Method for producing transport fuel and components thereof

Abstract

The present invention relates to a process for the production of jet fuels, diesel, or components thereof from a pretreated feed comprising at least 90 wt.-% liquid paraffins by a hydroisomerization reaction using a support-based metal impregnated EU-2-based zeolite as a catalyst. According to the method, the desired product distribution is adjusted by the hydroisomerization reaction temperature.

Description

Technical Field

[0001] This disclosure relates to methods for producing transport fuels or components thereof from alkane feedstocks, particularly jet fuels, diesel fuels or components thereof, and more particularly to methods including hydroisomerization of alkane feedstocks in the presence of a catalyst comprising an active metal and EU-2 zeolite. Background Technology

[0002] Transportation fuels such as aviation gasoline, jet fuel, gasoline, and diesel can be produced from a variety of feedstocks, including crude oil, coal, vegetable oil, animal fat, waste oil and residual oil and fat, municipal waste, waste plastics, and even used tires. Furthermore, the production of transportation fuels has been proposed starting with the reduction of carbon dioxide with renewable hydrogen, via a reverse water-gas shift reaction, followed by, for example, a Fischer-Tropsch reaction to form the desired hydrocarbons.

[0003] This method includes one or more steps for converting the feedstock into an alkane feed. The alkane feedstock is typically further processed, for example, by hydrocracking and / or hydroisomerization, to obtain the desired performance of the transport fuel or its components.

[0004] It is known that the type of transport fuel can be controlled by the hydroisomerization reaction conditions. For example, EP 2138552B1 discloses a method for converting renewable feedstocks into diesel fuel by hydrotreating a catalyst containing at least one Group VIII metal and / or at least one Group VIB metal and at least one one-dimensional 10MR zeolite molecular sieve selected from ZSM-48 and ZBM-30 at a temperature in the range of 150°C to 500°C, followed by using the catalyst in the mixture.

[0005] EP 2275514 further converts renewable feedstocks into light fuels through a method involving the deoxygenation of natural fats or their derivatives, followed by hydrocracking and isomerization steps. The isomerization reaction is carried out in the presence of a catalyst based on a hydrogen transfer component and an acid component at temperatures ranging from 100°C to 500°C. The hydrogen transfer component is a transition metal selected from Groups 5-10 of the periodic table (IUPAC 1990), preferably Ni, Pd, Pt, Co, Mo, and V, and most preferably platinum. The acid component is preferably an inorganic oxide compound with acid sites, more preferably selected from alumina chloride and protonated 10- and 12-membered zeolites, and even more preferably selected from protonated PSH-3, β-, and MCM-22 zeolites. Most preferably, the acid component is protonated mordenite, protonated beta-zeolite, or protonated ZSM-12.

[0006] WO 2023126565 discloses a method for preparing renewable aviation fuel or components thereof from renewable feedstock, wherein the method includes separate hydrodeoxygenation and hydroisomerization steps, wherein the hydroisomerization is catalyzed by metal-impregnated graded ZSM-23. Summary of the Invention

[0007] This invention is based on the observation that when a feed containing at least 90 wt.% of pretreated liquid alkanes is hydroisomerized using an active metal selected from noble metals, nickel, and any combination thereof, and EU-2 zeolite supported on a support as a hydroisomerization catalyst, the product distribution can be adjusted to primarily produce jet fuel or its components, or diesel fuel or its components can be primarily produced by adjusting the hydroisomerization temperature.

[0008] Therefore, the object of the present invention is to provide a method for producing a transport fuel comprising jet fuel, diesel fuel, or components thereof, the method comprising: a) Provide a pretreated liquid feed comprising at least 90 wt.% alkanes; b) The pretreated liquid feed is subjected to a hydroisomerization reaction in the presence of a hydrogen stream and a hydroisomerization catalyst at a pressure of 1 bar to 100 bar, preferably 20 bar to 100 bar, more preferably 20 bar to 90 bar, for example 20 bar to 60 bar. The hydroisomerization catalyst comprises an active metal selected from noble metals, nickel, and any combination thereof, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica, wherein the content of the active metal in the catalyst is from 0.1 wt.-% to 7.0 wt.-%, and the SiO2 / Al2O3 molar ratio of the EU-2 zeolite is from 10 to 100, preferably from 15 to 85, for example from 40 to 80. The hydroisomerization reaction temperature is adjusted to between 270°C and 370°C to provide a hydroisomerization stream comprising the desired hydroisomerized hydrocarbon composition. i. For hydrocarbons suitable for use as jet fuel or components thereof and hydrocarbons suitable for use as diesel fuel or components thereof, the weight ratio is greater than 1, the temperature adjustment is 330°C to 370°C, preferably 336°C to 370°C, more preferably 336°C to 360°C, and ii. For hydrocarbons suitable for use as diesel fuel or components thereof and hydrocarbons suitable for use as jet fuel or components thereof, the weight ratio is greater than 1, adjusted to a temperature from 270°C to 324°C, preferably from 270°C to 320°C, more preferably from 280°C to 320°C, and c) Recovery from the hydroisomerization stream by separating hydrocarbons suitable for use as jet fuel or components thereof, or hydrocarbons suitable for use as diesel fuel or components thereof, as the main product.

[0009] Another object of the present invention is to provide a use of a catalyst comprising an active metal selected from noble metals, nickel, and any combination thereof, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica, wherein the active metal in the catalyst comprises an amount from 0.1 wt.% to 7.0 wt.% wt.-%, wherein the SiO2 / Al2O3 molar ratio of EU-2 zeolite is 10 to 100, preferably 15 to 85, such as 40 to 80, at a pressure of 1 bar to 100 bar, preferably 20 bar to 100 bar, more preferably 20 bar to 90 bar, for example 20 bar to 60 bar, at 270-324°C, preferably 270-320°C, more preferably 280-320°C, under an H2 stream used to regulate the product distribution of the hydroisomerization reaction to primarily produce diesel fuel or components thereof, and at 330-370°C, preferably 336-370°C, more preferably 336-360°C, primarily producing jet fuel or components thereof.

[0010] Several exemplary and non-limiting embodiments of the invention are described in the appended dependent claims.

[0011] Various exemplary and non-limiting embodiments of the invention, as well as their additional objects and advantages, will be best understood from the following description of specific examples and non-limiting embodiments when read in conjunction with the accompanying drawings.

[0012] The verbs “to comprise” and “to include” are used herein as open-ended restrictions, neither excluding nor requiring the presence of any unstated features. Unless otherwise expressly stated, features stated in the dependent claims may be freely combined with each other. Furthermore, it should be understood that the use of “an” or “a” (i.e., the singular form) throughout this document does not exclude a plurality. Attached Figure Description

[0013] Figure 1 An exemplary non-limiting flowchart of the method of the present invention for producing jet fuel or diesel from a liquid alkane feedstock is shown.

[0014] Figure 2 Exemplary carbon number distributions of hydroisomerization products from liquid alkane feedstocks using EU-2-based catalysts and commercially available catalysts at different hydroisomerization temperatures are shown.

[0015] Figure 3 An exemplary product distribution of hydroisomerization of a liquid n-chain alkane feed using an EU-2-based catalyst as the hydroisomerization temperature varies is shown.

[0016] Figure 4An exemplary product distribution of hydroisomerization of an alkane feed using a commercial reference catalyst is shown as a function of hydroisomerization temperature.

[0017] Figure 5 The cloud point of the hydroisomerization product is shown as a function of the hydroisomerization reaction temperature.

[0018] Figure 6 The pour point (PP) of the hydroisomerization product is shown as a function of the hydroisomerization reaction temperature.

[0019] Figure 7 The freezing point of the hydroisomerization product is shown as a function of the hydroisomerization reaction temperature. Detailed Implementation

[0020] This disclosure relates to using a catalyst comprising an active metal selected from precious metals, nickel, and any combination thereof, and EU-2 zeolite supported on a support as a hydroisomerization catalyst to convert a feedstock containing at least 90 wt.% liquid alkanes and having a suitable impurity distribution into a transport fuel or a component thereof at a specific reaction temperature.

[0021] The principle of this method is... Figure 1 The exemplary non-restrictive flowchart shown discloses and includes the following actions: 101. Provides a pretreated liquid feed comprising at least 90 wt.% alkanes; 102. Select the desired product; 103 Hydroisomerize the feed to the temperature at which the desired product is primarily produced; 104 Separate the desired product.

[0022] In this invention, jet fuel, also known as aviation turbine fuel, is a type of aviation fuel designed for use in aircraft powered by gas turbine engines. Jet fuels, as discussed herein, typically contain hydrocarbons with a carbon number range from C8 to C16, depending on the amount of n- and iso-alkanes and their degree of branching. Because the exact composition of jet fuel varies widely based on the feedstock and its subsequent processing, it is not possible to define jet fuel solely by the carbon number range of the hydrocarbons. Jet fuel is defined as a performance specification rather than a chemical composition; that is, the product needs to be suitable for use as jet fuel. The molecular weight range between hydrocarbons is defined by requirements of the product, such as cloud point or flash point, derived from the type of hydrocarbons present in the blend. Kerosene-type jet fuels typically contain alkanes with a carbon number distribution of approximately 8-16.

[0023] In this disclosure, diesel fuel typically contains hydrocarbons having a carbon number range from C12 to C21, depending on the amount of n- and iso-alkanes and their branches, and needs to have the desired properties that make it suitable for use as a diesel fuel.

[0024] It is generally known that alkanes and alkyl alkanes are synonyms and can be used interchangeably. Isoalkyl alkanes (i-alkanes) are branched, acyclic alkyl alkanes, and n-alkanes (n-alkanes) are unbranched, straight-chain alkyl alkanes. The term "multibranched" as used herein refers to isoalkyl alkanes containing more than one branch, such as two, three, or four branches, and is the opposite of "monobranched." In the context of this disclosure, the term "alkyl alkanes" refers to n-alkanes and / or isoalkyl alkanes. Similarly, the term "alkyl alkanes" herein refers to compositions comprising n-alkanes and / or isoalkyl alkanes.

[0025] The feed needs to be suitable for hydroisomerization, particularly the catalyst used for hydroisomerization. Furthermore, the feed needs to be in liquid form under processing conditions. Typically, alkane feeds contain a variety of impurities, depending on the feed source and the upstream processing desired to make the feed suitable for hydroisomerization of the alkane. Impurities herein refer to any kind of elemental metal, such as alkali metals, alkaline earth metals, or transition metals, or compounds containing them; compounds containing heteroatoms such as S, N, O, P, Si, or halogens; aromatic compounds; or even excess water, etc., substances that cannot be included in alkane feeds suitable for fuel applications. These impurities are typically removed, or at least reduced in quantity, using various purification or pretreatment methods in the various upstream processing steps that ultimately provide pretreated alkane feeds.

[0026] Typically, the feedstock entering hydroisomerization should not contain more than [amount missing].

[0027] ● 1 w-ppm, preferably no more than 0.5 w-ppm alkali metal and alkaline earth metal impurities, calculated as elemental alkali metals and alkaline earth metals; ● 1 w-ppm, preferably no more than 0.5 w-ppm, other metals, calculated as elemental metals; ● Nitrogen-containing impurities of 5 w-ppm, preferably not more than 1 w-ppm, more preferably not more than 0.2 w-ppm, calculated as elemental nitrogen; ● 5 w-ppm, for example, phosphorus-containing impurities not exceeding 1 w-ppm, calculated as elemental phosphorus; ● 1 w-ppm silicon impurities, calculated as elemental silicon; ● Sulfur-containing impurities of 10 w-ppm, preferably no more than 5 w-ppm, more preferably no more than 1 w-ppm, and most preferably no more than 0.4 w-ppm, calculated as elemental sulfur; ● Chlorine-containing impurities of 10 w-ppm, preferably no more than 5 w-ppm, calculated as elemental chlorine.

[0028] The level of impurities typically depends on the feedstock treatment prior to isomerization. If the isomerization feedstock is derived from electrosynthetic crude oil, i.e., obtained from CO2 and H2 via oligomerization or the Fischer-Tropsch pathway, the feedstock will be free of many metallic, sulfur-containing, or nitrogenous impurities, but may still contain some water that should be removed. If the feedstock is of biological origin, such as renewable materials like animal, plant, or fish oil / fat, the levels of metallic, oxygen-containing, sulfur-containing, or nitrogenous impurities may need to be reduced before further processing using separate pretreatment methods. The same applies to the use of fossil feedstocks.

[0029] Furthermore, under the processing conditions, the feed needs to be in liquid form. Gases and vapors, such as water vapor or ammonia, are preferably removed from the feed before being introduced into the hydroisomerization process.

[0030] Hydroisomerization is typically carried out in the presence of a hydrogen stream at a pressure of 1 to 100 bar, preferably 20 to 100 bar, more preferably 20 to 90 bar, for example 20 to 60 bar. The H2 stream is typically 100 to 800 N-L H2 / L feed (standard liters of hydrogen / L feed), preferably 200 to 600 N-L H2 / L feed.

[0031] The hydroisomerization catalyst used in the method of the present invention comprises an active metal, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica. The active metal is selected from noble metals such as Pt, Pd, Rh, and Ni, and any combination thereof. The active metal content of the catalyst is from 0.1 wt.% to 7.0 wt.% and preferably from 0.1 wt.% to 5.0 wt.%. According to embodiments, the active metal of the reduction catalyst is preferably used under an H2 flow of 360-380°C and 35-45 bar.

[0032] The active metal facilitates hydrogen separation within the catalyst. The support serves as a diluent for the catalyst system, preferably a three-component catalyst system, and it can modulate its thermal behavior and provide mechanical robustness to the structure. EU-2 zeolite primarily determines isomerization and cracking performance. The activity and selectivity of isomerization and cracking are influenced by other components in the structure.

[0033] The SiO2 / Al2O3 molar ratio of EU-2 zeolite is 10-100, preferably 15-85, for example 40-80, which has a balanced effect on the cracking and / or branching performance of the catalyst.

[0034] Preferably, EU-2 zeolite further comprises one or more of the following characteristics: Crystallinity is 50% to 95%, measured by X-ray diffraction (XRD) according to ASTM D5758-01 (2021).

[0035] BET has a specific surface area of ​​180m².2 / g to 450m 2 / g, for example 200m 2 / g to 300m 2 / g, determined by nitrogen physisorption. Appropriate porosity is required to facilitate access to the active sites of the material and improve reaction efficiency.

[0036] Acidity ranges from 80 μmol / g to 700 μmol / g, preferably from 150 μmol / g to 500 μmol / g, more preferably from 200 μmol / g to 400 μmol / g, such as from 350 μmol / g to 400 μmol / g, measured by a pyridine-FTIR method. Similarly, for the silica-alumina ratio, acidity affects the cracking and / or branching performance of the catalyst.

[0037] The ratio of Brønsted acid sites to Lewis acid sites ranges from 0.5 to 22, preferably from 5 to 15, as measured by pyridine-FTIR. This allows for tuning of catalyst activity to balance the isomerization / cracking ratio, enhancing the cracking of n-alkanes from intermediate positions, thereby favoring the formation of hydrocarbons suitable for use as jet fuel, diesel fuel, or components thereof.

[0038] Crystalline zeolite particles are basically needle-shaped, meaning that their morphology is mainly needle-shaped.

[0039] In the hydroisomerization process, n-chain alkanes are hydrocracked and / or converted to isochain alkanes. The catalyst of the present invention has been found to offer a higher tendency for branching than, for example, catalysts based on commercial SAPO-11. Furthermore, cracking initiates at lower temperatures, suggesting that this catalyst has the potential to produce jet fuels and renewable diesel fuels with improved cryogenic performance.

[0040] Furthermore, despite the high isomerization temperature, the catalyst of this invention can still avoid cracking into light hydrocarbons (<C4), i.e., the amount of cracking products remains within the range of transportation fuels and still contains multibranched compounds that ensure high quality. Other catalysts tend to further crack hydrocarbons, especially alkanes, into C1-C3 products and enhance high C loss, thereby reducing carbon efficiency as a desired outcome.

[0041] According to the method of the invention, the product distribution can be adjusted by carrying out the hydroisomerization reaction at different temperatures. The possibility of tailoring the isomerization products makes production flexible and market-driven. This flexibility allows for specific production for diesel and jet fuel, and even for renewable products such as aviation gasoline and / or naphtha, without the need for different catalysts, i.e., catalyst replacement in the reactor. Furthermore, the possibility of temperature adjustment helps mitigate the impact of varying feedstock quality on the processing.

[0042] Using the same catalyst to produce both jet fuel and diesel offers operational advantages. For example, using a single catalyst in the hydroisomerization reactor allows for easier control of reaction temperature, gas and liquid flow distribution, and the handling of catalyst deactivation, as these parameters are catalyst-dependent. Furthermore, using a single catalyst and a single reactor makes it easier and safer to switch between jet fuel and diesel production modes compared to using two different catalysts. Naturally, it also avoids the need for separate hydroisomerization reactors to produce both jet fuel and diesel.

[0043] The hydroisomerization products primarily consist of C5-C22 hydrocarbons, which can be separated or fractionated into different products, preferably by distillation. Fractionation can be performed as needed. A portion of the hydrocarbons in the jet fuel range and diesel range can be modified by varying the temperature of the isomerization reaction using the catalyst disclosed herein.

[0044] For example, as shown in Table 1, increasing the processing temperature significantly increases the yield of hydrocarbons in the jet fuel range.

[0045] Table 1.

[0046] The catalyst in this method can hydrocracking hydrocarbons suitable for inclusion in the jet fuel hydrocarbon range without producing excessive amounts of light hydrocarbons, such as C1-C3 hydrocarbons. Furthermore, the catalyst in this method provides longer branching of hydrocarbons, thus enhancing the reduction of the cold properties of the formed hydrocarbons.

[0047] The adjustable temperature range allows the desired product to be the main component of the hydroisomerization reaction, i.e., the major product.

[0048] According to the embodiments, the hydroisomerization reaction is carried out at a temperature in the range of 330°C to 370°C, preferably 336°C to 370°C, and more preferably 336°C to 360°C. This temperature range primarily produces hydrocarbons suitable for jet fuels or their components, having an initial distillation boiling point of about 106°C and a final distillation boiling point of about 280°C at atmospheric pressure (1 bar (absolute pressure)). The pressure of the hydroisomerization reaction is 1 to 100 bar, preferably 20 to 100 bar, more preferably 20 to 90 bar, such as about 20 to 60 bar.

[0049] According to another embodiment, the hydroisomerization reaction is carried out at a temperature ranging from 270°C to 324°C, preferably from 270°C to 320°C, and more preferably from 280°C to 320°C. This temperature range primarily produces hydrocarbons suitable for diesel fuel or its components, having an initial distillation boiling point of about 170°C at atmospheric pressure (1 bar (absolute pressure)) and a final distillation boiling point of about 360°C at atmospheric pressure (1 bar (absolute pressure)). The pressure of the hydroisomerization reaction is from 1 to 100 bar, preferably from 20 to 100 bar, more preferably from 20 to 90 bar, such as about 20 to 60 bar.

[0050] In this implementation, the hydroisomerization stream undergoes a separation step to produce...

[0051] The fraction that boils between 106°C and 280°C at atmospheric pressure (1 bar (absolute pressure)) is used to recover jet fuel or its components, or

[0052] The fraction that boils between 170°C and 360°C at atmospheric pressure (1 bar (absolute pressure)) is used to recover diesel fuel or its components.

[0053] In addition, other fractions can be recovered, such as fractions that boil at atmospheric pressure (1 bar (absolute pressure)) between 36°C and 135°C, i.e., aviation gasoline (avgas) or its components.

[0054] The separation may include one or more of the following: distillation, fractionation, evaporation, flash separation, membrane separation, extraction, distillation using extractive distillation, chromatography, molecular sieve adsorbents, thermal diffusion, complex formation, preferably at least distillation.

[0055] Any separated fraction may be subjected to one or more further purification and / or fractionation steps. Optional purification and / or fractionation steps or treatments may be selected depending on the desired end use and / or the desired purity of the fraction.

[0056] According to one embodiment, the method involves producing sustainable aviation fuel (SAF) or a component thereof. SAF is aviation fuel that meets standards that emphasize environmental, social, and economic "triple bottom line" considerations. Sustainable aviation fuel is produced from alkane feedstock obtained from renewable resources.

[0057] To date, few pathways for producing sustainable aviation fuel (SAF) have been approved for blending with jet fuels under ASTM D7566, including Fischer-Tropsch hydrotreated synthetic alkane kerosene and synthetic alkane kerosene produced from hydrotreated esters and fatty acids.

[0058] The feedstock for hydroisomerization can be derived from a variety of different feedstocks and suitable upgrading methods. The feedstock can be of biological origin, i.e., renewable feedstocks such as those from vegetable oils, fish oils, and / or animal fats, typically containing triglycerides, esters of free fatty acids, and fatty acids (see, for example, WO2023126562 for detailed feed materials). It can further include waste and residues, such as waste cooking oil, palm oil plant effluent, acid oils, brown grease, municipal solid waste, etc., or it can be derived from recycled materials, such as solid or liquid biomass, end-of-life tires, liquefied organic waste, or residues. The feedstock can further include petrochemicals or different mixtures of petrochemicals and renewable oils. It can even be derived from e-crude, i.e., using different grades of carbon dioxide and hydrogen as starting materials for synthetic hydrocarbons.

[0059] The renewable properties of carbon-containing compositions (such as bio-derived feedstocks and products, i.e., renewable feedstocks and products) can be demonstrated by the fact that by 1950, the feedstocks... 14 C isotope content and air 14 The determination is made by comparing the C isotope content. 14 Carbon isotope content can serve as evidence of a renewable source of raw materials or products. Compared to carbon atoms from fossil sources, carbon atoms in renewable materials contain a higher number of unstable radioactive carbon atoms (C). 14 C) Atoms. Therefore, through analysis 12 C and 14 The ratio of carbon isotopes can distinguish between carbon compounds derived from biological sources and those derived from fossil sources. Therefore, a specific ratio of these isotopes can be used to identify and quantify renewable carbon compounds and to differentiate them from non-renewable (i.e., fossil carbon compounds). The isotope ratio does not change during chemical reactions. An example of a suitable method for analyzing carbon content from biological sources is ASTM D6866 (2020). An example of how ASTM D6866 can be applied to determine the renewable content in fuels is provided in Dijs et al., Radiocarbon, 48(3), 2006, pp. 315-323. For the purposes of this invention, a carbon-containing material is considered to be of renewable origin if it contains 90% or more modern carbon, such as 100% modern carbon, as measured using ASTM D6866.

[0060] As defined herein, recycled feedstocks or even synthetic crude oil can be based on reused and / or recycled renewable carbon from any available source.

[0061] The renewable feedstock may include animal and fish oils / fats, vegetable oils and / or vegetable and / or microbial oils, typically containing oxygen, sulfur, nitrogen, phosphorus and / or silicon as heteroatoms and metals as the main impurities. The hydrocarbons obtained after hydrotreating typically have a carbon number of C12-C22 or even C28, depending on the feedstock used, with the hydrocarbon distribution peaking around C16-C18.

[0062] Depending on the type and amount of heteroatoms and impurities, oils derived from renewable feedstocks are typically pretreated using various methods, such as degumming, decolorization, heat treatment, and RBD (refining, decolorization, and deodorization).

[0063] If the feedstock contains fossil crude oil, the resulting hydrocarbons typically contain heteroatoms, primarily sulfur and nitrogen, as well as metallic impurities. Therefore, this type of feedstock requires pretreatment similar to that for renewable feedstocks to purify it.

[0064] Synthetic hydrocarbons produced from carbon dioxide and hydrogen (typically via syngas) are essentially free of heteroatoms or metallic impurities. Therefore, specific pretreatment methods are not necessarily required. However, depending on the uptake method, the carbon number distribution of the resulting hydrocarbons can be broad, ranging from light hydrocarbons (C1-C3) to waxes (C50+).

[0065] Typically, waste and residual materials contain a wide variety of heteroatom compounds that are often more difficult to remove by conventional feedstock pretreatment methods typically used for pretreatment of triacylglycerol-containing matrices. Waste and residual materials may include accumulated alkali and alkaline earth metals such as sodium, potassium, calcium, and magnesium; other metals such as iron or copper; nitrogen-containing compounds such as amines and amides; phosphorus-containing compounds such as phospholipids; silicon-containing compounds such as siloxanes and polydimethylsiloxane (PDMS); halides; sulfur-containing compounds, etc., depending on the type of residue / waste. These materials, particularly in higher quantities, are typically detrimental to catalysts used in hydrotreating and / or isomerization and need to be reduced or removed before the feedstock is fed onto the catalyst.

[0066] Depending on the level of pretreatment, fats, oils, and greases can contain high levels of impurities, such as approximately 1-1000 w-ppm (wt ppm) of phosphorus; and approximately 1-500 wt ppm of total metals, primarily sodium, potassium, magnesium, calcium, iron, and copper. It is not uncommon for animal fats to contain, for example, 1000 w-ppm or even higher levels of nitrogen (measured as elemental nitrogen).

[0067] Several known methods exist for removing or reducing the amount of hazardous materials, and different purification or pretreatment methods are typically applied. Generally, any means used for purifying the feed can be employed.

[0068] Exemplary pretreatment methods suitable for this disclosure include treatment with inorganic acids, degumming, treatment with hydrogen, heat treatment, deodorization, washing with water, treatment with alkali, demetallization, distillation, solid removal, decolorization, and any combination thereof.

[0069] Contaminating metals can be removed from the feedstock, for example, by treatment with inorganic acids. Most phosphorus, present as phosphates, can be removed by degumming. Triglycerides can also be pre-hydrogenated (pretreated with hydrogen). This reduces not only the amount of oxygenated compounds (HDO), but also the levels of unsaturation, sulfur, and nitrogen (HDS, HDN). Solid feedstocks, such as fats, should be liquefied, for example, by heating, before hydrodeoxygenation. Pretreatment of solid feedstocks can further include one or more of the following: grinding, stirring, filtering, and ultrasonic treatment. The feedstock can be further decolorized and / or deodorized.

[0070] Pretreatment may be selected from heat treatment followed by optional evaporation of volatiles; heat treatment with an adsorbent (HTA), optionally followed by flash evaporation; degumming; and decolorization. According to one embodiment, pretreatment includes any one, any combination, or all of the following steps: degumming, chemical treatment, water washing, demetallization, decolorization, complete (or partial) hydrogenation, acid gas removal, and / or dehydration. The pretreatment also typically includes steps for removing impurities from the feedstock, including any suitable steps for removing solids from a liquid, including filtration, centrifugation, and precipitation; and removing volatiles from a liquid, for example, by evaporation. In the pretreatment, the feedstock comprising organic material of biological origin as previously defined is purified and a purified feedstock is obtained.

[0071] In one embodiment, pretreatment is selected from heat treatment, which optionally followed by evaporation of the evaporator, thereby heating the feedstock at a temperature of 80°C to 325°C, preferably 180°C to 300°C, more preferably 200°C to 280°C, for a residence time of 1 minute to 300 minutes. Following heat treatment may be an evaporation step, in which compounds, particularly those containing silicon and phosphorus, are removed. Examples of heat treatment of feedstocks containing organic materials can be found in WO 2020 / 016405. Filtration may also follow heat treatment, as an addition to or alternative to evaporation. When the feedstock contains brown oils or acidified soaps, pretreatment typically includes heat treatment with or without a filter aid (adsorbent), followed by filtration and, possibly, decolorization.

[0072] In one embodiment, the pretreatment is selected from heat treatment with an adsorbent (HTA), optionally followed by flash evaporation. HTA is particularly suitable as a pretreatment when the feedstock contains CTO and / or TOP, but HTA is also suitable for other feedstocks. Heat treatment with an adsorbent (HTA) can be carried out at temperatures from 180°C to 325°C, preferably from 200°C to 300°C, more preferably from 240°C to 280°C, optionally in the presence of an acid. The adsorbent can be selected from aluminum silicate, silica gel, and mixtures thereof, and is typically added in amounts from 0.1 wt.-% to 10 wt.-%, for example, 0.5 wt.-%. Examples of HTA can be found in WO 2020 / 016410.

[0073] In one embodiment, pretreatment is selected from decolorization. Decolorization can be carried out by adding acid in an amount of 500 to 5000 ppm based on the feed. The decolorization treatment can be carried out at a temperature of 60°C to 90°C and includes a drying step at 110°C to 130°C. Decolorization is completed by a filtration step to remove the solids formed and any possible filter aids. In one example, decolorization includes the following sequence

[0074] (1) Add 1000-4000 ppm citric acid (50 wt.-% water) at 85°C for 10 minutes; (2) Add 0.1-1 wt.% of adsorbent / filter aid at 85°C, 800 mbar, for 20 minutes; (3) Dry at 120°C, 80 mbar, for 25 minutes; (4) Filter at 120°C and 2.5 bar.

[0075] Both heat treatment (HT) and heat treatment with adsorbent (HTA) can be carried out under pressure, ranging from 500 kPa to 5000 kPa. Furthermore, water can be added up to 5 wt.% (e.g., 1-3 wt.%) before or during HT and HTA. Evaporation, such as flash evaporation, can be carried out after HT or HTA or any other pretreatment stage and can be performed at approximately 160°C, such as from 150°C to 225°C, under pressures ranging from 10 mbar to 100 mbar.

[0076] In one embodiment, the pretreatment includes heat treatment (HT) and decolorization.

[0077] In one embodiment, the pretreatment includes heat treatment (HT) with alkali addition and decolorization.

[0078] In one embodiment, the pretreatment includes heat treatment with adsorption (HTA), followed by flash evaporation (removing light components such as those containing Si components by evaporation) and decolorization.

[0079] In one embodiment, the pretreatment includes mixing the feedstock with water and a metal reactant, and then hydrothermally purifying the mixture, wherein heat, pressure, and turbulence induce a reaction with inorganic impurities, resulting in salt formation. The salt can then be separated and removed from the organic phase of the feedstock.

[0080] In addition, pretreatment may include or may not include additional steps such as solid removal (using techniques such as centrifugation or filtration) before and / or after HT or HTA, water washing, degumming, hydrolysis, distillation, strong acid treatment, secondary decolorization, or any combination of the above methods.

[0081] Properly purified feedstocks, obtained through pretreatment, extend catalyst lifetime in hydrodeoxygenation and subsequent hydroisomerization reactions.

[0082] Pretreated renewable feedstocks can undergo hydrotreating to remove oxygen (hydrodeoxygenation, HDO), sulfur (hydrodesulfurization, HDS), nitrogen (hydrodenitrification, HDN), and halogens (hydrodehydrohalogenation, HDX). Furthermore, some compounds, such as aromatics and possible double bonds, can also be removed via hydrotreating. Several methods exist for hydrotreating feedstocks.

[0083] In a preferred embodiment, the renewable feedstock comprising animal fats, vegetable oils, waste and / or residual materials is first pretreated to a purity level suitable for guiding the feedstock to hydrodeoxygenation, so as to remove or deplete heteroatoms and other impurities using a hydrodeoxygenation catalyst. The hydrodeoxygenation of renewable oxygenated hydrocarbons is carried out under reaction conditions including one or more of the following: a. Temperatures ranging from 250°C to 400°C, preferably from 280°C to 380°C, and more preferably from 300°C to 360°C. b. Pressure in the range of 10 bar to 200 bar, preferably from 20 bar to 100 bar, and more preferably from 20 bar to 80 bar. c. Depending on hydrogen consumption, at 0.25 h -1 up to 3.0 h -1 , preferably 0.5 h -1 up to 3.0 h -1 More preferably 0.7 h -1 Up to 2.5 h -1 Optimal choice 1.0 h -1 Up to 2.0 h -1 Heavy space velocity (WHSV) within the range. d. H2 flow rate in the range of 350 to 1500 NL H2 / L feed, preferably 350 to 1100 NL H2 / L feed, and most preferably 350 to 1000 N-L H2 / L feed, where NL H2 / L represents the standard liter of hydrogen per liter of feed to the HDO reactor, and e. A hydrodeoxygenation catalyst selected from Pd, Pt, Ni, Co, Mo, Ru, Rh, W or any combination thereof supported on a support, preferably Ni, Co, Mo and W supported on a support.

[0084] According to one embodiment, the hydrodeoxygenation catalyst is selected from CoMo, NiMo, NiW and CoNiMo supported on a support, wherein the support is preferably alumina and / or silica.

[0085] According to a specific embodiment, the hydrodeoxygenation reaction conditions include a temperature in the range of 250°C to 400°C, a pressure in the range of 20 bar to 80 bar, and a WHSV of 0.5 h. -1 Up to 3 hours -1 Within the range, and the H2 flow rate is 350 -1 500 NL H2 / L feed, and hydrodeoxygenation catalyst.

[0086] The hydrodeoxygenation reaction produces a hydrodeoxygenated effluent, which is further processed by gas-liquid separation to produce a gas stream and a liquid hydrodeoxygenated effluent containing at least 90 wt.% alkanes.

[0087] Therefore, a liquid hydrotreating effluent containing at least 90 wt.% alkanes is obtained. This effluent meets the purity requirements of the hydroisomerization feed of the present invention. In embodiments, the hydrodeoxygenation liquid stream derived from renewable feedstock contains at least 92 wt.% of the total hydrocarbon weight, more preferably at least 95 wt.% and most preferably at least 99 wt.% alkanes. The amount of n-alkanes can be high, preferably greater than 85 wt.% and more preferably greater than 90 wt.% (e.g., 95 wt.%), especially when NiMo / Al₂O₃ is used as the hydrodeoxygenation catalyst for most feedstocks.

[0088] The production of synthetic hydrocarbons from carbon dioxide and hydrogen typically involves the indirect conversion of gases into syngas, a mixture of carbon monoxide and hydrogen. Syngas can be prepared by converting organic carbonaceous materials into a mixture of carbon monoxide and hydrogen with some carbon dioxide separated from the syngas at high temperatures (>700°C) without combustion, using controlled amounts of oxygen and / or steam. This method is well known in the art.

[0089] In this embodiment, the syngas is prepared from hydrogen and carbon dioxide via a reverse water-gas shift (rWGS) reaction. According to a preferred embodiment, the hydrogen used in this method is green hydrogen produced from renewable energy sources (such as solar energy) to power the electrolysis of water, and the carbon dioxide is CO2 captured from industrial renewable processes. These methods are well known in the art.

[0090] If the syngas contains impurities derived from the feedstock, such as carbon dioxide, methane, water, nitrogen, hydrogen sulfide, ammonia, hydrogen chloride, tar, and small particles such as ash and soot, the syngas can be purified to make it suitable for hydrocarbon synthesis. The purified syngas preferably has a hydrogen to carbon monoxide molar ratio of 2.5:1 to 0.5:1, more preferably 2.1:1 to 1.8:1, and more preferably about 2:1.

[0091] Syngas can be further converted into hydrocarbons using appropriate conversion methods, such as oligomerization methods, like Fischer-Tropsch (FT) synthesis, methanol synthesis (MtJ), or any alternatives thereof. The Fischer-Tropsch (FT) and alcohol-to-jet fuel (AtJ) pathways are currently accepted by the ASTM D7566 jet fuel standard and allow for the production of aviation fuels.

[0092] In this embodiment, the syngas is further converted into liquid hydrocarbons using the Fischer-Tropsch (FT) process. The FT process occurs in the presence of a metal catalyst, typically at temperatures of 150–300°C and pressures of one to several tens of atmospheres. This method is well known in the art. Typical FT effluents comprise at least 50 wt.% hydrocarbons boiling at atmospheric pressure above 370°C, and typically have at least 60 wt.% alkane content, less than 1 wt.% aromatic compounds, less than 2 wt.% cycloalkanes, less than 0.1 wt.% nitrogen content, and less than 0.1 wt.% sulfur content. Alkanes can be purified from aromatics and cycloalkanes. Typically, no pretreatment is required to remove residual heteroatoms.

[0093] In the method of the present invention, a fraction containing at least 90 wt.% liquid hydrocarbon alkanes is separated from the FT effluent by, for example, distillation and directed to hydroisomerization.

[0094] In one embodiment, the syngas is converted into an alcohol, such as methanol or ethanol, which further reacts to form the corresponding olefin. The olefin, such as C2-C4 olefins, can be oligomerized—i.e., dimerized, trimerized, tetramerized, or co-oligomerized—using a suitable heterogeneous or homogeneous catalyst to form olefins of the desired carbon length. Typically, the olefin is then subsequently hydrogenated to an alkane of the corresponding carbon chain length.

[0095] The effluent from the refining step can be further purified before being directed to hydroisomerization. Typically, purification involves subjecting the refining process effluent to gas-liquid separation, i.e., removing gases such as carbon monoxide, carbon dioxide, water, possibly hydrogen sulfide, ammonia, and low-boiling hydrocarbons from the liquid hydrocarbon stream. In gas-liquid separation, the refining process effluent is separated into gaseous and liquid streams; this separation can be achieved through a stripping step, distillation, or flash evaporation.

[0096] The resulting feed stream, directed to hydroisomerization, is primarily in liquid form.

[0097] In one embodiment, the liquid alkane stream is obtained from syngas via FT conversion at 150-300°C and 1-40 bar in the presence of an Fe or Co-based catalyst.

[0098] In this embodiment, the liquid alkane stream is obtained from syngas via an olefin oligomerization route over an acidic catalyst.

[0099] According to another aspect, the present invention relates to the use of a catalyst comprising an active metal selected from noble metals, nickel, and any combination thereof, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica, wherein the SiO2 / Al2O3 molar ratio of the EU-2 zeolite is from 10 to 100, preferably from 15 to 85, for example from 40 to 80, and wherein the content of the active metal in the catalyst is from 0.1 wt% to 7.0%. wt.-%, used for the hydroisomerization of liquid alkanes at temperatures from 270°C to 370°C, at pressures from 1 bar to 100 bar, preferably from 20 bar to 100 bar, more preferably from 20 bar to 90 bar, for example from 20 bar to 60 bar, at 270-324°C, preferably 270-320°C, more preferably 280-320°C, under an H2 stream used to regulate the product distribution of the hydroisomerization reaction to primarily produce diesel fuel or components thereof, and at 330-370°C, preferably 336-370°C, more preferably 336-360°C, primarily producing jet fuel or components thereof.

[0100] The H2 flow rate is preferably 100-800 N-L H2 / L, more preferably 200-600 N-L H2 / L.

[0101] Preferably, EU-2 zeolite further comprises one or more of the following characteristics: Crystallinity is 50% to 95%, measured by X-ray diffraction (XRD) according to ASTM D5758-01 (2021). BET has a specific surface area of ​​180m². 2 / g to 450m 2 / g, for example 200m 2 / g to 300m 2 / g, determined by nitrogen physisorption. The acidity ranges from 80 μmol / g to 700 μmol / g, preferably from 150 μmol / g to 500 μmol / g, and more preferably from 200 μmol / g to 400 μmol / g, for example from 350 μmol / g to 400 μmol / g, as measured by pyridine-FTIR. The ratio of Brønsted acid sites to Lewis acid sites ranged from 0.5 to 20, as measured by pyridine-FTIR, and Crystalline zeolite particles are basically needle-shaped particles.

[0102] experiment

[0103] The physicochemical properties of the hydroisomerization catalysts are shown in Table 2. Commercially available Pt-impregnated SAPO-11-based catalysts were used as a reference.

[0104] Table 2. Physicochemical properties based on EU-2 (with 0.5 wt.-% Pt and no support), and a reference catalyst.

[0105]

[0106] Isomerization reactions of fresh catalysts were tested using a pretreatment and hydrodeoxygenation zone feed derived from a mixture of animal fats and vegetable oils, and the catalysts were passivated prior to use. Samples were: (i) EU-2-based zeolite impregnated with 0.5 wt.% Pt on an alumina support; and (ii) a reference catalyst. The process parameters used are summarized below: Drying: 125°C, 8 h, N2 flow Reduction: 370°C, 2 h, 40 bar, H2 flow Wetting: 150°C, 2 h, 40 bar, H2 flow Passivation: 150°C, 2 h, 40 bar, H2 flow, along with renewable alkanes and 0.2 wt.% tributylamine (TBA). Stabilization and reaction: 40 bar, H2 flow rate, LHSV 1.4 h -1 A 1.5 mL catalyst (75–150 µm) with an H2 / oil ratio of 300 NL / L was diluted with SiC F100 (106–150 µm) at a volume ratio of 1:1.

[0107] Liquid alkane feed at 50°C has a yield of 758.3 kg / m³. 3 Its density and cloud point at 20°C.

[0108] Renewable alkanes were hydroisomerized at different temperatures using both Pt-impregnated commercial catalysts and Pt-impregnated EU-2-based catalysts. wt.-% yields suitable for use with jet fuels, diesel fuels, or portions thereof at different hydroisomerization temperatures are collected in Table 3.

[0109] Table 3

[0110] As can be seen from the table, across the entire tested hydroisomerization temperature range, hydroisomerization using the EU-2-based catalyst produced significantly more jet fuel-range hydrocarbons and their components than the commercial reference catalyst. Furthermore, hydroisomerization using the commercial reference catalyst produced diesel-suitable hydrocarbons or their components as the main products, while EU-2 allows for selection of the main products by adjusting the hydroisomerization temperature.

[0111] Figure 2 The figure shows the carbon number distribution of hydroisomerization of alkane feedstocks using the commercially available reference catalyst and EU-2-based catalyst of the present invention at different temperatures. As can be clearly seen, the catalyst of the present invention allows for the adjustment of hydroisomerization reaction conditions to favor the formation of hydrocarbons suitable for use as components of jet fuels, simply by adjusting the reaction temperature.

[0112] Figure 3 and Figure 4 The yields of hydrocarbons boiling at atmospheric pressure in different temperature ranges via hydroisomerization using either an EU-2-based catalyst or a commercial reference catalyst are shown, respectively, as the hydroisomerization temperature varies. As illustrated, the product distribution using the reference catalyst is significantly less sensitive to the hydroisomerization temperature.

[0113] When hydroisomerization reactions were carried out at different temperatures and using commercially available hydroisomerization catalysts or EU-2-based catalysts as catalysts, the 1 / n ratios and branching amounts of fractions suitable for jet fuel, diesel, and their components are shown in Tables 4 and 5, respectively. Although the hydroisomerization products obtained using commercially available catalysts have higher 1 / n ratios than those obtained using EU-2-based catalysts, the EU-2-based catalysts produce more branched hydrocarbons suitable for jet fuel or its components for fractions suitable for injection across the entire tested hydroisomerization range.

[0114] Table 4. i / n ratio (wt.-% / wt.-%) and amount of branching (wt.-%), for fractions suitable for jet fuel, diesel, and their components when the hydroisomerization reaction is carried out at different temperatures and using a commercial hydroisomerization catalyst.

[0115]

[0116] Table 5. i / n ratio (wt.-% / wt.-%) and amount of branching (wt.-%) for fractions suitable for jet fuel, diesel and its components when hydroisomerization reaction is carried out at different temperatures and using EU-2 based hydroisomerization catalysts.

[0117]

[0118] Regarding the diesel produced, when hydroisomerization is carried out at temperatures of 330°C or below, the product obtained using the EU-2-based catalyst has a better i / n ratio and a higher degree of branching compared to the product obtained using a commercial catalyst.

[0119] Figure 5 The cloud point of the liquid product samples from the tested catalysts is shown. For all temperature ranges, the zeolite-containing catalyst based on EU-2 produced liquid products with lower cloud points than those obtained with the commercial reference catalyst. From T>325°C, the difference in cloud point values ​​is very significant, which is related to the formation of C4-C9. For example, at 340°C, the product from the EU-2-based catalyst has a cloud point of approximately -80°C, close to the detection limit, while the product from hydroisomerization with the commercial reference catalyst has a cloud point of -40°C.

[0120] Figure 6 and Figure 7 Exemplary pour points (PP) and freezing points of liquid products obtained using EU-2 zeolite and a commercially available reference catalyst as hydroisomerization catalysts are shown. The data confirm that the EU-2-based catalyst is advantageous for forming liquid products with improved cold properties. For PP, for example, at 330°C, the product from the EU-2-based catalyst has a pour point of approximately -81°C, close to the detection limit, while the product from the commercial reference catalyst has a pour point of -65.8°C.

Claims

1. A method for producing a transport fuel comprising jet fuel, diesel fuel, or components thereof, the method comprising the following steps: a) Provide a pretreated liquid feed comprising at least 90 wt.% alkanes; b) The feed is subjected to a hydroisomerization reaction at a pressure of 1 bar to 100 bar, preferably 20 bar to 100 bar, more preferably 20 bar to 90 bar, for example 20 bar to 60 bar, in the presence of a hydrogen stream and a hydroisomerization catalyst comprising an active metal selected from noble metals, nickel, and any combination thereof, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica, wherein the active metal content in the catalyst is from 0.1 wt.-% to 7.0 wt.-%, and wherein the SiO2 / Al2O3 molar ratio of the EU-2 zeolite is from 10 to 100, preferably from 15 to 85, for example from 40 to 80, and The hydroisomerization reaction temperature is adjusted between 270°C and 370°C to provide the desired hydroisomerized hydrocarbon composition, wherein i. For hydrocarbons suitable for use as jet fuel or components thereof, and hydrocarbons suitable for use as diesel fuel or components thereof, the weight ratio is greater than 1, and is adjusted to 330°C to 370°C, preferably 336°C to 370°C, more preferably 336°C to 360°C; as well as ii. For hydrocarbons suitable for use as diesel fuel or components thereof, the weight ratio of hydrocarbons suitable for use as jet fuel or components thereof is greater than 1, the temperature is adjusted to be from 270°C to 324°C, preferably from 270°C to 320°C, more preferably from 280°C to 320°C; and c) By separation, recover hydrocarbons suitable for use as jet fuel or components thereof as major products from the desired hydroisomerization stream; or hydrocarbons suitable for use as diesel fuel or components thereof.

2. The method according to claim 1, wherein, The EU-2 zeolite further includes one or more of the following characteristics: Crystallinity is 50% to 95%, measured by X-ray diffraction (XRD) according to ASTM D5758-01 (2021). BET has a specific surface area of ​​180m². 2 / g to 450m 2 / g, for example 200m 2 / g to 300m 2 / g, determined by nitrogen physisorption. Acidity ranges from 80 µmol / g to 700 µmol / g, preferably from 150 µmol / g to 500 µmol / g, more preferably from 200 µmol / g to 400 µmol / g, for example from 350 µmol / g to 400 µmol / g, measured by pyridine-FTIR. The ratio of Brønsted acid sites to Lewis acid sites ranged from 0.5 to 20, as measured by pyridine-FTIR, and The crystalline EU-2 zeolite particles are basically needle-shaped.

3. The method according to claim 1 or 2, wherein, The pretreated liquid feed contains no more than 1 w-ppm, preferably no more than 0.5 w-ppm, alkali metal and alkaline earth metal impurities, calculated as elemental alkali metals and alkaline earth metals; 1 w-ppm, preferably no more than 0.5 w-ppm, other metals, calculated as elemental metals; Nitrogenous impurities of 5 w-ppm, preferably no more than 1 w-ppm, more preferably no more than 0.2 w-ppm, calculated as elemental nitrogen; 5 w-ppm, for example, phosphorus-containing impurities not exceeding 1 w-ppm, are calculated as elemental phosphorus; 1 w-ppm silicon impurities, calculated as elemental silicon; Sulfur-containing impurities of 10 w-ppm, preferably no more than 5 w-ppm, more preferably no more than 1 w-ppm, and most preferably no more than 0.4 w-ppm, calculated as elemental sulfur; Chlorine-containing impurities of 10 w-ppm, preferably no more than 5 w-ppm, calculated as elemental chlorine.

4. The method according to any one of claims 1 to 3, wherein, The hydroisomerization temperature is adjusted between 330°C and 370°C, preferably between 336°C and 370°C, and more preferably between 336°C and 360°C, to produce a hydroisomerization stream in which the weight ratio of hydrocarbons suitable for use as jet fuel or components thereof to hydrocarbons suitable for use as diesel fuel or components thereof is greater than 1, and at least a fraction boiling from 107°C to 280°C at atmospheric pressure (1 bar (absolute pressure)) is separated from the hydroisomerization stream, thereby recovering jet fuel or components thereof.

5. The method according to any one of claims 1 to 3, wherein, The hydroisomerization temperature is adjusted between 270°C and 324°C, preferably between 270°C and 320°C, and more preferably between 280°C and 320°C, to produce a hydroisomerization stream in which the weight ratio of hydrocarbons suitable for use as diesel fuel or components thereof to hydrocarbons suitable for use as jet fuel or components thereof is greater than 1, and at least a fraction with a boiling point of 170°C to 360°C at atmospheric pressure (1 bar (absolute pressure)) is separated from the hydroisomerization stream, thereby recovering diesel fuel or components thereof.

6. The method according to any one of claims 1 to 5, wherein, In step b), the H2 flow rate is 100 to 800 N-LH2 / L feed.

7. The method according to any one of claims 1 to 6, wherein, The active metal is platinum, palladium, or rhodium, the active metal is impregnated on the support, and the active metal content of the hydroisomerization catalyst is from 0.4 wt.-% to 0.6 wt.-% of the catalyst, for example about 0.5 wt.-%.

8. The method according to any one of claims 1 to 7, wherein, Step a) includes i. Provide renewable raw materials ii. Pre-treat the renewable raw material to reduce the amount of impurities therein, so that the renewable raw material is free from: alkali metal and alkaline earth metal impurities greater than 10 w-ppm (calculated as elemental alkali metals and alkaline earth metals); other metals greater than 10 w-ppm (calculated as elemental metals); nitrogen-containing impurities greater than 1000 w-ppm (calculated as elemental nitrogen); phosphorus-containing impurities greater than 30 w-ppm (calculated as elemental phosphorus); and silicon-containing impurities greater than 5 w-ppm (calculated as elemental silicon); to produce the pre-treated renewable raw material. iii. Subjecting the pretreated renewable feedstock to a hydrodeoxygenation reaction to produce a hydrodeoxygenated effluent, wherein the hydrodeoxygenation reaction comprises one or more of the following: a. Temperatures in the range of 250°C to 400°C, preferably 260°C to 380°C, more preferably 280°C to 360°C, such as 300°C to 330°C. b. Pressure in the range of 10 bar to 200 bar, preferably from 20 bar to 100 bar, and more preferably from 20 bar to 80 bar. c. From 0.25 h -1 Up to 3 hours -1 Preferred from 0.5 h -1 up to 3.0 h -1 More preferably from 0.7 h -1 Up to 2.5 h -1 The optimal choice is from 1.0 h -1 Up to 2.0 h -1 WHSV within the range, d. An H2 stream with a feed rate of 350 to 1500 NL H2 / L, preferably 350 to 1100 NL H2 / L, and more preferably 350 to 1000 NL H2 / L. e. A hydrodeoxygenation catalyst on a support, said hydrodeoxygenation catalyst being selected from Pd, Pt, Ni, Co, Mo, Ru, Rh, and W or any combination thereof, to produce a hydrodeoxygenation stream, and iv. Pass the hydrodeoxygenated stream through a gas-liquid separator to produce a gaseous stream and the pretreated liquid feed containing at least 90 wt.% alkanes.

9. The method of claim 8, wherein, based on the total weight of the hydrocarbon products, the hydrodeoxygenation stream comprises at least 92 wt.-%, preferably at least 95 wt.-%, more preferably at least 99 wt.-%, of alkanes.

10. The method according to any one of claims 1 to 7, wherein, Step a) includes i. Provide raw materials containing CO2 and H2; ii. Convert the raw materials into syngas; iii. Upgrading syngas into hydrocarbons via oligomerization, preferably via Fischer-Tropsch synthesis or methanol synthesis, to produce upgraded effluent. iv. Performing gas-liquid separation on the improved effluent to produce a gas stream and a liquid effluent; and v. Separating a feed containing at least 90 wt.% alkanes from the liquid effluent.

11. Use of a catalyst in the hydroisomerization of liquid alkanes, said catalyst comprising an active metal selected from noble metals, nickel, and any combination thereof, EU-2 zeolite, and a support selected from alumina, silica, and alumina-silica, wherein the content of said active metal in the catalyst is from 0.1 wt% to 7.0 wt%. The EU-2 zeolite, with a SiO2 / Al2O3 molar ratio of 10 to 100, preferably 15 to 85, such as 40 to 80, is subjected to hydroisomerization at a temperature of 270°C to 370°C and a pressure of 1 bar to 100 bar, preferably from 20 bar to 100 bar, more preferably from 20 bar to 90 bar, for example from 20 bar to 60 bar, under an H2 flow to adjust the product distribution of the hydroisomerization reaction to primarily produce diesel fuel or its components at 270-324°C, preferably at 270-320°C, more preferably at 280-320°C, and primarily produce jet fuel or its components at 330-370°C, preferably at 336-370°C, more preferably at 336-360°C.

12. The use according to claim 11, wherein the EU-2 zeolite further comprises one or more of the following characteristics: Crystallinity is 50% to 95%, measured by X-ray diffraction (XRD) according to ASTM D5758-01 (2021). BET has a specific surface area of ​​180m². 2 / g to 450m 2 / g, for example 200m 2 / g to 300m 2 / g, determined by nitrogen physisorption. Acidity ranges from 80 µmol / g to 700 µmol / g, preferably from 150 µmol / g to 500 µmol / g, more preferably from 200 µmol / g to 400 µmol / g, for example from 350 µmol / g to 400 µmol / g, measured by pyridine-FTIR. The ratio of Brønsted acid sites to Lewis acid sites ranged from 0.5 to 20, as measured by pyridine-FTIR, and The crystalline EU-2 zeolite particles are basically needle-shaped.

13. The use according to claim 11 or 12, wherein the H2 flow is a feed of 100 to 800 N-LH2 / L, preferably 200 to 600 N-LH2 / L.

Images