METHOD FOR MANUFACTURED JET FUEL FROM RENEWABLE FUELS

Abstract

METHOD FOR MANUFACTURING A JET FUEL FROM RENEWABLE FEEDS The invention relates to a method for manufacturing a jet fuel comprising at least the steps of: a) subjecting a hydrocarbon feed comprising a hydrocarbon component of fossil origin to a hydrotreating step and obtaining a hydrotreated hydrocarbon feed; b) fractionating the hydrotreated hydrocarbon feed obtained in step a) and recovering a kerosene fraction as jet fuel, said kerosene fraction having a final boiling point less than or equal to 300 °C, the method being characterized in that the hydrocarbon feed subjected to hydrotreating step a) further comprises a renewable component comprising a diesel fraction of a hydrotreated oil, the renewable component representing at most 10% by volume of the total volume of the hydrocarbon feed.

Description

Title of the invention: METHOD FOR MANUFACTURED JET FUEL FROM RESOURCED FUELS NEW technical field

[0001] The present invention relates to the technical field of refining petroleum feedstocks of fossil origin and feedstocks of biological origin, particularly for the manufacture of jet fuel. More specifically, the invention relates to a process for obtaining jet fuel having a component of biological (or renewable) origin. Context of the invention

[0002] Conventional jet fuels, also called "jet fuel" or "kerosene," are produced from crude oil and contain a complex mixture of hydrocarbons that typically have 6 to 18 carbon atoms. These hydrocarbons include linear and branched alkanes, cycloalkanes, and aromatic hydrocarbons. The cutting points of the jet fuel fraction typically range from 140 °C to 240 °C.

[0003] A commercial jet fuel is typically obtained by blending different fuel bases. These fuel bases may be crude oil distillation fractions, possibly hydrotreated or sometimes subjected to a softening treatment (e.g., the MEROX process). These bases may also be fractions of a hydrocracker effluent or a catalytic cracker effluent (often after hydrotreatment). Other fuel bases may be prepared by other methods, such as Fischer-Tropsch synthesis followed by a cracking step. The choice of fuel bases and their relative proportions is made so that the final properties of the blend meet the required specifications.

[0004] Due to the depletion of fossil resources and growing environmental concerns, the use of molecules derived from biomass is increasingly sought after to replace fossil-based molecules. However, the preparation of jet fuel from biomass-derived molecules that can be directly used in jet fuel formulations represents a significant economic and environmental challenge. In particular, some countries, such as France, are implementing incentive taxes related to the incorporation of renewable energy in transportation, especially in the aviation sector. Previous art

[0005] A solution for obtaining jet fuel having a component of origin Biological aviation fuel blending involves mixing conventional jet fuel with a paraffinic base derived from renewable feedstocks as defined by ASTM D7566-21, thus enabling the production of alternative aviation fuels. Renewable feedstock aviation fuel bases that can be blended with fossil jet fuel are • Synthetic paraffinic kerosenes [SPK], produced from processes such as the Fischer-Tropsch process, the hydrotreating of esters and fatty acids [HEFA-SPK], or produced by the Alcohol-to-jet process (transformation of alcohol into kerosene) [ATJ-SPK], • Synthetic isoparaffins produced by hydrotreating fermented sugars [SIP-HFS], • Synthetic aromatic kerosenes obtained by alkylation of light aromatics from non-petroleum sources [SPK / A], • Synthetic kerosenes obtained from the hydrothermal conversion of fatty acid esters and fatty acids, • Synthetic paraffinic kerosenes [SPK] obtained from hydrotreated hydrocarbons, esters and fatty acids.

[0006] This solution, however, requires specific processing facilities to produce the paraffinic bases that will be mixed in the conventional jet.

[0007] Another solution is to co-treat a hydrocarbon of fossil origin with a feedstock of renewable origin, as provided for in particular in the ASTM D1655-21C standard.

[0008] Thus, document EP2346962 describes a process for obtaining a kerosene fraction, a portion of which is of biological origin. To this end, a petroleum-based feedstock mixed with a biological feedstock is subjected to a hydrotreating step and then fractionated to recover a kerosene fraction. The biological feedstock used is an animal oil and / or fat, or a mixture of these oils / fats. The oils and / or fats used are not transesterified or hydrotreated.

[0009] However, there is still a need for a process for manufacturing jet fuel with a biological component by co-treatment in a hydrotreating unit without modification of the process. Description of the invention

[0010] The invention proposes a method for manufacturing jet fuel comprising at least the steps of:

[0011] a) subject a hydrocarbon feed comprising a hydrocarbon component of fossil origin to a hydrotreating step and obtain a hydrotreated hydrocarbon feed; b) fractionate the hydrotreated hydrocarbon feed obtained in step a) and recover a kerosene fraction as jet fuel, said kerosene fraction having a final boiling point of less than or equal to 300 °C, measured in particular according to ASTM D86-12.

[0012] According to the invention, the hydrocarbon feed subjected to step a) of hydrotreating further comprises a component of renewable origin comprising a diesel fraction of a hydrotreated oil, the component of renewable origin representing at most 10% by volume of the total volume of the hydrocarbon feed.

[0013] The process according to the invention thus makes it possible to obtain aviation fuel, a portion of which is of renewable origin, also called SAF for "Sustainable Aviation Fuel". Furthermore, by using a diesel fraction of a hydrotreated oil, the process according to the invention makes it possible to valorize these diesel fractions for the manufacture of new fuels other than diesel engine fuels.

[0014] In particular, the process according to the invention can be implemented in existing hydrotreatment units. Detailed description of the invention

[0015] The terms "including" and "includes" as used herein are synonymous with "including", "includes" or "contains", "containing", and are inclusive or boundless and do not exclude additional features, elements or unspecified method steps.

[0016] The expressions % by weight and % by mass have an equivalent meaning and refer to the proportion of the mass of a product relative to 100g of a composition comprising it.

[0017] As used herein, "carbon number" or "Cn", where "n" is an integer, describes a hydrocarbon or molecule in which "n" denotes the number of carbon atoms, regardless of linearity or branching. Ranges of carbon atom numbers (e.g., C6 to C18, or C19+) refer to molecules having carbon atom numbers within the specified range (from 6 to 18 carbon atoms or 19 or more carbon atoms), including the extreme members of the range. However, it is not necessary for every carbon number within a range to be represented in the molecules described.

[0018] Carbon number distributions are determined by the actual boiling point distribution and by gas chromatography. As used in this specification, the total amount of normal-paraffins and isoparaffins at a given carbon number is determined by the ASTM D-5442 analysis of petroleum waxes by gas chromatography ("GC") or by an equivalent gas chromatography method. For example, the procedure described in the previous part may be carried out as described in the previous part. blication: Marko R. Djokic et al. Quantitative analysis of crude and stabilized bio-oils by comprehensive two-dimensional gas-chromatography. Journal of Chromatography A, 1257 (2012) ppl31-140.

[0019] Boiling points as mentioned herein are measured at atmospheric pressure, unless otherwise specified. An initial boiling point is defined as the temperature at which the first vapor bubble forms. A final boiling point is the highest temperature attainable during distillation. At this temperature, no more vapor can be transported to a condenser. The determination of the initial and final boiling points relies on techniques known in the trade, and several methods adapted according to the distillation temperature range are applicable, for example, NF EN 15199-1 (2020 version) or ASTM D2887-19 for measuring the boiling points of petroleum fractions by gas chromatography, ASTM D7169-05 for heavy hydrocarbons, ASTM D7500-15 (2019), D86-12, or DI 160-18 for distillates.

[0020] The density of a jet fuel type hydrocarbon can be measured according to ASTM D4052-18.

[0021] The cloud point of a hydrocarbon effluent of biological origin can be measured according to ASTM D2500-17a.

[0022] The content of aromatic compounds and naphthenes can be determined by gas chromatography (GcxGC reversed phase or by GC according to method UOP744). Fossil-derived hydrocarbon component

[0023] The fossil-based hydrocarbon component used in the present invention comprises fossil-based hydrocarbons. In one embodiment, the fossil-based hydrocarbon component may consist of fossil-based hydrocarbons. In this case, it does not comprise components of renewable origin.

[0024] Fossil-derived hydrocarbons usable in the present invention can advantageously be chosen from kerosene fractions.

[0025] In a preferred embodiment, the fossil-derived hydrocarbon component is a fossil-derived kerosene cut or a mixture of fossil-derived kerosene cuts.

[0026] A kerosene cut of fossil origin has boiling points ranging from 130 °C to 300 °C. It typically has an initial boiling point according to ASTM D86-12 of 130 to 160 °C and a final boiling point according to ASTM D86-12 of 220 °C to 300 °C.

[0027] These kerosene cuts can be:

[0028] - a kerosene cut obtained from the direct distillation of crude oil,

[0029] - a kerosene fraction obtained from various conversion processes such as cracking catalytic, hydrocracking and / or viscoreduction.

[0030] In the context of hydrotreating, the fossil-based hydrocarbons are advantageously a kerosene fraction or a mixture of kerosene fractions, preferably from the direct distillation of crude oil or from hydrocracking. Components of renewable origin

[0031] According to the invention, the hydrocarbon feedstock subjected to hydrotreating step a) comprises a renewable component comprising, or consisting of, a diesel fraction of a hydrotreated oil. In one embodiment, the hydrocarbon feedstock may optionally further comprise another renewable component comprising, or consisting of, alkyl esters of fatty acids, in particular methyl and / or ethyl esters of fatty acids.

[0032] By renewable origin component, we mean a component totally free of components of mineral or fossil origin.

[0033] The process according to the invention can thus include, upstream of step a) of hydrotreating, an initial step a1) of supplying a component of renewable origin comprising a diesel fraction of a hydrotreated oil, and optionally an initial step of supplying a2) another component of renewable origin comprising alkyl esters of fatty acids.

[0034] The supply step a1) may include:

[0035] - at least one step (i) of hydrotreating one or more oils of origin natural for producing hydrotreated oil,

[0036] - an optional step (ii) of isomerizing the hydrotreated oil to produce a hydrotreated and isomerized oil,

[0037] - an optional step of fractionating the hydrotreated oil or the hy oil hydrotreated and isomerized to recover a diesel fraction from a hydrotreated oil and / or an optional step of blending several diesel fractions from a hydrotreated oil,

[0038] The supply step a2) may include:

[0039] - a step (iii) of transesterification of one or more oils of natural origin with an alcohol to provide a renewable source component comprising alkyl esters of fatty acids.

[0040] These different steps are detailed below.

[0041] Component of renewable origin comprising a diesel fraction of a hydrotreated oil

[0042] The first renewable component used in the present invention comprises, or is made up of, a diesel fraction of a hydrotreated oil.

[0043] This diesel fraction of a hydrotreated oil is typically obtained by hydro (i) treatment of a natural oil or a mixture of natural oils, generally carried out in the presence of dihydrogen and at least one catalyst, to convert fatty acid esters and free fatty acids contained in a natural oil or a mixture of natural oils into linear or substantially linear paraffins. The diesel fraction of a hydrotreated oil may also be a mixture of diesel fractions of hydrotreated oils, each derived from the hydrotreatment of one or more natural oils.

[0044] A naturally sourced oil is defined as an oil that does not contain mineral oil of fossil origin.

[0045] Typically, an oil of natural origin may contain 50% or more, 60% or more, preferably 70% or more, of phenolic lipids, fatty acids and / or fatty acid esters (mono-, di-, triglycerides).

[0046] Typically, a naturally derived oil may contain fatty acid esters (mono-, di- or triglycerides) and / or free fatty acids, containing one to three C8-C24 acyl groups, saturated or unsaturated. When several acyl groups are present, they may be identical or different.

[0047] The oil of natural origin may be chosen from a vegetable oil, an animal oil or fat, a used oil, an oil produced by microorganisms, animal fats and / or used cooking oils which are animal by-products, as well as mixtures thereof.

[0048] The vegetable oil may be chosen from pine oil, rapeseed oil, sunflower oil, castor oil, peanut oil, linseed oil, babassu oil, hemp oil, linola oil, jatropha oil, peanut oil, rice bran oil, mustard oil, carinata oil, coconut oil, copra oil, olive oil, palm oil, cottonseed oil, corn oil, palm kernel oil, soybean oil, pumpkin seed oil, grapeseed oil, argan oil, jojoba oil, sesame oil, walnut oil, hazelnut oil, tung oil, rice oil, safflower oil, algae oil, used oils, nut shell oil (especially cashew nut shell oil), and any combination thereof.

[0049] Used oil includes used cooking oils (used food oils) and oils recovered from wastewater, such as trap and drain grease / oils, gutter oils, sewage oils, for example from wastewater treatment plants, and used grease from the food industry.

[0050] Animal fat can be chosen from tallow, lard, fat (yellow and brown fat), fish oil / fat, milk fat.

[0051] In particular, animal fats and used cooking oils, which are animal by-products and have the status of animal by-products within the meaning of the Regulation (EC) No 1069 / 2009 of the European Parliament and of the Council of 21 October 2009 and Commission Regulation (EU) No 142 / 2011 (Regulation implementing Regulation (EC) No 1069 / 2009).

[0052] Animal fats having the status of animal by-product are fatty residues of animal origin, other than used cooking oils, coming for example from food industries or rendering plants.

[0053] Used cooking oils having the status of animal by-products are used cooking food oils (used cooking oils or UCO), namely residues of fats of vegetable or animal origin used for human consumption, in the food industry, in collective or commercial catering.

[0054] Naturally derived oil can also be oil produced by microorganisms, whether natural or genetically modified, such as bacteria, yeasts (including oleaginous yeasts), algae, prokaryotes, or eukaryotes. In particular, these oils can be recovered by well-known mechanical or chemical extraction methods.

[0055] In a preferred embodiment, this oil of natural origin can be chosen from an animal fat and / or a used oil, and in particular from an animal fat and / or a used oil having the status of waste,

[0056] The hydrotreated oil is obtained by hydrotreating (i) oil(s) of natural origin in the presence of at least one catalyst. This hydrotreating step (i) can be carried out in one or more hydrotreating reactors. Any type of reactor commonly used for this type of reaction may be used, for example, a fixed-bed reactor, a stirred-tank reactor, a bubbling-bed reactor, a slurry-type reactor, etc., preferably a fixed-bed reactor.

[0057] Hydrotreating (i) can be carried out at a temperature of 100 to 550°C in the presence of dihydrogen at pressures ranging from 0.01 to 10 MPa. The ratio between dihydrogen and feedstock can be from 100 to 2000 Nl / l.

[0058] This hydrotreatment (i) can implement one or more reactions chosen from hydrodeoxygenation, decarboxylation and decarbonylation.

[0059] Hydrodeoxygenation is preferably carried out in continuous fixed bed reactors, continuous stirred tank reactors or slurry type reactors containing a solid catalyst which can be selected from oxides or sulfides of Ni, Mo, W, Co or mixtures such as NiW, NiMo, CoMo, NiCoW, NiCoMo, NiMoW and CoMoW as a catalytic phase, preferably supported on carbon, alumina, silica, a zeolite, titanium oxide or zirconia or mixtures thereof.

[0060] Hydrodeoxygenation can be carried out at a temperature of 200 to 500°C, preferably 220 to 400°C, under a pressure of 1 MPa to 10 MPa (10 to 100 bar), by example of 6 MPa, and with a dihydrogen / oil ratio of 100 to 2000 NI H2 / l, but preferably of 350 to 1500 NI H2 / l, for example of 800 NI H2 / l of oil.

[0061] Decarboxylation and / or decarbonylation is preferably carried out in the presence of a solid catalyst in batch reactors, continuous fixed-bed reactors, continuously stirred-tank reactors, or mud reactors. Decarboxylation and / or decarbonylation can be carried out directly with glycerides, any esters, or with free fatty acids.

[0062] The catalyst can be chosen from:

[0063] - the oxides or sulphides of Ni, Mo, W, Co, NiW, NiMo, CoMo, NiCoW, NiCoMo, NiMoW and CoMoW as a catalytic phase, preferably supported on carbon, alumina, silica, titanium oxide, zirconia, zeolite or mixed supports.

[0064] - metals or alloy mixtures of group 10 (Ni, Pt and Pd) and group 11 (Cu and Ag) supported by carbon, magnesia, zinc oxide, spinels (Mg2Al2O4, ZnAl2O4), perovskites (BaTiO3, ZnTiO3), calcium silicates (such as xonotlite), alumina, silica or silica-aluminas or mixtures thereof,

[0065] - basic oxides, such as alkali metal oxides, oxides alkaline-earths, lanthanide oxides, zinc oxide, spinels (Mg2Al2O4, ZnAl2O4), perovskites (BaTiO3, ZnTiO3), calcium silicates (such as xonotlite), either in bulk or dispersed on neutral or basic supports, on basic zeolites (such as alkaline or alkaline-earth zeolites with low silica / alumina content obtained by exchange or impregnation).

[0066] For optimal performance and stable continuous operation, it is preferable that the active metallic component of the catalyst, in the case of Ni, Mo, W, Co, or mixtures, be in the form of sulfides. Therefore, it is preferable that traces of decomposable (thermally or catalytically) sulfide compounds be present or intentionally added to the feedstock to maintain the metallic sulfide in its sulfide state. By way of example, these sulfur compounds may be H₂S, COS, CS₂, mercaptans (e.g., methyl sulfide), thioethers (e.g., dimethyl sulfide), disulfides (e.g., dimethyl disulfide), thiophenic and tetrahydrothiophenic compounds.

[0067] Decarboxylation and / or decarbonylation is carried out in the presence of dihydrogen, which stabilizes the catalytic activity by removing strongly adsorbed unsaturated species (for example, when decarbonylation is the predominant reaction pathway) from the catalyst surface through hydrogen addition reactions. The presence of dihydrogen can also hydrogenate the double bonds present in the acyl portion of the fatty acid to obtain paraffinic reaction products. from the decarboxylation process.

[0068] Decarboxylation and / or decarbonylation can be carried out at a temperature of 100 to 550°C in the presence of dihydrogen at pressures ranging from 0.01 to 10 MPa. The ratio between dihydrogen and feed charge can be from 100 to 2000 Nid.

[0069] The liquid effluent produced by the hydrotreatment (i) of oil(s) of natural origin typically comprises a hydrocarbon fraction consisting essentially of n-paraffins having about 8 to about 24 carbon atoms.

[0070] Part of this hydrocarbon fraction, after separation, can be returned to the inlet of the hydrotreating, in particular upstream of a deoxygenation reaction in order to absorb the heat of reaction, dilute the remaining impurities or supply more dihydrogen in dissolved form.

[0071] If it is desired to improve the cold properties of this hydrocarbon fraction, the liquid effluent produced by the hydrotreatment can be isomerized under isomerization conditions to isomerize at least partially the n-paraffins into isoparaffins.

[0072] Thus, in one embodiment, the first component of renewable origin can be a diesel fraction of a hydrotreated and isomerized oil.

[0073] In this case, the effluent exiting the hydrotreating step (i), and comprising the hydrotreated oil, is subjected in whole or in part to an isomerization step (ii), typically carried out in the presence of an isomerization catalyst, and optionally in the presence of hydrogen. In the latter case, it is referred to as hydroisomerization.

[0074] Isomerization catalysts are typically bifunctional catalysts comprising an acid function and a (de)hydrogenating function.

[0075] The acid function is generally provided by an amorphous or crystalline support, typically having a specific surface area of ​​100 to 700m2 / g and having an acidic surface, such as halogenated aluminas, (in particular fluorinated or chlorinated) or phosphated or sulfided, amorphous silica-aluminas (possibly containing boron), amorphous silica-aluminas-titaniums, sulfated zirconias, tungsten-containing zirconias and zeolites or a mixture thereof.Suitable support materials include amorphous alumina, amorphous silica-alumina, amorphous silica borate, amorphous silica-alumina-titanium, zeolites or modified zeolites having the following structures: ferrierite, beta zeolite, Y zeolite, mordenite zeolite and molecular sieves of the type ALPO-31, SAPO-11, SAPO-31, SAPO-37, SAPO-41, SM-3, MgAPSO-31, FU-9, NU-10, NU-23, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-50, ZSM-57, theta-1, EU-1, EU-13, ISL1, KZ-2, ISL4 and KZ-1, MeAPO-11, MeAPO-31, MeAPO-41, MeAPSO-11, MeAPSO-31, MeAPSO-41, MeAPSO-46, ELAPO-11, ELAPO-31, ELAPO-41, ELAPSO-11, ELAPSO-31, ELAPSO-41, each of them can be used alone or in combination. combination. The acidity of the support can be measured by methods well known to those skilled in the art. It can, for example, be carried out by temperature-programmed desorption (TPD) with ammonia, by infrared measurement of absorbed molecules (pyridine, CO2, etc.), by a catalytic cracking test, or by hydroconversion using a model molecule.

[0076] The (de)hydrogenation function is ensured either by one or more metals from group 6 of the periodic table of elements, or by a combination of at least one metal from group 6 and at least one metal from groups 8-10.

[0077] Suitable isomerization catalysts thus typically contain a zeolite, alumina and / or a metal selected from groups 6 and 8-10 of the periodic table and optionally a support.

[0078] Examples of catalysts exhibiting an isomerizing function include nickel oxide catalysts or nickel and tungsten oxides on an acidic support, such as amorphous silica / alumina, zeolite, ferrierite, phosphated alumina, phosphated silica / alumina and the like.

[0079] Preferably, the isomerization catalyst contains SAPO-11 or SAPO-41 or ZSM-22 or ZSM-23 or ferrierite and Pt, Pd or Ni and Al2O3 or SiO2. Typical isomerization catalysts are, for example, Pt / SAPO-11 / Al2O3, Pt / ZSM-22 / Al2O3, Pt / ZSM-23 / Al2O3, and Pt / SAPO-11 / SiO2. The catalysts can be used alone or in combination. The presence of hydrogen is particularly preferable to reduce catalyst deactivation. Especially preferably, the isomerization catalyst can be a bifunctional noble metal-based catalyst, such as the Pt-SAPO and / or Pt-ZSM catalyst, which is used in combination with hydrogen.

[0080] The isomerization step (ii) can for example be carried out at a temperature of 150-500°C, preferably 220-450°C, and at a pressure of 1 to 15MPa, preferably 1 to 9MPa or 2 to 6MPa (absolute).

[0081] The hourly space velocity can be from 0.1 to 20 h1, more preferably from 0.2 to 10 h1 and more preferably from 0.3 to 4 h1. The gases containing dihydrogen are introduced simultaneously with the feed charge at a ratio of 75 to 2500 NL(H2 ) / L of liquid feed charge, more preferably from 150 to 1500 or more preferably from 250 to 1000 NL(H2) / L of liquid feed charge.

[0082] Furthermore, the isomerization step (ii) is preferably a step that serves primarily to isomerize the hydrotreated effluent. In other words, while hydrotreatment generally results in low isomerization (usually less than 5% by mass), isomerization leads to a significant increase in the isoparaffin content. More precisely, it is preferable that the isoparaffin content (% by mass) be increased by the isomerization step by at least 30 percentage points, more preferably by at least 50 percentage points, more preferably-

[0083]

[0084]

[0085]

[0086]

[0087]

[0088]

[0089] reasonably by at least 60 percentage points, more preferably by at least 70 percentage points. This isomerization step (ii) can be implemented at the end of the hydrotreating step (i), for example by placing an isomerization catalyst bed downstream of the hydrotreating catalytic bed(s). The effluent produced by the hydrotreatment step (i) or the isomerization step (ii) can be fractionated to separate a liquid fraction and the non-condensable fractions and / or the unreacted dihydrogen, which can then be reused. In the present invention, it is the diesel fraction from the hydrotreating step (i) or the isomerization step (ii) that is used as a component of renewable origin. This diesel fraction typically corresponds to the liquid fraction of the hydrotreated or hydrotreated and isomerized effluent. This diesel fraction typically has an initial boiling point of 80 to 180 °C and a final boiling point of 360 °C or less, preferably 320 °C or less, notably measured according to ASTM D86-12. The diesel fraction used in the present invention may have one or more of the following characteristics: - a cloud point, from -20 °C to +10 °C, advantageously from -20 °C to +5 °C, from -18 °C to +5 °C or from -15 °C to +5 °C, in particular measured according to ASTM D2500-17a, or within any interval defined by two of these limits, - a paraffin content in C8 to C24, most often C8 to C20, of 95 to 100% by mass, advantageously of at least 97% by mass, at least 98% by mass or at least 99% by mass, or within any range defined by two of these limits, - a mass ratio of iso-paraffins / n-paraffins of 1.2 to 4.2, advantageously of 1.3 to 4, or in any interval defined by two of these limits. The renewable source component comprising a diesel fraction of a hydrotreated oil used in the present invention may have one or more of the following characteristics: - an initial boiling point of 80 to 180 °C and a final boiling point of 360 °C or less, preferably 320 °C or less, measured in particular according to ASTM D86-12, - a cloud point, from -20 °C to +10 °C, advantageously from -20 °C to +5 °C, from -18 °C to +5 °C or from -15 °C to +5 °C, in particular measured according to ASTM D2500-17a, or within any interval defined by two of these limits, - a paraffin content of C8 to C24, most often C8 to C20, of 95 to 100% by mass, advantageously of at least 97% by mass, of at least 98% by mass or at least 99% by mass, or within any interval defined by two of these limits, - a mass ratio of iso-paraffins / n-paraffins of 1.2 to 4.2, advantageously from 1.3 to 4 or in any interval defined by two of these limits.

[0090] Component of renewable origin comprising alkyl esters of fatty acids

[0091] In one embodiment, the hydrocarbon filler may comprise a second component of renewable origin which comprises, or is composed of, alkyl esters of fatty acids, the second component of renewable origin representing at most 5% of the total volume of the hydrocarbon filler. The content of the hydrocarbon filler subjected to step a) in the second component of renewable origin may be at most 1% by volume.

[0092] Advantageously, alkyl esters of fatty acids are methyl esters of fatty acids, methyl esters of fatty acids or mixtures thereof.

[0093] Alkyl esters of fatty acids are typically obtained by a step (iii) of transesterification of oil(s) of natural origin with an alcohol, advantageously methanol or ethanol.

[0094] During transesterification step (iii), the triglycerides contained in the natural oil(s) react with the alcohol to obtain alkyl esters of the fatty acids in a transesterification reactor. This reaction, well known to those skilled in the art, is usually carried out in the presence of a catalyst, by a homogeneous or heterogeneous acid or basic catalysis process, typically at a temperature of 25°C to 110°C or 35°C to 90°C and a reaction time of 30 minutes to 50 hours. For example, a catalyst / oil mass ratio of 0.25 to 8% and an alcohol / oil molar ratio of 3:1 to 15:1 may be used.

[0095] This reaction is carried out for example in the presence of acid catalysts (hydrochloric acid, sulfuric acid, sulfonic acid, boron trifluoride, zinc chloride, acid ion exchangers, aluminium trioxide, iron trioxide, etc.) or in the presence of basic catalysts such as alkali metal alkoxides and hydroxides as well as sodium or potassium carbonates (sodium hydroxide, potassium hydroxide, sodium ethoxide, potassium ethoxide, etc.).

[0096] The transesterification reaction can also be carried out under supercritical conditions, with the reaction being implemented at high pressures of 15-35 MPa and, in some cases, at high temperatures of 250-280°C, or even higher (300-350°C). Under these supercritical conditions, the reaction can be carried out in the absence or presence of a catalyst. Examples of usable conditions and catalysts are described in "Transesterification in Super-critical Conditions" by Somkiat Ngamprasertsith et al., Biodiesel - Feedstocks and Processing Technologies, November 2011, Chapter 12, pages 247-268. In the absence of For example, with a catalyst, it can operate at temperatures of 280-350°C, pressures of 19 to 35MPa, an alcohol / oil molar ratio of 24:1 to 42-1 and a reaction time of 5 to 30 min.

[0097] The alkyl esters of fatty acids used in the present invention can therefore advantageously be free of impurities such as unsaponifiable compounds, soaps, or other compounds derived from animal fats or used cooking oils used as raw materials. In particular, their unsaponifiable content can advantageously be less than or equal to 1% w / w (measured according to ISO 3596:2001).

[0098] The oil of natural origin may be as previously described. In a preferred embodiment, this oil of natural origin is selected from animal fat and / or used oil, and in particular from animal fat and / or used oil having waste status, thereby further reducing the environmental impact of the fluids produced by the process according to the invention. Advantageously, this oil of natural origin has a content of compounds other than glycerides and free fatty acids, and in particular other than triglycerides and free fatty acids, of less than or equal to 1% by mass.

[0099] The alkyl esters of fatty acids, and in particular the methyl or ethyl esters of fatty acids, used in the present invention may have carbon chains of 12 to 22 carbon atoms.

[0100] Preferably, the content of alkyl esters of fatty acids, and in particular methyl or ethyl esters of fatty acids, whose carbon chain contains 20 to 22 carbon atoms, shall be as low as possible, advantageously less than or equal to 2%m, or even 1% by mass, preferably zero, in order to improve cold properties and in particular freezing point.

[0101] Alternatively or in combination, alkyl esters of fatty acids, and in particular methyl or ethyl esters of fatty acids, may comprise at least 9% by mass or at least 20% by mass of alkyl esters of fatty acids having a carbon chain containing 12 to 16 carbon atoms.

[0102] Advantageously, particularly when produced from animal fats and / or used cooking oils which are animal by-products, alkyl esters of fatty acids, and in particular methyl or ethyl esters of fatty acids, may comprise at least one of the following characteristics: - at least 9% wt%, typically from 9% wt% to 64% wt%, of fatty acid methyl esters whose carbon chain contains 12 to 16 carbon atoms, - at least 25% w, typically from 30% w to 98% w, of fatty acid methyl esters whose carbon chain contains 18 carbon atoms, - at most 4% w, typically from 0% w to 2% w, of fatty acid methyl esters fat whose carbon chain contains 20 to 22 carbon atoms.

[0103] When these esters are produced from animal by-products which are animal fats, alkyl esters of fatty acids, and in particular methyl or ethyl esters of fatty acids, may comprise at least one of the following characteristics: - at least 20% wt, typically from 20% wt to 64% wt, of fatty acid methyl esters with a carbon chain containing 12 to 16 carbon atoms, - at least 25% wt, typically from 25% wt to 65% wt, of fatty acid methyl esters with a carbon chain containing 18 carbon atoms, - at most 4% wt%, typically from 0% wt% to 2% wt%, of fatty acid methyl esters whose carbon chain contains 20 carbon atoms, - at most 1%m, typically from 0%m to 1%m, of fatty acid methyl esters whose carbon chain contains 22 carbon atoms.

[0104] The process according to the invention can thus include a step of supplying alkyl esters of fatty acids, by transesterification of oils of natural origin with an alcohol, preferably with methanol, ethanol or mixtures thereof.

[0105] Advantageously, the alcohol is of renewable origin, for example obtained by conversion of a synthesis gas comprising CO / H2, this synthesis gas being derived from biomass (for example produced by biomass gasification, biomass pyrolysis, or by fermentation or anaerobic digestion of biomass in the presence of one or more microorganisms, possibly followed by partial oxidation of the biogas in the presence of dioxygen). These processes are well known to those skilled in the art. Hydrocarbon charge

[0106] The hydrocarbon feedstock introduced in step a) of the present invention contains a fossil-based hydrocarbon component and a renewable component comprising a diesel fraction of hydrotreated oil (or hydrotreated and isomerized oil) in a content of at most 10% by volume, preferably at most 9%, 8%, 7%, 6%, or 5% by volume relative to the hydrocarbon feedstock. In one embodiment, the content of this renewable component of the hydrocarbon feedstock may be at most 4%, 3%, 2%, or 1% by volume. Advantageously, the content of this renewable component of the hydrocarbon feedstock may be at least 0.1% by volume, advantageously at least 0.5% by volume.

[0107] In particular, the content of this renewable component of the hydrocarbon feed can be included in any interval defined by any two of the aforementioned limits.

[0108] Advantageously, the content of a component of renewable origin comprising alkyl esters of fatty acids, in particular methyl and / or ethyl esters The hydrocarbon content of the fatty acids may be from 0% to 5% by volume, advantageously from 0 to 1% by volume, for example, not more than 0.9%, 0.6%, or 0.5% by volume, or within any range defined by two of these limits. When the hydrocarbon content includes a component of renewable origin comprising alkyl esters of fatty acids, the content of the hydrocarbon content of this second component may advantageously be at least 0.1% by volume.

[0109] Thus, advantageously, the hydrocarbon charge comprises, or is made up of, the hydrocarbon component of fossil origin, the component of renewable origin comprising a diesel fraction of a hydrotreated oil (or of a hydrotreated and isomerized oil), and optionally the second component of renewable origin.

[0110] It may be possible, in particular, to adjust the content of the renewable component comprising a diesel fraction of hydrotreated oil, and optionally the content of the renewable component comprising alkyl esters of fatty acids, of the hydrocarbon feedstock within the aforementioned ranges so that the kerosene fraction recovered at the outlet of fractionation step b) has a freezing point of no more than -47 °C. Alternatively or in combination, the cutting points of the kerosene fraction recovered during fractionation step b) may be adjusted to recover a kerosene fraction having a freezing point of no more than -47 °C.

[0111] The hydrocarbon feed can be prepared by simply mixing the components, in particular upstream of the hydrotreating step a), or during step a).

[0112] It will thus be possible to plan to mix the components of the hydrocarbon feed upstream of at least one hydrotreating reactor in which step a) is implemented, or within this at least one reactor. Step a)

[0113] Step a) of hydrotreating the hydrocarbon feedstock can be carried out in one or more reactors. Any type of reactor commonly used for this type of reaction may be used, for example a fixed-bed reactor, a bubbling-bed reactor, a slurry reactor, etc., preferably a fixed-bed reactor.

[0114] In particular, a reactor of the type usually used for the hydrotreating of fossil-based hydrocarbons may be used.

[0115] Advantageously, step a) can be carried out under a pressure of 15 to 130 bar and at a temperature of 250 to 380 °C, preferably 280 to 340 °C, in the presence of dihydrogen and at least one hydrotreating catalyst.

[0116] Typically, a liquid hourly space velocity (LHSV) can be predicted: from 0.2 to 9 hr1, preferably 0.5 to 7 hr1, and more preferably 0.8 to 1.8 hr1, and a dihydrogen ratio of: 50 to 1500 Nm3 / m3 of charge, preferably 120 to 250 Nm3 / m3 and more preferably 120 to 200 Nm3 / m3.

[0117] Step a) can typically be implemented in at least one fixed-bed reactor, comprising one or more catalyst beds.

[0118] More specifically, step a) can be carried out under a pressure of 15 to 50 bar and at a temperature of 280 °C to 340 °C, in the presence of dihydrogen and at least one hydrotreating catalyst, typically with a dihydrogen content of 120 to 180 Nm³ / m³ of feed. Typically, an hourly spatial velocity of the liquid of 1 to 1.6 h⁻¹ can be expected.

[0119] The hydrotreating catalyst is a conventional hydrotreating catalyst. Conventional hydrotreating catalysts include, in particular, an active metallic compound such as nickel, platinum, palladium, rhenium, rhodium, nickel tungstate, nickel molybdenum, molybdenum, cobalt molybdenum, or nickel molybdenum, this metallic compound being deposited or not on a support. This support may generally include oxides such as silicas, aluminas, aluminosilicates (in particular zeolites), titanium oxides, or even carbon, molecular sieves, salts, or alkaline earth metals. When a support is present, it advantageously has a specific surface area ranging from 100 to 250 m² / g, preferably from 150 to 200 m² / g.

[0120] Advantageously, the catalyst may comprise at least two metals from groups 6, 9, 10, 11 of the periodic table of elements, preferably at least two metals such as NiMo, CoMo, or even CoNiMo, preferably on an alumina support.

[0121] When supported, conventional hydrotreating catalysts typically comprise a metal content of 0.01 to 25% by mass relative to the total mass of the catalyst, preferably 15 to 20% by mass, for example 20% by mass relative to the total mass of the catalyst.

[0122] In a preferred embodiment, the catalyst used does not exhibit isomerizing activity or exhibits negligible isomerizing activity under the reaction conditions. In other words, the catalyst does not promote the isomerization of hydrocarbon compounds present in the feed. When a support is present, it is preferably slightly acidic or non-acidic.

[0123] Thus, a catalyst not exhibiting an isomerizing function may comprise at least one metal from groups 6, 9, 10, 11 of the periodic table of elements, optionally on a support chosen from alumina, silica alumina, phosphate alumina, borated alumina, silica alumina phosphate, alone or in mixture.

[0124] The hydrotreatment step a) produces an effluent containing a liquid fraction containing the kerosene fraction, and a gaseous fraction. Step b)

[0125] The hydrotreated feed obtained at the outlet of step b) undergoes fractionation. This Fractionation can be carried out by distillation or stripping, in particular by adding a separation column, for example a distillation column, or a stripping column.

[0126] After the hydrotreating step, the effluent exiting the reactor is fractionated, typically by stripping, in order to recover a kerosene fraction. This fractionation can be carried out so that the kerosene fraction forms a jet fuel, meeting in particular the desired specifications.

[0127] The recovered kerosene fraction has a final boiling point of less than or equal to 300°C, in particular measured according to ASTM D86-12.

[0128] The initial boiling point according to ASTM D86-12 can be from 120 to 185°C. The final boiling point according to ASTM D86-12 can be from 220 to 300°C.

[0129] The recovered kerosene fraction may advantageously exhibit one or more of the following properties: - a kinematic viscosity at -20°C of 1.2 to 8.0 mm2 / s (NF EN ISO 3104-August 1996), - a density at 15°C of 775 to 840 kg / m3 (ASTM D4052-18 or IP 365), - a freezing point of no more than -47°C (ASTM D5972-23 or IP435), - a flash point of at least 38°C (IP170-21 or ASTM D56-21A).

[0130] In particular, the cutting points of the recovered kerosene fraction can be adapted to obtain a kerosene fraction that meets the required specifications, for example those of an Al jet according to ASTM D1655-21, especially at least with regard to the final distillation point and / or the freezing point and / or the flash point.

[0131] The fractionation step also allows the gas produced, in particular methane, to be recovered during the hydrotreating step. Description of the single figure

[0132] Fig. 1 is a simplified diagram of a hydrotreatment unit enabling the process to be implemented according to an embodiment of the invention.

[0133] This unit 1 includes a reactor 2 into which the feed to be treated is introduced by means of a line 3. This reactor contains one or more beds of hydrotreating catalysts.

[0134] The feedstock (C) in the present invention is a mixture of a kerosene feedstock of fossil origin and a component of renewable origin, which here comprises a diesel fraction of hydrotreated oil. Optionally, the feedstock (C) may also contain another component of natural origin comprising alkyl esters of fatty acids. In the example, the various components of the feedstock (C) are introduced simultaneously; however, they could also be introduced separately.

[0135] A line 4 recovers the effluent from reactor 2 and conveys it to a section of Separation 5.

[0136] A heat exchanger 6 is placed downstream of the reactor on line 4 in order to heat the charge circulating in line 3, upstream of the reactor.

[0137] Upstream of this heat exchanger 6, a line 7, connected to line 3, supplies the load to be treated with a gas rich in H2.

[0138] Downstream of the heat exchanger 6, and upstream of the reactor 2, the feed mixed with the H2-rich gas circulating in line 3 is heated by a furnace 8.

[0139] Thus, the feed is mixed with the hydrogen-rich gas, then brought to the reaction temperature by the heat exchanger 6 and the furnace 8 before entering reactor 2. It then passes into reactor 2.

[0140] Upon exiting the reactor, the resulting mixture is cooled and then separated in the separation section 5, for example by stripping, which makes it possible to obtain:

[0141] - a gaseous fraction (G), containing in particular water from stripping, of gaseous hydrocarbons, an acidic gas rich in H2S, part of which is here reinjected into the H2-rich gas mixed with the feed, by means of a line 9,

[0142] - a kerosene (K) cup.

[0143] The example below illustrates the invention without limiting its scope. Examples

[0144] Two kerosene cuts taken from the outlet of an atmospheric crude distillation unit were mixed with various components of renewable origin.

[0145] The characteristics of the fossil-derived kerosene cuts used, denoted "Kero-1" and "Kero-2", are presented in Table 1 below.

[0146] [Table 1] Characteristics of kerosene cuts Characteristics Unit Method Kero-1 Kero-2 Density at 15°C kg / m3 ASTM D4052-18 0.7977 0.8089 Freezing Point °C ASTM D5972 -23 -61.1 -50.1 Distillation ASTM D86-12 Initial Point °C 143.1 144.8 5% distilled °C 164.7 165.4 10% distilled °C 168.5 169.5 15% distilled °C 172.4 174 20% distilled °C 175.6 178.3 30% distilled °C 180.8 186.1 40% distilled °C 186.1 194.1 50% distilled °C 190.8 202.7 60% distilled °C 195.6 212.2 70% distilled °C 201.0 222.4 80% distilled °C 207.2 233 90% distilled °C 215.7 246.4 95% distilled °C 222.4 257 Final point °C 230.7 267 Distilled volume 98.3 99.6 Residue 1.3 1.2

[0147] Three components of renewable origin were used: “HVO -17°C”, “HVO -11°C”, “HVO +4°C” which are hydrotreated and isomerized oils having cloud points of approximately -17°C, -11°C and +4°C respectively.

[0148] The main characteristics of these fillers are presented in Table 2. The distribution of iso-paraffins and n-paraffins was determined by an inverse phase GCxGC-FID analysis.

[0149] [Table 2] Characteristics of components of renewable origin Analysis Unit Method HVO -17°C HVO -11°C HVO +4°C Density at 15°C Kg / m3 NF EN ISO 12185 774.2 774.22 779.99 Cloud Point °C NF EN 23015 -16.8 -11.4 +4.2 Filterability Limit Temperature °C NF EN 116 -16 -1 Distillation Initial Point °C 149.6 5% °C 188.7 10% °C 204.1 15% °C 218.6 20% °C 232.9 30% °C 252.7 40% °C 265.5 50% °C 273.6 60% °C 278.6 70% °C 282.6 80% °C 285.6 90% °C 287.0 95% °C 286.2 End point °C 292.2 Distilled volume 98.1 Residue 1.5 Chain lengths ISO 5508:1990 n-para i-para n-para i-para n-para i-para Saturated <C8 0,33 0,31 0,31 C8 %m 0,36 0,91 0,33 0,86 0,13 0,41 C9 %m 0,57 2,10 0,55 1,95 0,18 0,67 CIO %m 0,64 2,99 0,68 2,99 0,24 0,92 Cil %m 0,59 3,61 0,66 3,81 0,24 1,12 C12 %m 0,62 3,92 0,73 4,39 0,34 1,22 C13 %m 0,40 3,54 0,55 4,19 0,21 1,08 C14 %m 0,65 3,38 1,52 4,03 0,68 1,22 C15 %m 1,24 1,95 1,62 1,87 2,14 1,87 C16 %m 6,86 21,13 7,56 15,99 16,19 17,01 C17 %m 2,91 7,24 2,22 1,72 3,00 3,63 C18 %m 5,20 27,38 7,30 32,71 19,05 26,57 C19 %m 0,04 0,13 0,04 0,07 0,08 0,00 C20 %m 0,04 0,15 0,04 0,21 0,18 0,33 C21 %m 0,00 0,04 0,00 0,00 0,02 0,01 C22 %m 0,00 0,00 0,00 0,00 0,04 0,04 C23 %m 0,00 0,00 0,00 0,00 0,01 0,00 C24 %m 0,00 0,00 0,00 0,00 0,01 0,00 C25 %m 0,00 0,00 0,00 0,00 0,00 0,00 C26 %m 0,00 0,00 0,00 0,00 0,00 0,00 C27 %m 0.00 0.00 0.00 0.00 0.00 0.00 C28 %m 0.00 0.00 0.00 0.00 0.00 0.00 Total %m 20.11 78.46 23.81 74.80 42.75 56.11 Saturates >C28 %m 0.00 0.00 0.00 Naphthenes %m 1.08 0.99 0.73 Mono-aromatics + NMA %m 0.02 0.09 0.03 Di-aromatics %m 0.00 0.00 0.00 Tri-aromatics %m 0.00 0.00 0.00 FAME %m 0.00 0.00 0.07 Unknowns %m 0.00 0.00 0.01 Total %m 100.00 100.00 100.00 Mass ratio i / n 3.90 3.14 1.31

[0150] The catalyst used is a CoMo type catalyst. The operating conditions are presented in Table 3.

[0151] [Table 3] Hydrotreatment operating conditions Total pressure at reactor inlet (barg) 30 Partial pressure H2 at reactor outlet (bara) 23 H2 / HC (NL / L) 150 WH (h') 2 Temperature at reactor inlet (°C) 290

[0152] The freezing point (denoted FP) was determined for the effluents obtained for each feed; the results are presented in Table 4 below. Each of these effluents corresponds to the liquid fraction exiting the reactor after gas separation.

[0153] In Table 4, AFP corresponds to the difference (denoted) between the freezing point of hydrotreated kerosene alone and in a mixture with the renewable component considered. AFP thus represents the degradation of the freezing point of the effluent produced for the different renewable compounds.

[0154] [Table 4] Freezing Point Measurements (ASTM Method D5972-23) Renewable fuel source incorporation rate (%vol) FP (°C) AFP Kero-1 - -61.1 0 Kero-1 + HVO -17°C 5 -55.6 5.5 Kero-1 + HVO -11°C 3 -55.6 5.5 Kero-1 + HVO +4°C 1 -61.0 0.1 Kero-2 -50.1 0 Kero-2 + HVO -17°C 3 -48.8 1.3 Kero-1 + HVO -11°C 2 -49.1 1.0 Kero-1 + HVO +4°C 1 -48.5 1.6

[0155] It is observed that the cold properties are only slightly modified when renewable components are incorporated in co-processing. Furthermore, the quantity of renewable component can be adjusted so that the resulting mixture has a freezing point of no more than -47°C. It should be noted that up to 10% by volume of a renewable component can be incorporated, as demonstrated by the freezing points of mixtures containing the Kero-1 kerosene fraction, which remain well below the maximum value of -47°C.

[0156] Tables 5 and 6 gather the other properties of the effluents obtained during the co-processing of Kero-1 with the components of renewable origin, more precisely of the 140°C+ fraction of the effluent exiting the hydrotreatment reactor.

[0157] It is observed that the 140°C+ fractions of the effluents obtained comply with most of the specifications of an Al jet.

[0158] [Table 5] Co-processing Kero-1 and renewable origin components HVO -17°C, HVO-11°C and HVO +4°C Unit Method Spec. Jet Al ASTM D1655-2 1 Charge Kero-1 Kero-1 +5% HVO -17°C Kero-1 +3% HVO -1% Kero-1 +1% HVO +4°C FP °C ASTM D5972-23 -61.1 -55.6 -55.6 -61.0 -47 max Smoke Point mm ASTM D1322-19 24.5 24.2 23.5 18 min Viscosity at -20°C mm² / s NF EN ISO 3104-August 1996 3.563 3.493 3.421 8 max Viscosity at -40°C mm² / s NF EN ISO 3104-August 1996 6.769 6.478 6.356 12 max Density at 15°C kg / m³ ASTM D4052-18 797.71 796.53 797.04 797.57 775-840 Distillation ASTM D86-12 Initial point °C 143.1 144.5 145.2 143.1 5% 164.7 163.4 163.6 163.3 10% 168.5 168.8 168.3 168.3 200 max 15% 172.4 172.7 172.3 172.2 20% 175.6 175.9 175.5 175.4 30% 180.8 181.4 181.1 180.8 40% 186.1 186.7 186.3 185.8 50% 190.8 191.8 191.1 190.6 60% 195.6 197.1 196.2 195.6 70% 201.0 203.2 202.0 201.1 80% 207.2 211.0 209.4 207.8 90% 215.7 223.8 220.7 217.6 95% 222.4 243.0 235.8 227.4 Endpoint 230.7 264.3 256.0 245.3 300 max Aromatic content by HPLC %vol ASTMD 6379-21 16.1 16.5 16.8 25 max

[0159] [Table 6] Coprocessing Kero-2 and renewable origin components HVO -17°C, HVO-11°C and HVO +4°C Unit Method Spec. Jet Al ASTM D1655-2 1 Charge Kero-2 Kero-2 +5% HVO -17°C Kero-2 +3% HVO -ire Kero-2 +1% HVO +4°C FP °C ASTM D5972-23 -50.1 -48.8 -49.1 -48.5 -47 max Smoke Point mm ASTM D1322-19 21 21.8 21.1 20.7 18 min Viscosity at -20°C mm2 / s NF EN ISO 3104-August 1996 4.176 4.274 4.255 4.236 8 max Viscosity at -40°C mm2 / s NF EN ISO 3104-August 1996 8.384 8.649 8.604 8.360 12 max Density at 15°C kg / m3 ASTM D4052-18 808.8 807.88 808.21 808.61 775-840 Distillation ASTM D86-12 Initial point °C 144.8 144.6 144.0 142.9 5% 165.4 165.0 164.9 164.2 10% 169.5 170.5 170.5 170.2 200 max 15% 174 174.7 174.6 174.5 20% 178.3 179.0 178.7 178.6 30% 186.1 187.0 186.2 186.0 40% 194.1 194.7 194.4 194.0 50% 202.7 202.9 202.9 202.5 60% 212.2 212.7 212.3 211.8 70% 222.4 223.2 222.5 222.0 80% 233 234.5 233.7 232.9 90% 246.4 249.0 247.7 246.9 95% 257 261.9 260.2 259.0 Endpoint 267 271.8 271.0 269.8 300 max Aromatic content by HPLC %vol ASTMD 6379-21 21 20.2 18.2 19.2 25 max

Claims

Claims

1. A method for manufacturing a jet fuel comprising at least the steps of: a) subjecting a hydrocarbon feedstock comprising a hydrocarbon component of fossil origin to a hydrotreatment step and obtaining a hydrotreated hydrocarbon feedstock; b) fractionating the hydrotreated hydrocarbon feedstock obtained in step a) and recovering a kerosene fraction as jet fuel, said kerosene fraction having a final boiling point of less than or equal to 300°C, the method being characterized in that the hydrocarbon feedstock subjected to the hydrotreatment step a) further comprises a component of renewable origin comprising a diesel fraction of a hydrotreated oil, the component of renewable origin representing at most 10% by volume of the total volume of the hydrocarbon feedstock.

2. Manufacturing process according to claim 1, in which the content of the hydrocarbon feedstock subjected to step a) of component of renewable origin comprising a diesel fraction of a hydrotreated oil is at least 0.1% by volume.

3. A manufacturing method according to any one of claims 1 or 2, wherein the component of renewable origin comprising a diesel fraction of a hydrotreated oil used in the present invention has one or more of the following characteristics: - an initial boiling point of 80 to 180°C and a final boiling point of less than or equal to 360°C, preferably less than or equal to 320°C, - a cloud point of -20°C to +10°C, advantageously of -20°C to +5°C, of ​​-18°C to +5°C or of -15°C to +5°C, - a C8 to C24 paraffin content, most often of C8 to C20, of 95 to 100% by mass, - an iso-paraffins / n-paraffins mass ratio of 1.2 to 4.

2.

4. A manufacturing process according to any one of claims 1 to 3, wherein the hydrocarbon feedstock subjected to the hydrotreatment step further comprises a second component of renewable origin comprising alkyl esters of fatty acids, the second component of renewable origin representing at most 5% of the total volume of the hydrocarbon feedstock.

5. Manufacturing process according to claim 4, in which the content of the hydrocarbon feedstock subjected to step a) in second component of renewable origin is at most 1% by volume.

6. Manufacturing method according to claim 4 or 5, wherein the second component of renewable origin comprises one or more of the following characteristics: - the fatty acid alkyl esters have carbon chains of 12 to 22 carbon atoms, - the fatty acid alkyl esters comprise at least 9% by mass or at least 20% by mass of fatty acid alkyl esters whose carbon chain contains from 12 to 16 carbon atoms, - the content of fatty acid alkyl esters whose carbon chain contains from 20 to 22 carbon atoms is less than or equal to 2% by mass.

7. A manufacturing method according to any one of claims 1 to 6, wherein the hydrocarbon component of fossil origin is a kerosene fraction or a mixture of kerosene fractions.

8. Manufacturing process according to any one of claims 1 to 7, in which step a) is carried out under a pressure of 15 to 130 bars and at a temperature of 250 and 380°C, in the presence of dihydrogen and at least one hydrotreatment catalyst.

9. Manufacturing process according to any one of claims 1 to 8, in which step a) is carried out in the presence of at least one hydrotreatment catalyst comprising at least one metal from groups 6, 9, 10, 11 of the periodic table of elements, optionally on a support chosen from alumina, silica alumina, phosphated alumina, borated alumina, phosphated silica alumina, alone or as a mixture.

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