in the reaction stream obtained from the pre-reconstruction reaction. Simultaneously, the reaction oil and gas in the reaction stream obtained from the pre-reconstruction reaction can further undergo a reconstruction reaction.

[0063] In one embodiment of the present invention, there is no limitation on the fossil feedstock oil, and any oil known in the art that can be used for catalytic conversion, especially heavy feedstock oil, can be used, such as crude oil, atmospheric residue, vacuum residue, vacuum wax oil, heavy oil, oil sands asphalt, catalytic cracking slurry oil, asphalt, wax oil, Fischer-Tropsch synthetic oil and coal liquefaction oil, but is not limited thereto.

[0064] In one embodiment of the present invention, the fossil feedstock oil comprises at least a portion of the following heavy hydrotreated distillate oils, preferably, the fossil feedstock oil is at least a portion of the following heavy hydrotreated distillate oils. In another embodiment of the present invention, the fossil feedstock oil optionally further comprises at least one selected from crude oil, atmospheric residue, vacuum residue, vacuum wax oil, heavy oil, oil sands bitumen, catalytic cracking slurry oil, bitumen, wax oil, Fischer-Tropsch synthetic oil, and coal liquefaction oil.

[0065] In one embodiment of the present invention, the reconstructed catalyst of the present invention is used in the first reconstructed treatment of step S0, and after the first reconstructed stage, the first reconstructed reaction stream containing the catalyst enters the reconstructed step for a second reconstructed treatment. That is, in the present invention, the fresh catalyst / regenerated catalyst first participates in the first reconstructed treatment in the pre-reconstructed step, and the catalyst after the first reconstructed stage then participates in the second reconstructed treatment.

[0066] Therefore, in the preparation method of the present invention, if a reconstruction step is included before step S0, no new catalyst needs to be introduced in the reconstruction step of step S1. Furthermore, in the present invention, the first reconstruction reactant is not subjected to gas-solid separation treatment; it is entirely fed into the reconstruction step of step S1.

[0067] In one embodiment of the present invention, in step S1, an oxygen-containing organic compound is introduced into the reconstitution step; wherein the weight ratio of the introduced oxygen-containing organic compound to the bio-raw material oil is (0.01-0.8):1, preferably (0.02-0.4):1.

[0068] In one embodiment of the present invention, the oxygen-containing organic compound is at least one selected from alcohols, ketones and ethers having 4 or fewer carbon atoms, preferably one or more selected from methanol, ethanol, dimethyl ketone, dimethyl ether and diethyl ether.

[0069] In one embodiment of the present invention, the oxygen-containing organic compound is mixed with the bio-based oil and then introduced into the reconstitution step. Alternatively, the reconstitution step can be introduced separately or in multiple streams.

[0070] In this invention, by introducing oxygen-containing organic compounds into the reconstruction reaction and co-converting them with the bio-based oil, the heat released from the conversion of the oxygen-containing organic compounds is used to supplement the heat of the reconstruction reaction of the bio-based oil, thereby further improving the yield of aviation fuel components obtained from the reconstruction of bio-based oil molecules, and further increasing the content of cycloalkanes and aromatics in the aviation fuel components, which is beneficial to obtaining aviation fuel components with high energy density and low freezing point.

[0071] In one embodiment of the present invention, the heavy oil obtained in step S2 separation step is subjected to hydrogenation treatment.

[0072] Specifically, in one embodiment of the present invention, the preparation method further includes a hydrogenation step S3, wherein heavy oil and hydrogen are brought into contact under a hydrogenation catalyst to carry out a hydrogenation reaction to obtain a hydrogenated product of heavy oil.

[0073] In one embodiment of the present invention, in step S3, the hydrogenation step, the heavy oil and hydrogen are brought into contact under a hydrogenation catalyst to perform hydrogenation saturation treatment, thereby obtaining the hydrogenated product of the heavy oil.

[0074] In one embodiment of the present invention, an aviation fuel component, namely the second aviation fuel component of the present invention, can be further obtained from the hydrogenation product of heavy oil obtained in step S3. This second aviation fuel component can be used alone as the aviation fuel component of the present invention, and its freezing point and other physical properties meet the requirements for aviation fuel.

[0075] Therefore, in one embodiment of the present invention, the preparation method includes an S4 fractionation reflux step, wherein the heavy oil hydrotreating product is fractionated to obtain a second aviation fuel component and a heavy hydrotreating fraction oil, and at least a portion of the heavy hydrotreating fraction oil is recycled back to the pre-reconstruction step of S0 as a fossil feedstock oil.

[0076] In one embodiment of the present invention, a first aviation fuel component and a second aviation fuel component are blended to obtain a blended oil, which is the aviation fuel component of the present invention. This blended oil is also the aviation fuel component of the present invention, and its freezing point and other physical properties meet the requirements for aviation fuel.

[0077] In one embodiment of the present invention, the first aviation fuel component and the second aviation fuel component can be blended in any ratio without specific limitation. For example, the blending ratio of the first aviation fuel component and the second aviation fuel component by weight can be 0.1:99.9 to 99.9:0.1.

[0078] In this invention, the reconstruction reaction of bio-based oil is coupled with a hydrotreating process to prepare aviation fuel components. The resulting aviation fuel components have a high yield and the content of cycloalkane components in the aviation fuel components is more than 20% by weight. The bio-based oil can be further converted into high-energy-density, low-freezing-point aviation fuel components that can be used directly with a high yield. This can greatly simplify the production process of aviation fuel components and reduce the energy consumption cost in the production process.

[0079] In one embodiment of the present invention, in the S4 fractionation reflux step, at least a portion of the heavy hydrotreated distillate is recycled back to the S1 reconstitution step.

[0080] In one embodiment of the present invention, the cut-off point between the second aviation fuel component and the heavy hydrotreated distillate is any temperature selected between 250 and 300°C.

[0081] In one embodiment of the present invention, the cut-off point between the second aviation fuel component and the heavy hydrotreated distillate is 250°C, 260°C, 270°C, 280°C, 290°C, or 300°C.

[0082] In one embodiment of the present invention, the initial boiling point of the second aviation fuel component is any temperature between 100 and 180°C.

[0083] In one embodiment of the present invention, the initial boiling point of the second aviation fuel component is 100°C, 110°C, 120°C, 130°C, 140°C, 150°C, 160°C, 170°C, or 180°C.

[0084] In one embodiment of the present invention, the reaction conditions of the pre-reconstruction step in step S0 include: a reaction temperature of 330-500°C, preferably 330-450°C.

[0085] In one embodiment of the present invention, in the pre-reconstruction step of step S0, the reaction temperature of the pre-reconstruction step is 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C, 400°C, 410°C, 420°C, 430°C, 440°C, 450°C, 460°C, 470°C, 480°C, 490°C, or 500°C.

[0086] In one embodiment of the present invention, in the pre-reconfiguration step of step S0, the heavy hourly space velocity is 1-95 h. -1 Preferably 10-70h -1 .

[0087] In one embodiment of the present invention, in the pre-reconstruction step of step S0, the reaction time is 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds.

[0088] In one embodiment of the present invention, in the pre-reconstruction step of step S0, the weight ratio of the catalyst to the fossil feedstock oil is 3-25, preferably 5-20.

[0089] In one embodiment of the present invention, the reaction conditions in the reconstruction step of step S1 include: a reaction temperature of 200-330°C, preferably 280-330°C.

[0090] In one embodiment of the present invention, in the reconstruction step of step S1, the reaction temperature of the reconstruction reaction is 200℃, 210℃, 220℃, 230℃, 240℃, 250℃, 260℃, 270℃, 280℃, 290℃, 300℃, 310℃, 320℃ or 330℃.

[0091] In one embodiment of the present invention, the reaction conditions for the reconstruction step in step S1 include: a heavy hourly space velocity of 1-95 h⁻¹. -1 Preferably 10-70h -1 .

[0092] In one embodiment of the present invention, in the reconstruction step of step S1, the reaction conditions of the reconstruction step include: the reaction time is 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds.

[0093] In one embodiment of the present invention, when there is a pre-S0 remodeling step, the weight ratio of the catalyst used in the pre-S0 remodeling step to the bio-based oil used in the remodeling step is 3 to 25, preferably 5 to 20.

[0094] In one embodiment of the present invention, when there is a pre-reconstruction step S0, the weight ratio of the bio-raw material oil used in the reconstruction step S1 to the first reconstruction reaction stream is (1-90):1, preferably (3-80):1.

[0095] In this invention, the hydrogenation step S3 can be performed under conventional hydrogenation conditions in the art.

[0096] In one embodiment of the present invention, the conditions for the hydrogenation reaction include: a reaction pressure of 2.5–25.0 MPa, preferably 3.5–18.5 MPa; a reaction temperature of 120–400°C, preferably 150–390°C; and a hydrogen-to-oil volume ratio of 220–2600 Nm³. 3 / m 3 Preferably, it is 310–2100 Nm 3 / m 3 The volumetric hourly space velocity (VHSV) is 0.05–20.0 h⁻¹. -1 Preferably, the time is 0.15 to 10.5 h. -1 .

[0097] In one embodiment of the present invention, the hydrogenation catalyst comprises a support and an active component supported on the support, wherein the metal element in the active component comprises at least one Group VIII metal, at least one Group VIB metal, and optional additives.

[0098] In one embodiment of the present invention, the hydrogenation catalyst comprises, based on the weight of the hydrogenation catalyst, 1 to 38 wt% of a Group VIII metal, 1 to 51 wt% of a Group VIB metal, and 0 to 11 wt% of additives.

[0099] In one embodiment of the present invention, the Group VIII metal of the hydrogenation catalyst may include nickel (Ni), cobalt (Co), and iron (Fe).

[0100] In one embodiment of the present invention, the Group VIB metal of the hydrogenation catalyst may include molybdenum (Mo) and tungsten (W).

[0101] In one embodiment of the present invention, the additives of the hydrogenation catalyst are selected from one or more of fluorine, phosphorus, magnesium, titanium and platinum.

[0102] In one embodiment of the present invention, the support for the hydrogenation catalyst is selected from at least one of alumina, amorphous silica-alumina, and zeolite.

[0103] The preparation method of the present invention may further include a regeneration step in step S6, wherein the catalyst to be generated is regenerated by coking to obtain a regenerated catalyst, and the regenerated catalyst is returned to the reconstruction step for recycling; or, if a pre-reconstruction step is performed, the catalyst is returned to the pre-reconstruction step for recycling.

[0104] There are no restrictions on the conditions for coking and regenerating the spent catalyst; the coking temperature and coking atmosphere can be those commonly used in the field for catalyst regeneration.

[0105] In one embodiment of the present invention, when the pre-reconstruction step is not performed, the regenerated catalyst is cooled to 300-500°C, preferably to 350-450°C, through a heat exchange step and then returned to the reconstruction step for recycling.

[0106] In one embodiment of the present invention, during the pre-reconstruction step, the regenerated catalyst is cooled to 300-500°C via a heat exchange step, preferably to 350-450°C, and then returned to the pre-reconstruction step for recycling.

[0107] In this invention, the regenerated catalyst is cooled to 300–500°C, preferably 350–450°C, via a heat exchange step. This allows for a greater conversion of heavy hydrotreated distillate oil or bio-based feedstock oil into aviation fuel components, preventing excessively high temperatures from causing further over-cracking of the aviation fuel components and reducing the yield. The heat exchange step utilizes a heat exchanger, which can be a heat extractor selected from industrially mature heat extractors (such as dense-phase external heat extractors). The high-temperature regenerated catalyst exchanges heat with the water-vapor mixture in the external heat extractor to generate saturated steam, removing excess heat from the regenerated catalyst. The temperature of the regenerated catalyst is controlled within the range of 300–500°C and 350–450°C, and the removed waste heat can be utilized subsequently.

[0108] In one embodiment of the present invention, the regeneration step is carried out in the presence of oxygen-containing gas.

[0109] In one embodiment of the present invention, the conditions for the regeneration step include: the temperature of the coke regeneration is 400-750°C, preferably 500-600°C; the bed pressure is 0.1-0.45 MPa, preferably 0.12-0.40 MPa; and the residence time of oxygen-containing gas is 0.1-300 seconds, preferably 1-240 seconds.

[0110] In one embodiment of the present invention, a method for preparing aviation fuel components is provided, comprising the following steps:

[0111] S0, Pre-reconstruction step, wherein the heavy hydrotreated distillate from the fractionation reflux step S4 below is contacted with a reconstruction catalyst under pre-reconstruction conditions to perform a first reconstruction treatment and obtain a first reconstruction reaction stream.

[0112] S1, Reconstruction Step, wherein the first reconstruction reaction stream, bio-feed oil, optional oxygenated organic compounds, and optional heavy hydrotreated distillate from the fractionation reflux step in S4 below are subjected to a second reconstruction treatment under reconstruction reaction conditions to obtain reaction oil gas and catalyst to be generated; the reconstruction reaction conditions include: a reaction temperature of 200-330℃, preferably 280-330℃; and a reaction time of 0.01-200 seconds, preferably 0.1-80 seconds, more preferably 1-20 seconds;

[0113] S2, separation step, wherein the reaction oil and gas are separated to obtain dry gas, liquefied gas, naphtha, first aviation fuel component and heavy oil products;

[0114] S3, Hydrogenation step, wherein the heavy oil and hydrogen are brought into contact under a hydrogenation catalyst to carry out a hydrogenation reaction, thereby obtaining the hydrogenated product of the heavy oil.

[0115] S4, a fractionation and reflux step, wherein the heavy oil hydrotreating product is fractionated to obtain a second aviation fuel component and a heavy hydrotreating distillate; at least a portion of the heavy hydrotreating distillate is recycled back as fossil feedstock to the pre-reconstruction step of S0; and optionally, at least a portion of the heavy hydrotreating distillate is recycled back to the reconstruction step of S1; and

[0116] S5. Blending step: Blend the first aviation fuel component and the second aviation fuel component to obtain an aviation fuel component.

[0117] [System for preparing aviation fuel components]

[0118] The present invention also provides a system for preparing aviation fuel components, characterized in that it comprises the following units:

[0119] The remodeling unit is equipped with a bio-based oil inlet and a catalyst inlet, wherein the bio-based oil and the remodeling catalyst are brought into contact under remodeling reaction conditions to carry out a remodeling reaction, and the resulting reaction oil and gas and the catalyst to be generated are obtained.

[0120] A separation unit, connected downstream of the remodeling unit, separates the reacted oil and gas to obtain a first aviation fuel component and heavy oil.

[0121] In one embodiment of the present invention, a pre-reconstruction region is provided in the upstream portion of the reconstruction unit, and a reconstruction region is provided in the downstream portion of the reconstruction unit, wherein...

[0122] The pre-reconstruction zone includes a fossil feedstock inlet and a catalyst inlet. The fossil feedstock is brought into contact with the reconstruction catalyst under pre-reconstruction conditions to undergo the first reconstruction treatment, yielding the first reconstruction reaction stream.

[0123] The reconstruction zone is connected to the pre-reconstruction zone. The reconstruction zone is provided with a bio-based oil inlet. The first reconstruction reaction stream and the bio-based oil from the pre-reconstruction zone are brought into contact under reconstruction reaction conditions to undergo a second reconstruction process, resulting in reaction oil and gas and a catalyst to be generated.

[0124] In the system for preparing aviation fuel components of the present invention, the fossil feedstock inlet can be fed with heavy hydrotreated distillate oil from the fractionation reflux unit.

[0125] In one embodiment of the present invention, the system for preparing aviation fuel components further includes a hydrogenation unit connected downstream of a separation unit, wherein heavy oil from the separation unit is contacted with hydrogen in the presence of a hydrogenation catalyst to undergo a hydrogenation reaction, yielding a hydrogenated product of the heavy oil; and

[0126] A fractionation reflux unit, connected downstream of the hydrotreating unit, fractionates the hydrotreating products of heavy oil from the hydrotreating unit to obtain a second aviation fuel component and heavy hydrotreating distillate. The fractionation reflux unit is also connected upstream of the pre-reconstruction zone, allowing at least a portion of the heavy hydrotreating distillate to be recycled back to the pre-reconstruction zone as fossil feedstock for a first reconstruction process. Optionally, the fractionation reflux unit is connected upstream of the reconstruction zone, recycling at least a portion of the heavy hydrotreating distillate back to the reconstruction zone for a second reconstruction process.

[0127] A blending unit, wherein the first aviation fuel component and the second aviation fuel component are blended to obtain an aviation fuel component.

[0128] In one embodiment of the present invention, the reconstructing zone is further provided with an oxygen-containing organic compound inlet, so that the oxygen-containing organic compound enters the reconstructing zone to participate in the second reconstructing process.

[0129] In one embodiment of the present invention, the reconstructing zone is further provided with a heavy hydrogenated distillate oil inlet, so that at least a portion of the heavy hydrogenated distillate oil from the fractionation reflux unit is recycled back to the reconstructing zone for a second reconstructing process.

[0130] In one embodiment of the present invention, the system for preparing aviation fuel components further includes a catalyst regeneration unit connected downstream of a separation unit, which regenerates the spent catalyst from the separation unit by coking to obtain a regenerated catalyst, and is connected upstream of a reconstruction unit to feed the regenerated catalyst into the reconstruction unit for recycling; or, if a pre-reconstruction zone exists, it is connected upstream of the pre-reconstruction zone to feed the regenerated catalyst into the pre-reconstruction zone for recycling.

[0131] In one embodiment of the present invention, a heat exchange unit is provided between the catalyst regeneration unit and the reconstruction unit, so that the regenerated catalyst is cooled to 300-500°C, preferably to 350-450°C, via the heat exchange unit.

[0132] In one embodiment of the present invention, the catalyst regeneration unit and the pre-reconstruction zone of the reconstruction unit are connected, and a heat exchange unit is provided between the catalyst regeneration unit and the pre-reconstruction zone, so that the regenerated catalyst is cooled to 300-500°C, preferably to 350-450°C, via the heat exchanger.

[0133] In one embodiment of the present invention, the catalyst regeneration unit and the reconstruction zone of the reconstruction unit are connected, and a heat exchange unit is provided between the catalyst regeneration unit and the reconstruction zone, so that the regenerated catalyst is cooled to 300-500°C, preferably to 350-450°C, through the heat exchange unit.

[0134] In one embodiment of the present invention, the pre-reconstruction zone and the reconstruction zone each independently use a reconstruction reactor, wherein the reconstruction reactor is selected from one or more combinations of fluidized bed, fixed bed, moving bed and slurry bed; preferably, the fluidized bed reactor is selected from one or more combinations of riser, constant velocity fluidized bed, constant diameter fluidized bed, upward conveyor line and downward conveyor line, or two or more combinations of the same reactor, the combination including series and / or parallel connection; wherein the riser is selected from constant diameter riser or variable diameter riser.

[0135] In one embodiment of the present invention, the pre-reconstruction zone and the reconstruction zone each use a reconstruction reactor, wherein the reconstruction reactor is a variable diameter riser reactor; or, the reconstruction reactor comprises a riser and a fluidized bed from bottom to top.

[0136] In one embodiment of the present invention, the pre-reconstruction zone and the reconstruction zone use the same reconstruction reactor, which are located in the upstream and downstream zones of the reconstruction reactor, respectively.

[0137] In one embodiment of the present invention, the reconstructed reactor can be a variable-diameter riser reactor. For example, the variable-diameter riser includes, from bottom to top along the axial direction, a first riser section, an expanding section, a dense-phase fluidizing section, a narrowing section, and a second riser section; wherein, the diameter of the expanding section continuously increases from bottom to top along the axial direction, and the angle between the sidewall of the expanding section and the axis can be 5° to 60°; the ratio of the diameter to the height of the dense-phase fluidizing section can be (1 to 20):1; the diameter of the narrowing section continuously decreases from bottom to top along the axial direction, and the angle between the sidewall of the narrowing section and the axis can be 5° to 60°. A material distributor is also provided at the head of the dense-phase fluidizing section. Furthermore, the radial cross-section of the variable-diameter riser reactor is approximately circular.

[0138] The system for preparing aviation fuel components of the present invention can implement the method for preparing aviation fuel components of the present invention. Therefore, in the present invention, each unit / part of the system corresponds to each step of the preparation method.

[0139] In one embodiment of the present invention, a system for preparing aviation fuel components is provided, comprising the following units:

[0140] The reconstructing unit includes a pre-reconstruction zone upstream and a reconstructing zone downstream. The pre-reconstruction zone has a fossil feedstock oil inlet and a catalyst inlet, wherein the fossil feedstock oil is contacted with the reconstructing catalyst under pre-reconstruction conditions for a first reconstruction treatment, yielding a first reconstructed reaction stream. The reconstructing zone is connected to the pre-reconstruction zone and has a bio-feedstock oil inlet, an optional oxygen-containing organic compound inlet, and an optional heavy hydrogenated distillate oil inlet, wherein the first reconstructed reaction stream from the pre-reconstruction zone, the bio-feedstock oil, the optional oxygen-containing organic compound, and the optional heavy hydrogenated distillate oil are contacted under reconstruction reaction conditions for a second reconstruction treatment, yielding a reaction oil-gas and a catalyst to be generated.

[0141] A separation unit, connected downstream of the reconstruction unit, separates the reaction oil and gas to obtain dry gas, liquefied gas, naphtha, first aviation fuel component and heavy oil products.

[0142] The hydrogenation unit is connected downstream of the separation unit, which allows the heavy oil from the separation unit to come into contact with hydrogen in the presence of a hydrogenation catalyst to carry out a hydrogenation reaction and obtain the hydrogenated product of the heavy oil.

[0143] A fractionation reflux unit, connected downstream of the hydrotreating unit, fractionates the hydrotreating products of heavy oil from the hydrotreating unit to obtain a second aviation fuel component and heavy hydrotreating distillate. The fractionation reflux unit is also connected upstream of the pre-reconstruction zone, allowing at least a portion of the heavy hydrotreating distillate to be recycled back to the pre-reconstruction zone as fossil feedstock for a first reconstruction process. Optionally, the fractionation reflux unit is connected upstream of the reconstruction zone, recycling at least a portion of the heavy hydrotreating distillate back to the reconstruction zone for a second reconstruction process.

[0144] A blending unit, wherein the first aviation fuel component and the second aviation fuel component are blended to obtain an aviation fuel component.

[0145] [Aerospace fuel composition]

[0146] This invention provides an aviation fuel component, wherein, based on the weight of the component, it comprises 30-70% (preferably 40-50%) of alkanes, 20-50% (preferably 29-45%) of total cycloalkanes, and 10-25% (preferably 15-25%) of total aromatics, and has a freezing point below -40°C, preferably below -65°C. The total cycloalkanes, based on the weight of the total cycloalkanes, comprise 60-83% (preferably 65-83%) of monocyclic cycloalkanes, 16-35% (preferably 16-30%) of dicyclic cycloalkanes, and 1-10% (preferably 2-8%) of tricyclic cycloalkanes.

[0147] In one embodiment of the present invention, the aviation fuel component of the present invention comprises the aviation fuel component of the present invention.

[0148] In one embodiment of the present invention, the final boiling point of the aviation fuel component of the present invention is 250-300°C.

[0149] In the aviation fuel composition of the present invention, the sum of the respective weight percentages of alkanes, total cycloalkanes and total aromatics is taken as 100% by weight.

[0150] In this invention, the monocyclic aromatic hydrocarbons include alkylbenzenes, indenes, and tetrahydronaphthalenes.

[0151] In one embodiment of the present invention, the aviation fuel component of the present invention comprises, based on the weight of the total aromatics, 30-63.5% (preferably 40-63%) of alkylbenzenes, 34.5-70% (preferably 37-60%) of indenes and / or tetrahydronaphthalenes.

[0152] In one embodiment of the present invention, the aviation fuel component of the present invention comprises, based on the weight of the total aromatics, 30-63.5% (preferably 40-63%) of alkylbenzenes, 34.5-60% (preferably 35-55%) of indenes and / or tetrahydronaphthalenes.

[0153] In this invention, indene includes indene and other indene compounds.

[0154] In one embodiment of the present invention, the aviation fuel component of the present invention contains 10-25% total monocyclic aromatic hydrocarbons and less than 1% total bicyclic aromatic hydrocarbons, based on the weight of the component.

[0155] The aviation fuel component obtained by this invention has an aromatic hydrocarbon content of less than 25% by weight, preferably less than 22% by weight, and a cycloalkanes content of more than 20% by weight, preferably more than 29% by weight, and more preferably more than 30% by weight. The aviation fuel component has a freezing point of less than or equal to -45°C, preferably less than -65°C. The aviation fuel component provided by this invention contains a relatively high amount of cycloalkanes, which have a higher calorific value per unit volume than straight-chain alkanes, thus improving the low-temperature fluidity of the aviation fuel component. At the same time, the aviation fuel component contains aromatics with high volumetric energy density, further improving the energy density of the aviation fuel component.

[0156] The following describes a specific embodiment of the present invention with reference to the flowchart shown in Figure 1. As shown in Figure 1, the regenerated catalyst from the regenerator 8 is introduced into the bottom (region I) of the fluidized bed reactor via pipeline 11. The catalyst moves upward along the fluidized bed reactor under the influence of pre-lift steam from pipeline 1. Simultaneously, the heavy hydrogenation fraction is introduced into the bottom of the fluidized bed reactor via pipeline 22. The two reactants come into contact in region I of the fluidized bed reactor for a first reconstruction treatment, resulting in a first reconstructed reaction stream that continues to move upward along the fluidized bed reactor under the influence of pre-lift steam. At the same time, the preheated bio-feed oil comes into contact with the first reconstructed reaction stream via pipeline 2 in region II of the fluidized bed reactor for a second reconstruction treatment, resulting in a reaction stream. The reaction stream enters the cyclone separator in the settling tank 5 for gas-solid separation, yielding the catalyst to be regenerated and the reaction oil gas. The reaction oil gas enters the gas collection chamber 6, while the catalyst fine powder returns to the settling tank 5 via the feed leg. The spent catalyst in settling tank 5 flows to stripping section 4, where it comes into contact with stripping steam from pipeline 3 for stripping. The stripped oil and gas from the spent catalyst enters collecting chamber 6 via cyclone separator. The stripped spent catalyst enters regenerator 8 via inclined tube 7, where, under the condition of main air supplied via pipeline 9, the coke on the spent catalyst is burned off, regenerating the deactivated spent catalyst. The flue gas enters the flue gas fan via pipeline 10, and the regenerated catalyst obtained from the regeneration is returned to the bottom of fluidized bed reactor 2 via pipeline 11 for recycling.

[0157] The reaction oil and gas enter the subsequent product separation unit 13 via pipeline 12. The separated dry gas is led out via pipeline 14, the liquefied gas via pipeline 15, the naphtha via pipeline 16, the first aviation fuel component via pipeline 17, and the heavy oil with a boiling point higher than the cut point enters the hydrogenation unit 19 via pipeline 18 to contact the hydrogenation catalyst and hydrogen introduced via pipeline 20 for hydrogenation reaction. The hydrogenated saturated product is separated, and the obtained second aviation fuel component is led out via pipeline 21. The hydrogenated heavy hydrogenated distillate oil continues to circulate to the bottom (region I) of the fluidized bed reactor via pipeline 22 for the first remodeling treatment.

[0158] In one embodiment of the present invention, the following solution is provided:

[0159] Option 1. A method for preparing bio-aviation kerosene components, characterized in that the method includes the following steps:

[0160] The bio-based feedstock oil is brought into contact with a molecular sieve catalyst in a molecular reconstruction reactor to carry out a molecular reconstruction catalytic reaction, yielding a reaction oil gas and a catalyst to be generated; the reaction oil gas is then separated to obtain dry gas, liquefied gas, naphtha, a first bio-aviation kerosene component, and heavy oil products;

[0161] The heavy oil and hydrogen are brought into contact with a hydrogenation catalyst in a hydrogenation unit and subjected to a hydrogenation reaction under hydrogenation reaction conditions to saturate the heavy oil with hydrogen, thereby obtaining a hydrogenated heavy oil product.

[0162] The hydrogenated product of the heavy oil is fractionated to obtain a second bio-aviation kerosene component and a heavy hydrogenated distillate. The heavy hydrogenated distillate is then recycled back to the reconstruction catalytic reactor for molecular reconstruction catalytic reaction.

[0163] Wherein, the cut-off point between the first bio-aviation kerosene component and the heavy oil product is any temperature between 200 and 300°C; the cut-off point between the second bio-aviation kerosene component and the heavy hydrotreated distillate is any temperature between 250 and 300°C.

[0164] Option 2. According to the method in Option 1, wherein the bio-based oil is derived from one or more of vegetable oils, animal oils, microbial oils, waste cooking oils, and oil refinery by-products;

[0165] Preferably, the bio-based oil is selected from fatty acid esters with 16 to 18 carbon atoms;

[0166] Preferably, the content of unsaturated fatty acid esters in the bio-based raw material oil is 10-80% by weight;

[0167] Scheme 3. The method according to Scheme 1, wherein the conditions for the molecular reconstruction catalytic reaction include: a reaction temperature of 100–450°C, preferably 200–400°C; and a weight hourly space velocity of 1–95 h⁻¹. -1 Preferably 5-85h -1 The weight ratio of the molecular sieve catalyst to the bio-based oil is 3–25, preferably 5–20; the reaction time is 0.01–200 seconds, preferably 0.1–80 seconds.

[0168] Option 4. The method according to Option 1, wherein the molecular sieve catalyst comprises zeolite, inorganic oxide and optionally clay;

[0169] Based on the weight of the molecular sieve catalyst, the molecular sieve catalyst comprises 1-50% by weight of zeolite, 5-99% by weight of inorganic oxides and 0-70% by weight of clay.

[0170] The zeolite includes mesoporous zeolite and optional macroporous zeolite; based on the weight of the zeolite, the content of mesoporous zeolite is 51-100% by weight, and the content of macroporous zeolite is 0-49% by weight; the molar ratio of SiO2 to Al2O3 in the mesoporous zeolite is greater than or equal to 50, preferably greater than or equal to 80.

[0171] The mesoporous zeolite is selected from at least one of ZSM series zeolites, ZRP zeolite and mordenite;

[0172] The macroporous zeolite is selected from at least one of rare earth Y-type zeolite, rare earth HY-type zeolite, ultra-stable Y-type zeolite, high-silica Y-type zeolite and β-type zeolite;

[0173] Option 5. According to the method described in Option 1, wherein the initial boiling point of the first bio-aviation kerosene component and the second bio-aviation kerosene component are any temperature between 100 and 180°C, and the final boiling point is any temperature between 250 and 300°C.

[0174] Scheme 6. The method according to Scheme 1, wherein the method further includes: introducing an oxygen-containing organic compound into the molecular reconstruction reactor for co-conversion with the bio-based oil; the weight ratio of the oxygen-containing organic compound introduced into the molecular reconstruction reactor to the bio-based oil per unit time is (0.02~0.2):1;

[0175] The oxygen-containing organic compound is selected from at least one of alcohols and ethers with 4 or fewer carbon atoms, preferably one or more of methanol, ethanol, dimethyl ketone, dimethyl ether and diethyl ether;

[0176] Option 7. The method according to Option 1, wherein the molecular reconstruction reactor is selected from one or a combination of several of fluidized bed, fixed bed, moving bed and slurry bed;

[0177] The fluidized bed reactor is selected from one or more of the following: riser, constant velocity fluidized bed, constant diameter fluidized bed, upward conveyor line, and downward conveyor line, or two or more of the same type of reactor, wherein the combination includes series and / or parallel connection; wherein the riser is selected from a constant diameter riser or a variable diameter fluidized bed;

[0178] Option 8. The method according to Option 7, wherein the molecular reconstruction reactor is a variable diameter fluidized bed reactor;

[0179] Alternatively, the molecular reconstruction reactor may include a riser and a fluidized bed from bottom to top.

[0180] Option 9. The method according to Option 1, wherein the conditions for the hydrogenation reaction include: a reaction pressure of 2.5–25.0 MPa, preferably 3.5–18.5 MPa; a reaction temperature of 120–400°C, preferably 150–390°C; and a hydrogen-to-oil volume ratio of 220–2600 Nm³. 3 / m 3 Preferably, it is 310–2100 Nm 3 / m 3 The liquid hourly space velocity (LHSV) is 0.05–20.0 h⁻¹. -1 Preferably, the time is 0.15 to 10.5 h. -1 ;

[0181] Preferably, the hydrogenation catalyst comprises a support and an active component supported on the support, wherein the metal element in the active component comprises at least one Group VIII metal, at least one Group VIB metal, and optional additives;

[0182] Preferably, based on the weight of the hydrogenation catalyst, the hydrogenation catalyst comprises 1 to 38 wt% of a Group VIII metal, 1 to 51 wt% of a Group VIB metal, and 0 to 11 wt% of additives.

[0183] Preferably, the additive is selected from one or more of fluorine, phosphorus, magnesium, titanium and platinum;

[0184] Preferably, the carrier is selected from at least one of alumina, amorphous silica-alumina, and zeolite;

[0185] Scheme 10. The method according to Scheme 1, wherein the method further includes: stripping and coking the spent catalyst to obtain a regenerated catalyst, and returning the regenerated catalyst to the fluidized bed reactor for recycling, preferably cooling the regenerated catalyst to 200-400°C via a heat exchanger before returning it to the fluidized bed reactor for recycling;

[0186] The coke regeneration is carried out in the presence of oxygen-containing gas; the temperature of the coke regeneration is 400-750℃, preferably 500-600℃; the bed pressure is 0.1-0.45MPa, preferably 0.12-0.40MPa; and the residence time of the oxygen-containing gas is 0.1-300 seconds, preferably 1-240 seconds.

[0187] Example

[0188] The present invention will be further illustrated by the following examples, but these examples are not intended to limit the invention. All raw materials used in the examples are commercially available.

[0189] The properties of the bio-based oils in the following examples and comparative examples are listed in Table 1.

[0190] The molecular sieve catalyst used in the following examples and comparative examples is designated TCC-1, containing 30% by weight of mesoporous zeolite ZSM-5, with the balance being an alumina support. The molar ratio of SiO2 to Al2O3 in the ZSM-5 zeolite is 170, and it was produced by Sinopec Qilu Branch. The properties of the molecular sieve catalyst are listed in Table 2.

[0191] In the examples and comparative examples, hydrogenation catalyst A was supported on alumina and, based on the weight of the hydrogenation catalyst, comprised 2.6 wt% NiO, 29 wt% MoO3, and 5 wt% platinum additive. The properties of hydrogenation catalyst A are listed in Table 3.

[0192] The net calorific value of aviation fuel components is determined according to GB / T 384-2025 "Determination of Calorific Value of Hydrocarbon Fuels - Oxygen Bomb Calorimeter Method".

[0193] Table 1 Properties of Biomass Raw Materials

[0194] Table 2 Properties of Molecular Sieves Catalysts

[0195] Table 3 Properties of hydrogenation catalysts

[0196] Example 1

[0197] Example 1 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0198] Heavy hydrotreated distillate is introduced to the bottom of the variable-diameter riser reactor. The regenerated catalyst, after heat exchange via a heat exchanger on pipeline 11, is introduced to the bottom of the reactor and undergoes a first remodeling treatment (pre-remodeling step) in region I of the reactor, yielding a first remodeled reaction stream. This first remodeled reaction stream is introduced to region II of the subsequently connected riser reactor. Simultaneously, preheated bio-feedback oil (properties shown in Table 1) is introduced to region II of the same riser reactor. The bio-feedback oil and the first remodeled reaction stream undergo a second remodeling treatment (remodeling step) in region II of the riser reactor. The resulting reaction stream, containing reacted oil and gas and the regenerated catalyst, is separated in a settling tank. The regenerated catalyst is stripped in stripping section 4 and then enters regenerator 8 via pipeline 7.

[0199] The resulting reaction oil and gas are separated according to their boiling range in a separation unit. The dry gas obtained from the separation is led out through pipeline 14, the liquefied gas through pipeline 15, the naphtha through pipeline 16, the first aviation fuel component through pipeline 17, and the heavy oil product with a boiling point higher than the cut point through pipeline 18. The first aviation fuel component and the heavy oil product are obtained; the cut point for the first aviation fuel component and the heavy oil product is 230℃; the boiling range of the first aviation fuel component is 150–230℃.

[0200] Heavy oil is introduced into a medium-sized hydrotreating unit and contacted with a hydrotreating catalyst and hydrogen for hydrosaturation treatment to obtain the hydrogenated product of heavy oil. The hydrosaturation conditions include: a reaction pressure of 5 MPa, a reaction temperature of 280℃, and a hydrogen-to-oil volume ratio of 1000 Nm³. 3 / m 3 .

[0201] The hydrogenation products of heavy oil are fractionated to obtain a second aviation fuel component and a heavy hydrogenated distillate; the cut point of the second aviation fuel component and the heavy hydrogenated distillate is 300℃; the distillation range of the second aviation fuel component is 150~300℃.

[0202] The heavy hydrotreated distillate is recycled back to the bottom of the variable-diameter riser reactor for the first remodeling treatment; the spent catalyst is introduced into the regenerator 8 via pipeline 7 for coke burn regeneration, and the regenerated catalyst is returned to the bottom of the variable-diameter riser reactor via pipeline 11 for recycling. The regeneration conditions for the spent catalyst include: oxygen-containing gas is air; regeneration temperature is 580℃; bed pressure is 0.3MPa; and oxygen-containing gas residence time is 180 seconds.

[0203] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0204] Example 2

[0205] Example 2 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0206] Each operation is the same as in Example 1, and the processing conditions are shown in Table 4.

[0207] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0208] Example 3

[0209] Example 3 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0210] The operations are the same as in Example 1. In addition, methanol is introduced into region II of the riser reactor, so that the bio-feed oil, methanol and the first reconstitution reaction stream come into contact in region II of the riser reactor to carry out the second reconstitution treatment (reconstitution step).

[0211] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0212] Example 4

[0213] Example 4 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0214] Each operation is the same as in Example 1, and the processing conditions are shown in Table 4.

[0215] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0216] Example 5

[0217] Example 5 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0218] Each operation is the same as in Example 1, and the processing conditions are shown in Table 4.

[0219] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0220] Example 6

[0221] Example 6 was conducted on the experimental setup shown in the flowchart of Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor. Specifically, regions I and II of the riser reactor were combined. That is, in this example, the pre-remodeling step was not performed.

[0222] Bio-based feedstock oil and heavy hydrotreated distillate oil are mixed at a weight ratio of 5:1 and introduced into the bottom of a variable-diameter riser reactor. Methanol is introduced simultaneously. The regenerated catalyst is introduced into the bottom of the reactor via pipeline 11. In the reaction zone of the riser reactor, a remodeling reaction (remodeling step) takes place. The resulting reaction stream containing reacted oil and gas and the spent catalyst is separated in a settling tank. The spent catalyst is stripped in stripping section 4 and then enters regenerator 8 via pipeline 7.

[0223] The resulting reaction oil and gas are separated according to their boiling range in a separation unit. The dry gas obtained from the separation is led out through pipeline 14, the liquefied gas through pipeline 15, the naphtha through pipeline 16, the first aviation fuel component through pipeline 17, and the heavy oil product with a boiling point higher than the cut point through pipeline 18. The first aviation fuel component and the heavy oil product are obtained; the cut point for the first aviation fuel component and the heavy oil product is 230℃; the boiling range of the first aviation fuel component is 150–230℃.

[0224] Heavy oil is introduced into a medium-sized hydrotreating unit and contacted with a hydrotreating catalyst and hydrogen for hydrosaturation treatment to obtain the hydrogenated product of heavy oil. The hydrosaturation conditions include: a reaction pressure of 5 MPa, a reaction temperature of 280℃, and a hydrogen-to-oil volume ratio of 1000 Nm³. 3 / m 3 .

[0225] The hydrogenation products of heavy oil are fractionated to obtain a second aviation fuel component and a heavy hydrogenated distillate; the cut point of the second aviation fuel component and the heavy hydrogenated distillate is 300℃; the distillation range of the second aviation fuel component is 150~300℃.

[0226] The heavy hydrotreated distillate is recycled back to the bottom of the variable-diameter riser reactor in the required proportion for remodeling reaction; the spent catalyst is introduced into the regenerator 8 via pipeline 7 for coke burn regeneration, and the regenerated catalyst is returned to the bottom of the variable-diameter riser reactor via pipeline 11 for recycling. The regeneration conditions for the spent catalyst include: oxygen-containing gas is air; regeneration temperature is 580℃; bed pressure is 0.3MPa; and oxygen-containing gas residence time is 180 seconds.

[0227] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0228] Example 7

[0229] Example 7 was conducted on the experimental setup shown in the flowchart of Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor. Specifically, regions I and II of the riser reactor were combined. That is, in this example, the pre-remodeling step was not performed.

[0230] Bio-based feedstock oil and methanol are introduced together into the bottom of the variable-diameter riser reactor. The regenerated catalyst is introduced into the bottom of the reactor via pipeline 11. In the reaction zone of the riser reactor, a remodeling reaction (remodeling step) takes place. The resulting reaction stream containing reacted oil and gas and the regenerated catalyst is separated in a settling tank. The regenerated catalyst is stripped in stripping section 4 and then enters regenerator 8 via pipeline 7.

[0231] The resulting reaction oil and gas are separated according to their boiling range in a separation unit. The dry gas obtained from the separation is led out through pipeline 14, the liquefied gas through pipeline 15, the naphtha through pipeline 16, the first aviation fuel component through pipeline 17, and the heavy oil product with a boiling point higher than the cut point through pipeline 18. The first aviation fuel component and the heavy oil product are obtained; the cut point for the first aviation fuel component and the heavy oil product is 230℃; the boiling range of the first aviation fuel component is 150–230℃.

[0232] Heavy oil is introduced into a medium-sized hydrotreating unit and contacted with a hydrotreating catalyst and hydrogen for hydrosaturation treatment to obtain the hydrogenated product of heavy oil. The hydrosaturation conditions include: a reaction pressure of 5 MPa, a reaction temperature of 280℃, and a hydrogen-to-oil volume ratio of 1000 Nm³. 3 / m 3 .

[0233] The hydrogenation products of heavy oil are fractionated to obtain a second aviation fuel component and a heavy hydrogenated distillate; the cut point of the second aviation fuel component and the heavy hydrogenated distillate is 300℃; the distillation range of the second aviation fuel component is 150~300℃.

[0234] The spent catalyst is introduced into regenerator 8 via pipeline 7 for coke burn-off regeneration, and the regenerated catalyst is returned to the bottom of the variable-diameter riser reactor via pipeline 11 for recycling. The regeneration conditions for the spent catalyst include: oxygen-containing gas is air; regeneration temperature is 580℃; bed pressure is 0.3MPa; and oxygen-containing gas residence time is 180 seconds.

[0235] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0236] Example 8

[0237] Example 8 was conducted on the experimental setup shown in the flowchart in Figure 1. In this example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic unit with a variable-diameter riser reactor.

[0238] Each operation is the same as in Example 1, and the processing conditions are shown in Table 4.

[0239] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0240] Comparative Example 1

[0241] Comparative Example 1 was conducted on the experimental setup shown in the flowchart in Figure 1. In this comparative example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic converter with a variable-diameter riser reactor. Regions I and II of the riser reactor were combined.

[0242] Bio-based feedstock oil and heavy hydrotreated distillate oil are mixed at a weight ratio of 5:1 and introduced into the bottom of a variable-diameter riser reactor. Methanol is introduced simultaneously. The regenerated catalyst is introduced into the bottom of the reactor via pipeline 11. In the reaction zone of the riser reactor, a reconstruction reaction takes place. The resulting reaction stream containing reacted oil and gas and the spent catalyst is separated in a settling tank. The spent catalyst is stripped in stripping section 4 and then enters regenerator 8 via pipeline 7.

[0243] The resulting reaction oil and gas are separated according to their boiling range in a separation unit. The dry gas obtained from the separation is led out through pipeline 14, the liquefied gas through pipeline 15, the naphtha through pipeline 16, the first aviation fuel component through pipeline 17, and the heavy oil product with a boiling point higher than the cut point through pipeline 18. The first aviation fuel component and the heavy oil product are obtained; the cut point for the first aviation fuel component and the heavy oil product is 230℃; the boiling range of the first aviation fuel component is 150–230℃.

[0244] Heavy oil is introduced into a medium-sized hydrotreating unit and contacted with a hydrotreating catalyst and hydrogen for hydrosaturation treatment to obtain the hydrogenated product of heavy oil. The hydrosaturation conditions include: a reaction pressure of 5 MPa, a reaction temperature of 280℃, and a hydrogen-to-oil volume ratio of 1000 Nm³. 3 / m 3 .

[0245] The hydrogenation products of heavy oil are fractionated to obtain a second aviation fuel component and a heavy hydrogenated distillate; the cut point of the second aviation fuel component and the heavy hydrogenated distillate is 300℃; the distillation range of the second aviation fuel component is 150~300℃.

[0246] The heavy hydrotreated distillate is recycled back to the bottom of the variable-diameter riser reactor in the required proportion for remodeling reaction. The spent catalyst is introduced into the regenerator 8 via pipeline 7 for coke burn regeneration, and the regenerated catalyst is returned to the bottom of the variable-diameter riser reactor via pipeline 11 for recycling. The regeneration conditions for the spent catalyst include: oxygen-containing gas is air; regeneration temperature is 580℃; bed pressure is 0.3MPa; and oxygen-containing gas residence time is 180 seconds.

[0247] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0248] Comparative Example 2

[0249] Comparative Example 2 was conducted on the experimental setup shown in the flowchart in Figure 1. In this comparative example, the bio-feedstock oil underwent a remodeling reaction experiment on a medium-sized catalytic converter with a variable-diameter riser reactor. Regions I and II of the riser reactor were combined.

[0250] Bio-based feedstock oil and heavy hydrotreated distillate oil are mixed at a weight ratio of 4:1 and introduced into the bottom of a variable-diameter riser reactor. Methanol is introduced simultaneously. The regenerated catalyst is introduced into the bottom of the reactor via pipeline 11. In the riser reactor, it contacts the reconstituted catalyst to undergo a reconstitution reaction. The resulting stream containing reacted oil and gas and the spent catalyst is separated in a settling tank. The spent catalyst is stripped in stripping section 4 and then enters regenerator 8 via pipeline 7.

[0251] The resulting reaction oil and gas are separated according to their boiling range in a separation unit. The dry gas obtained from the separation is led out through pipeline 14, the liquefied gas through pipeline 15, the naphtha through pipeline 16, the first aviation fuel component through pipeline 17, and the heavy oil product with a boiling point higher than the cut-off point through pipeline 18. The first aviation fuel component and the heavy oil product are obtained; the cut-off point for the first aviation fuel component and the heavy oil product is 230℃; the boiling range of the first aviation fuel component is 150–230℃.

[0252] Heavy oil is introduced into a medium-sized hydrotreating unit and contacted with a hydrotreating catalyst and hydrogen for hydrosaturation treatment to obtain the hydrogenated product of heavy oil. The hydrosaturation conditions include: a reaction pressure of 5 MPa, a reaction temperature of 280℃, and a hydrogen-to-oil volume ratio of 1000 Nm³. 3 / m 3 .

[0253] The hydrogenation products of heavy oil are fractionated to obtain a second aviation fuel component and a heavy hydrogenated distillate; the cut point of the second aviation fuel component and the heavy hydrogenated distillate is 300℃; the distillation range of the second aviation fuel component is 150~300℃.

[0254] The heavy hydrotreated distillate is recycled back to the bottom of the variable-diameter riser reactor in the required proportion for remodeling reaction. The spent catalyst is introduced into the regenerator 8 via pipeline 7 for coke burn regeneration, and the regenerated catalyst is returned to the bottom of the variable-diameter riser reactor via pipeline 11 for recycling. The regeneration conditions for the spent catalyst include: oxygen-containing gas is air; regeneration temperature is 580℃; bed pressure is 0.3MPa; and oxygen-containing gas residence time is 180 seconds.

[0255] The processing conditions, hydrogenation reaction conditions, and product distribution are shown in Table 4. The aviation fuel component, as a product, is obtained by mixing the first and second aviation fuel components, and the properties of the resulting aviation fuel component are shown in Table 5.

[0256] As can be seen from the data in Table 4, the method of this invention can achieve a high yield of aviation fuel components, and the yield can be further improved when the heavy hydrotreated distillate is recycled. Additionally, the yield of aviation fuel components can also be increased by refining the pre-reconstituted oil at an appropriate temperature.

[0257] Furthermore, as can be seen from Comparative Examples 1 and 2, if the temperature of the reconstruction reaction is too high, it will lead to the generation of a large amount of liquefied gas, and the yield of aviation fuel components will be greatly reduced.

[0258] As can be seen from the data in Table 5, the aviation fuel components obtained in the embodiments of the present invention have a relatively high content of cycloalkanes, while the content of aromatics does not exceed 25% by weight, and the freezing point of the fuel components is below -65°C. In contrast, the aviation fuel components in Comparative Examples 1 and 2 have relatively low contents of cycloalkanes, while having a high proportion of aromatics and low net calorific value.

[0259] This indicates that the method of the present invention can effectively convert biomass raw materials into aviation fuel components, resulting in aviation fuel components with higher energy density and lower freezing point.

[0260] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, and these simple modifications all fall within the protection scope of the present invention.

[0261] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the present invention will not describe the various possible combinations separately.

[0262] Furthermore, various different embodiments of the present invention can be combined in any way, as long as they do not violate the spirit of the present invention, they should also be regarded as the content disclosed by the present invention.

Claims

1. A method for preparing an aviation fuel component, characterized in that, It includes the following steps: S1. Reconstruction step, wherein the bio-based oil and the reconstruction catalyst are brought into contact under reconstruction reaction conditions to carry out a reconstruction reaction, thereby obtaining reactive oil and gas and the catalyst to be generated. The reconstruction reaction conditions include: a reaction temperature of 100-350°C, preferably 200-330°C; and a reaction time of 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds. S2, separation step, wherein the reaction oil and gas are separated to obtain a first aviation fuel component and heavy oil.

2. The method according to claim 1, wherein, The bio-based oil is derived from one or more of the following: vegetable oil, animal oil, microbial oil, waste cooking oil, and oil refinery by-products. Preferably, the bio-based oil is selected from fatty acid esters with 14 to 20 carbon atoms; Preferably, the content of unsaturated fatty acid esters in the bio-based oil is 10% to 80% by weight.

3. The method according to claim 1 or 2, wherein it satisfies at least one of the following conditions: The conditions for the reconstruction reaction include: The reaction temperature is 100–300℃, preferably 200–280℃; the weight hourly space velocity is 1–95 h⁻¹. -1 Preferably 5-85h -1 The weight ratio of the catalyst to the bio-based oil is 3-25, preferably 5-20; the reaction time is 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds. The cutting point between the first aviation fuel component and the heavy oil is any temperature selected between 130 and 300°C, preferably any temperature selected between 150 and 280°C; The initial boiling point of the first aviation fuel component is any temperature between 100 and 180°C.

4. The method according to any one of claims 1-3, wherein, The catalyst includes zeolite, inorganic oxides, and optionally clay; Based on the weight of the catalyst, the catalyst comprises 1% to 50% by weight of zeolite, 5% to 99% by weight of inorganic oxides, and 0% to 70% by weight of clay; wherein the zeolite comprises mesoporous zeolite and optionally macroporous zeolite; based on the weight of the zeolite, the content of mesoporous zeolite is 51% to 100% by weight, and the content of macroporous zeolite is 0% to 49% by weight. The catalyst further satisfies at least one of the following conditions: The molar ratio of SiO2 to Al2O3 in the mesoporous zeolite is 50 or more, preferably 80 or more, and the molar ratio of SiO2 to Al2O3 does not exceed 300, preferably not more than 280. The mesoporous zeolite is selected from at least one of ZSM series zeolites, ZRP zeolite and mordenite; The macroporous zeolite is selected from at least one of rare earth Y-type zeolite, rare earth HY-type zeolite, ultra-stable Y-type zeolite, high-silica Y-type zeolite, and β-type zeolite.

5. The method according to any one of claims 1-4, wherein, Prior to the reconstruction step in step S1, a pre-reconstruction step S0 is further included, wherein, S0, Pre-reconstruction step, wherein fossil feedstock oil is contacted with a reconstruction catalyst under pre-reconstruction conditions to undergo a first reconstruction treatment, yielding a first reconstruction reaction stream; and S1, Reconstruction Step, wherein the first reconstruction reaction stream and bio-based oil are subjected to a second reconstruction treatment under reconstruction reaction conditions to obtain reaction oil and gas and catalyst to be generated.

6. The method according to any one of claims 1-5, wherein, Prior to the reconstruction step in step S1, a pre-reconstruction step in step S0 is further included. S0, Pre-reconstruction step, wherein at least a portion of the heavy hydrotreated distillate from step S4 is used as a fossil feedstock and is contacted with a reconstruction catalyst under pre-reconstruction conditions to undergo a first reconstruction treatment, thereby obtaining a first reconstruction reaction stream. S1, Reconstruction step, wherein at least a portion of the first reconstruction reaction stream, bio-feedback oil, and optionally the heavy hydrotreated distillate from step S4 are subjected to a second reconstruction treatment under reconstruction reaction conditions to obtain reaction oil and gas and catalyst to be generated. S2, Separation step, wherein the reacted oil and gas are separated to obtain a first aviation fuel component and heavy oil. S3, Hydrogenation step, wherein the heavy oil and hydrogen are brought into contact under a hydrogenation catalyst to carry out a hydrogenation reaction, thereby obtaining the hydrogenated product of the heavy oil. S4, Fractionation and Reflux Step, wherein the heavy oil hydrotreating product is fractionated to obtain a second aviation fuel component and heavy hydrotreating distillate, at least a portion of the heavy hydrotreating distillate is recycled back to the pre-reconstruction step of S0 as a fossil feedstock, and optionally at least a portion of the heavy hydrotreating distillate is recycled back to the reconstruction step of S1. S5. Blending step: Blend the first aviation fuel component and the second aviation fuel component to obtain an aviation fuel component.

7. The method according to claim 6, wherein, The cutting point between the first aviation fuel component and the heavy oil is any temperature selected between 130 and 300°C, preferably any temperature selected between 150 and 280°C; the cutting point between the second aviation fuel component and the heavy hydrotreated distillate is any temperature selected between 250 and 300°C. The initial boiling point of the first aviation fuel component and the second aviation fuel component are any temperature between 100 and 180°C.

8. The method according to any one of claims 1-7, wherein, In step S1, an oxygen-containing organic compound is introduced into the reconstitution step; wherein the weight ratio of the introduced oxygen-containing organic compound to the bio-based oil is (0.01-0.8):1, preferably (0.02-0.4):1; Preferably, the oxygen-containing organic compound is at least one selected from alcohols, ketones and ethers having 4 or fewer carbon atoms, and more preferably one or more selected from methanol, ethanol, dimethyl ketone, dimethyl ether and diethyl ether.

9. The method according to claim 5 or 6, wherein it satisfies at least one of the following conditions: In step S0, the reaction conditions for the pre-reconstruction step include: The reaction temperature is 330-500℃, preferably 330-450℃; the weight hourly space velocity is 1-95 h⁻¹. -1 Preferably 10-70h -1 The reaction time is 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds; the weight ratio of the catalyst to the fossil feedstock oil is 3-25, preferably 5-20. In step S1, the reaction conditions for the reconstruction step include: a reaction temperature of 200-330℃, preferably 280-330℃; and a weight hourly space velocity of 1-95 h⁻¹. -1 Preferably 10-70h -1 The reaction time is 0.01-200 seconds, preferably 0.1-80 seconds, and more preferably 1-20 seconds; The weight ratio of the bio-based oil used in the reconstruction step of step S1 to the first reconstruction reaction stream is (1-90):1, preferably (3-80):1; The weight ratio of the catalyst used in the pre-reconstruction step to the bio-based oil used in the reconstruction step is 3 to 25, preferably 5 to 20.

10. The method according to claim 6 or 7, wherein, The conditions for the hydrogenation reaction include: a reaction pressure of 2.5–25.0 MPa, preferably 3.5–18.5 MPa; a reaction temperature of 120–400 °C, preferably 150–390 °C; and a hydrogen-to-oil volume ratio of 220–2600 Nm³. 3 / m 3 Preferably, it is 310–2100 Nm 3 / m 3 The volumetric hourly space velocity (VHSV) is 0.05–20.0 h⁻¹. -1 Preferably, the time is 0.15 to 10.5 h. - 1 ; Preferably, the hydrogenation catalyst comprises a support and an active component supported on the support, wherein the metal element in the active component comprises at least one Group VIII metal, at least one Group VIB metal, and optional additives; Preferably, based on the weight of the hydrogenation catalyst, the hydrogenation catalyst comprises 1 to 38 wt% of a Group VIII metal, 1 to 51 wt% of a Group VIB metal, and 0 to 11 wt% of additives. Preferably, the additive is selected from one or more of fluorine, phosphorus, magnesium, titanium and platinum; Preferably, the carrier is selected from at least one of alumina, amorphous silica-alumina, and zeolite.

11. The method according to any one of claims 1-10, wherein, The method also includes: S6. Regeneration step, wherein the catalyst to be regenerated is subjected to coking regeneration to obtain a regenerated catalyst, and the regenerated catalyst is returned to the previous reconstruction step for recycling. Preferably, the regenerated catalyst is cooled to 300-500°C through a heat exchange step, preferably to 350-450°C, and then returned to the previous reconstruction step for recycling. Alternatively, if the previous reconstruction step is not performed, the catalyst is returned to the reconstruction step for recycling. In this case, preferably, the regenerated catalyst is cooled to 300-500°C through a heat exchange step, preferably to 350-450°C, and then returned to the reconstruction step for recycling. The conditions for coke regeneration include: coke regeneration is carried out in the presence of oxygen-containing gas; the coke regeneration temperature is 400–750°C, preferably 500–600°C; the bed pressure is 0.1–0.45 MPa, preferably 0.12–0.40 MPa; and the residence time of oxygen-containing gas is 0.1–300 seconds, preferably 1–240 seconds.

12. A system for preparing aviation fuel components, characterized in that, Includes the following units: The remodeling unit is equipped with a bio-based oil inlet and a catalyst inlet, wherein the bio-based oil and the remodeling catalyst are brought into contact under remodeling reaction conditions to carry out a remodeling reaction, and the resulting reaction oil and gas and the catalyst to be generated are obtained. A separation unit, connected downstream of the remodeling unit, separates the reacted oil and gas to obtain a first aviation fuel component and heavy oil.

13. The system according to claim 12, wherein, A pre-reconstruction region is provided in the upstream portion of the reconstruction unit, and a reconstruction region is provided in the downstream portion of the reconstruction unit, wherein... The pre-reconstruction zone includes a fossil feedstock inlet and a catalyst inlet. The fossil feedstock is brought into contact with the reconstruction catalyst under pre-reconstruction conditions to undergo the first reconstruction treatment, yielding the first reconstruction reaction stream. The reconstruction zone is connected to the pre-reconstruction zone. The reconstruction zone is provided with a bio-based oil inlet. The first reconstruction reaction stream and the bio-based oil from the pre-reconstruction zone are brought into contact under reconstruction reaction conditions to undergo a second reconstruction process, resulting in reaction oil and gas and a catalyst to be generated.

14. The system according to claim 13, characterized in that, It further includes the following units: The hydrogenation unit is connected downstream of the separation unit, which allows the heavy oil from the separation unit to come into contact with hydrogen in the presence of a hydrogenation catalyst to carry out a hydrogenation reaction and obtain the hydrogenated product of the heavy oil. A fractionation reflux unit is connected downstream of the hydrotreating unit, wherein the hydrotreating product of heavy oil from the hydrotreating unit is fractionated to obtain a second aviation fuel component and heavy hydrotreating distillate. The fractionation reflux unit is connected upstream of the pre-reconstruction zone, so that at least a portion of the heavy hydrotreating distillate is recycled back to the pre-reconstruction zone as fossil feedstock for a first reconstruction process. Optionally, the fractionation reflux unit is connected upstream of the reconstruction zone, and at least a portion of the heavy hydrotreating distillate is recycled back to the reconstruction zone for a second reconstruction process. and A blending unit, wherein the first aviation fuel component and the second aviation fuel component are blended to obtain an aviation fuel component.

15. The system according to claim 13 or 14, wherein, The reconstruction zone is further provided with an oxygen-containing organic compound inlet, allowing the oxygen-containing organic compounds to enter the reconstruction zone and participate in the second reconstruction process.

16. The system according to any one of claims 12-15, further comprising a catalyst regeneration unit connected downstream of the separation unit to regenerate the spent catalyst from the separation unit by coking to obtain a regenerated catalyst, and connected upstream of the reconstruction unit to feed the regenerated catalyst into the reconstruction unit for recycling; or, if a pre-reconstruction zone exists, connected upstream of the pre-reconstruction zone to feed the regenerated catalyst into the pre-reconstruction zone for recycling. Preferably, a heat exchange unit is provided between the regeneration unit and the reconstruction unit, so that the regenerated catalyst is cooled to 300-500°C, preferably to 350-450°C.

17. The system according to any one of claims 12-16, wherein, The pre-reconstruction zone and the reconstruction zone each use a reconstruction reactor independently. The reconstruction reactor is selected from one or more combinations of fluidized bed, fixed bed, moving bed, and slurry bed. Preferably, the fluidized bed reactor is selected from one or more combinations of risers, constant velocity fluidized beds, constant diameter fluidized beds, upward conveying lines, and downward conveying lines, or two or more combinations of the same type of reactor, including series and / or parallel connections. The riser is selected from a constant diameter riser or a variable diameter riser; and / or The pre-reconstruction zone and the reconstruction zone each use a reconstruction reactor independently. The reconstruction reactor is a variable diameter riser reactor, or the reconstruction reactor includes a riser and a fluidized bed from bottom to top. Preferably, the pre-reconstruction zone and the reconstruction zone use the same reconstruction reactor, which are located in the upstream and downstream zones of the reconstruction reactor, respectively.

18. Aviation fuel components, wherein, Based on the weight of the components, the mixture comprises 30-70% (preferably 40-50%) of alkanes, 20-50% (preferably 29-45%) of total cycloalkanes, and 10-25% (preferably 15-25%) of total aromatics, with a freezing point below -40°C, preferably below -65°C. The total cycloalkanes, based on their weight, comprise 60-83% (preferably 65-83%) of monocyclic cycloalkanes, 16-35% (preferably 16-30%) of dicyclic cycloalkanes, and 1-10% (preferably 2-8%) of tricyclic cycloalkanes.

19. The aviation fuel component according to claim 18, wherein, At least one of the following conditions must be met: Based on the weight of the total aromatics, the total aromatics contain 30-63.5% (preferably 40-63%) of alkylbenzenes, 34.5-70% (preferably 37-60%) of indenes and / or tetrahydronaphthalenes; The final boiling point of the aviation fuel component is 250–300°C.

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