Process for producing a jet fuel from feedstocks of renewable origin

Abstract

The invention relates to a process for producing a jet fuel, the process 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, the kerosene fraction having a final boiling point of less than or equal to 300°C, the process being characterised 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.

Description

[0001] TITLE: PROCESS FOR MANUFACTURING JET FUEL FROM FEEDSTOCKS OF RENEWABLE ORIGIN

[0002] Technical field

[0003] The present invention relates to the technical field of refining petroleum feedstocks of fossil origin and feedstocks of biological origin, in particular for the manufacture of jet fuel. More particularly, the invention relates to a method for obtaining jet fuel having a component of biological (or renewable) origin.

[0004] Background to the invention

[0005] Conventional jet fuels, also known as jet fuel, kerosene, 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 straight-chain and branched alkanes, cycloalkanes, and aromatic hydrocarbons. The cutpoints of the jet fuel fraction typically range between 140 °C and 240 °C.

[0006] Commercial jet fuel is typically produced by blending different fuel bases. These fuel bases may be crude oil distillation cuts, possibly hydrotreated or sometimes subjected to a sweetening treatment (e.g., the MEROX process). These bases may also be cuts from a hydrocracker effluent or a catalytic cracker effluent (often after hydrotreatment). Other fuel bases may be prepared by other routes, such as Fischer-Tropsch synthesis followed by a cracking step. The choice of fuel bases and their relative proportions are made to ensure that the final properties of the blend meet the desired specifications.

[0007] Due to the scarcity of fossil resources and growing environmental concerns, the use of molecules derived from biomass is increasingly sought to replace molecules of fossil origin. However, the preparation of jet fuel from molecules derived from biomass that can be directly used in the formulation of jet fuel represents a real economic and environmental challenge. In particular, some countries such as France are implementing incentive taxes relating to the incorporation of renewable energy in transport and in particular for the aviation sector.

[0008] Prior Art One solution for obtaining jet fuel with a component of biological origin consists of mixing a conventional jet with a paraffinic base derived from renewable feedstocks as provided for by the ASTM D7566-21 standard, thus allowing the production of alternative aviation fuels. Aviation fuel bases derived from renewable feedstocks that can be incorporated into fossil jet are

[0009] • Synthetic paraffinic kerosenes [SPK], produced by processes such as the Fischer-Tropsch process, hydrotreatment of esters and fatty acids [HEFA-SPK], or produced by the Alcohol-to-jet route (transformation of alcohol into kerosene) [ATJ-SPK],

[0010] • Synthetic isoparaffins produced by hydrotreatment from fermented sugars [SIP-HFS],

[0011] • Synthetic aromatic kerosenes obtained by alkylation of light aromatics from non-petroleum sources [SPK / A],

[0012] • Synthetic kerosenes obtained from the hydrothermal conversion of fatty acid esters and fatty acids,

[0013] • Synthetic paraffinic kerosenes [SPK] obtained from hydrocarbons, esters and hydrotreated fatty acids.

[0014] This solution, however, requires specific processing facilities to produce the paraffinic bases which will be mixed with the conventional jet.

[0015] Another solution consists of co-processing a hydrocarbon of fossil origin with a feedstock of renewable origin, as provided for in particular in the ASTM D1655-21 c standard.

[0016] Thus, document EP2346962 describes a process for obtaining a kerosene fraction, part of which is of biological origin. For this purpose, a feedstock of petroleum origin mixed with a feedstock of biological origin is subjected to a hydrotreatment step, then fractionated in order to recover a kerosene fraction. The feedstock of biological origin 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.

[0017] However, there is still a need for a process for manufacturing jet fuel with a component of biological origin by co-treatment in a hydrotreatment unit without modifying the process.

[0018] Description of the invention

[0019] The invention provides a process 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 less than or equal to 300°C, measured in particular according to the ASTM D86-12 standard.

[0020] According to the invention, the hydrocarbon feedstock subjected to 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.

[0021] The process according to the invention thus makes it possible to obtain an aviation fuel, a portion of which is of renewable origin, also called SAF for "Sustainable Aviation Fuel" in English. In addition, by using a diesel fraction of a hydrotreated oil, the process according to the invention makes it possible to recover these diesel fractions for the manufacture of new fuels other than diesel engine fuels.

[0022] In particular, the method according to the invention can be implemented in existing hydrotreatment units, in particular using a conventional hydrotreatment catalyst, preferably a catalyst whose active metal compound is chosen from nickel, cobalt and / or molybdenum.

[0023] Detailed description of the invention

[0024] The terms "comprising" and "comprises" as used herein are synonymous with "including," "includes," or "contains," "containing," and are inclusive or unbounded and do not exclude additional features, elements, or method steps not specified.

[0025] The expressions % by weight and % by mass (also noted “%m”) have an equivalent meaning and refer to the proportion of the mass of a product relative to 100g of a composition comprising it.

[0026] 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. Carbon number ranges (e.g., C6 to C18, or C19+) refer to molecules having carbon numbers within the stated 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 that every carbon number in a range be represented in the molecules described. 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 iso-paraffins at a given carbon number is determined by ASTM D-5442 analysis of petroleum waxes by gas chromatography ("GC") or an equivalent gas chromatographic method. For example, this may be as described in: Marko R. Djokic et al. Quantitative analysis of crude and stabilized bio-oils by comprehensive two-dimensional gas-chromatography. Journal of Chromatography A, 7257 (2012) pp131-140.

[0027] Boiling points as mentioned here are measured at atmospheric pressure, unless otherwise stated. An initial boiling point is defined as the temperature value from which a first vapor bubble is formed. A final boiling point is the highest temperature achievable during a distillation. At this temperature, no more vapor can be transported to a condenser. The determination of the initial and final points uses techniques known in the art 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 the measurement of boiling points of petroleum fractions by gas chromatography, ASTM D7169-05 for heavy hydrocarbons, ASTM D7500-15(2019), D86-12 or D1160-18 for distillates.

[0028] The density of a jet fuel type hydrocarbon can be measured according to ASTM D4052-18.

[0029] The cloud point of a biologically derived hydrocarbon effluent can be measured according to ASTM D2500-17a.

[0030] The content of aromatic compounds and naphthenes can be determined by gas chromatography (reverse-phase GcxGC or by GC according to method UOP744).

[0031] Hydrocarbon component of fossil origin

[0032] 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.

[0033] Hydrocarbons of fossil origin that can be used in the present invention may advantageously be chosen from kerosene fractions. In a preferred embodiment, the hydrocarbon component of fossil origin is a kerosene fraction of fossil origin or a mixture of kerosene fractions of fossil origin.

[0034] A fossil-based kerosene fraction 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.

[0035] These kerosene cuts can be:

[0036] - a kerosene cut from the direct distillation of crude oil,

[0037] - a kerosene cut from different conversion processes such as catalytic cracking, hydrocracking and / or visbreaking.

[0038] Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, has:

[0039] - a freezing point of not more than -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or

[0040] - 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.

[0041] In the context of hydrotreatment, the fossil hydrocarbons are advantageously a kerosene cut or a mixture of kerosene cuts, preferably from the direct distillation of crude oil or from hydrocracking.

[0042] Components of renewable origin

[0043] According to the invention, the hydrocarbon feedstock subjected to hydrotreatment step a) comprises a component of renewable origin comprising, or consisting of, a diesel fraction of a hydrotreated oil. In one embodiment, the hydrocarbon feedstock may optionally further comprise another component of renewable origin comprising, or consisting of, alkyl esters of fatty acids, in particular methyl and / or ethyl esters of fatty acids.

[0044] A component of renewable origin means a component that is completely free of components of mineral or fossil origin.

[0045] The process according to the invention can thus comprise, upstream of the hydrotreatment step a), an initial step a1) of supplying a component of renewable origin comprising a diesel fraction of a hydrotreated oil, and optionally an initial step a2) of supplying another component of renewable origin comprising alkyl esters of fatty acids.

[0046] The supply step a1) may comprise: - at least one step (i) of hydrotreatment of one or more oils of natural origin to produce a hydrotreated oil,

[0047] - an optional step (ii) of isomerization of the hydrotreated oil to produce a hydrotreated and isomerized oil,

[0048] - an optional step of fractionating the hydrotreated oil or the hydrotreated and isomerized oil to recover a diesel fraction from a hydrotreated oil and / or an optional step of mixing several diesel fractions from a hydrotreated oil,

[0049] Supply step a2) may include:

[0050] - a step (iii) of transesterification of one or more oils of natural origin with an alcohol to provide a component of renewable origin comprising alkyl esters of fatty acids.

[0051] These different stages are detailed below.

[0052] Renewable component comprising a diesel fraction of an oil

[0053] The first renewable component used in the present invention comprises, or consists of, a diesel fraction of a hydrotreated oil.

[0054] This diesel fraction of a hydrotreated oil is typically obtained by hydrotreatment (i) of an oil of natural origin or a mixture of oils of natural origin, generally carried out in the presence of dihydrogen and at least one catalyst to transform the fatty acid esters and the free fatty acids, contained in an oil of natural origin or a mixture of oils of natural origin, 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 originating from the hydrotreatment of one or more oils of natural origin.

[0055] A naturally derived oil is defined as an oil that does not contain mineral oil of fossil origin.

[0056] Typically, a naturally occurring oil may contain 50%m or more, 60%m or more, preferably 70%m or more, of phenolic lipids, fatty acids and / or fatty acid esters (mono-, di-, triglycerides).

[0057] Typically, a naturally occurring oil may contain fatty acid esters (mono-, di-, or triglycerides) and / or free fatty acids, containing one to three C8-C24 acyl groups, either saturated or unsaturated. When multiple acyl groups are present, they may be the same or different.

[0058] The oil of natural origin may be chosen from vegetable oil, animal oil or fat, used oil, oil produced by microorganisms, animal fats and / or used cooking oils which are animal by-products, as well as mixtures thereof.

[0059] The vegetable oil can be chosen from pine oil, rapeseed oil, sunflower oil, castor oil, peanut oil, linseed oil, babasu 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 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 (including cashew nut shell oil), and any combination thereof.

[0060] Used oil includes used cooking oils (used cooking oils) and oils recovered from waste water, such as trap and drain grease / oils, gutter oils, sewer oils, e.g. from water treatment plants, and used greases from the food industry.

[0061] Animal fat can be chosen from tallow, lard, fat (yellow and brown fat), fish oil / fat, milk fat.

[0062] In particular, it will be possible to use animal fats and used cooking oils which are animal by-products and have the status of animal by-products within the meaning of Regulation (EC) No 1069 / 2009 of the European Parliament and of the Council of 21 October 2009 and Commission Regulation (EU) No 142 / 2011 (implementing regulation of Regulation EC No 1069 / 2009).

[0063] Animal fats with animal by-product status are fatty residues of animal origin, other than used cooking oils, originating for example from food industries or rendering plants. Used cooking oils with animal by-product status are used cooking oils (used cooking oils or UCO), namely residues of fats of plant or animal origin used for human consumption, in the food industry, in collective or commercial catering.

[0064] The oil of natural origin may also be an oil produced by microorganisms, natural or genetically modified, such as bacteria, yeasts, in particular oleaginous yeasts, algae, prokaryotes or eukaryotes. In particular, these oils may be recovered by well-known mechanical or chemical extraction methods. In a preferred embodiment, this oil of natural origin may 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,

[0065] Hydrotreated oil is obtained by hydrotreatment (i) of oil(s) of natural origin in the presence of at least one catalyst. This hydrotreatment step (i) can be carried out in one or more hydrotreatment reactors. Any type of reactor normally used for this type of reaction can be used, for example a fixed bed reactor, a stirred tank reactor, an ebullated bed reactor, a slurry type reactor, etc., preferably a fixed bed reactor.

[0066] Hydrotreatment (i) may 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 of dihydrogen to feedstock may be 100 to 2000 Nl / I.

[0067] This hydrotreatment (i) can implement one or more reactions chosen from hydrodeoxygenation, decarboxylation and decarbonylation.

[0068] The hydrodeoxygenation is preferably carried out in continuous fixed bed reactors, continuous stirred tank reactors or slurry type reactors containing a solid catalyst which may be selected from oxides or sulfides of Ni, Mo, W, Co or mixtures such as NiW, NiMo, CoMo, NiCoW, NiCoMo, NiMoW and CoMoW as the catalytic phase, preferably supported on carbon, alumina, silica, zeolite, titania or zirconia or mixtures thereof.

[0069] The 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), for example 6 MPa, and with a dihydrogen / oil ratio of 100 to 2000 NI H2 / I, but preferably 350 to 1500 NI H2 / I, for example 800 NI H2 / I of oil.

[0070] Decarboxylation and / or decarbonylation is preferably carried out in the presence of a solid catalyst in batch-type tank reactors, continuous fixed-bed reactors, continuous stirred-tank reactors or slurry reactors. Decarboxylation and / or decarbonylation can be carried out directly with glycerides, any esters or with free fatty acids.

[0071] The catalyst can be chosen from:

[0072] - oxides or sulfides of Ni, Mo, W, Co, NiW, NiMo, CoMo, NiCoW, NiCoMo, NiMoW and CoMoW as catalytic phase, preferably supported on carbon, alumina, silica, titanium oxide, zirconia, zeolite or on mixed supports.

[0073] - metals or mixtures of alloys from group 10 (Ni, Pt and Pd) and group 11 (Cu and Ag) supported by carbon, magnesia, zinc oxide, spinels (Mg2Al2O4, ZnA^CU), perovskites (BaTiOs, ZnTiOs), calcium silicates (such as xonotlite), alumina, silica or silica-aluminas or mixtures thereof,

[0074] - basic oxides, such as alkali metal oxides, alkaline earth oxides, lanthanide oxides, zinc oxide, spinels (Mg2Al2O4, ZnA^CU), perovskites (BaTiOs, ZnTiOs), calcium silicates (such as xonotlite), either in bulk or dispersed on neutral or basic supports, on basic zeolites (such as alkali or alkaline earth zeolites with low silica / alumina content obtained by exchange or impregnation).

[0075] For optimum performance and stable continuous operation, it is preferable that the active metal component of the catalyst in the case of Ni, Mo, W, Co or mixtures, is in the form of sulfides. It is therefore preferable that traces of decomposable sulfur compounds (thermally or catalytically) are present or added intentionally to the feedstock in order to maintain the metal sulfide in its sulfide state. For example, these sulfur compounds can be H2S, COS, CS2, mercaptans (e.g., methyl sulfide), thioethers (e.g., DiMethylSulfide), disulfides (e.g., DiMethyldiSulfide), thiophene and tetrahydrothiophene compounds.

[0076] Decarboxylation and / or decarbonylation is carried out in the presence of dihydrogen which stabilizes the catalytic activity by removing strongly adsorbed unsaturated species (e.g. when decarbonylation is the predominant reaction pathway) from the catalyst surface by 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.

[0077] 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 of dihydrogen to feedstock can be 100 to 2000 Nl / I.

[0078] 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.

[0079] Part of this hydrocarbon fraction, after separation, can be returned to the hydrotreatment inlet, in particular upstream of a deoxygenation reaction in order to absorb the heat of reaction, dilute the remaining impurities or provide more dihydrogen in dissolved form.

[0080] 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 at least partially isomerize the n-paraffins into isoparaffins.

[0081] Thus, in one embodiment, the first renewable component may be a diesel fraction of a hydrotreated and isomerized oil.

[0082] In this case, the effluent leaving the hydrotreatment 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, we speak of hydroisomerization.

[0083] Isomerization catalysts are typically bifunctional catalysts comprising an acid function and a (de)hydrogenating function.

[0084] The acid function is generally provided by an amorphous or crystalline support, typically presenting a specific surface area of ​​100 to 700m 2 / g and having an acidic surface, such as halogenated aluminas (in particular fluorinated or chlorinated) or phosphated or sulphurised, amorphous silica-aluminas (possibly containing boron), amorphous silica-aluminas-titaniums, sulphated zirconias, zirconias containing tungsten 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, ISI-1, KZ-2, ISI-4 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 which can be used alone or in 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 the absorbed molecules (pyridine, CO .. .), by a catalytic cracking test or by hydroconversion using a model molecule.

[0085] The (de)hydrogenation function is performed 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.

[0086] 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.

[0087] Examples of catalysts having an isomerization 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.

[0088] Preferably, the isomerization catalyst contains SAPO-11 or SAPO-41 or ZSM-22 or ZSM-23 or ferrierite and Pt, Pd or Ni and AI2O3 or SiCh. Typical isomerization catalysts are, for example, Pt / SAPO-11 / AI2O3, Pt / ZSM-22 / AI2O3, Pt / ZSM-23 / A Os and Pt / SAPO-11 / SiC>2. The catalysts may be used alone or in combination. The presence of hydrogen is particularly preferred to reduce catalyst deactivation. Particularly preferably, the isomerization catalyst may be a bifunctional noble metal catalyst, such as Pt-SAPO and / or Pt-ZSM catalyst, which is used in combination with hydrogen.

[0089] The isomerization step (ii) may 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 6 MPa (absolute).

[0090] The hourly space velocity can be from 0.1 to 20 h' 1, more preferably 0.2 to 10 h -1 and more preferably from 0.3 to 4 h' 1 . The dihydrogen-containing gases are introduced simultaneously with the feedstock at a ratio of 75 to 2500 NL(H2) / L of liquid feedstock, more preferably 150 to 1500 or more preferably 250 to 1000 NL(H2) / L of liquid feedstock.

[0091] 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 (generally less than 5% by mass), isomerization leads to a significant increase in the isoparaffin content. More specifically, it is preferable that the content (% by mass) of isoparaffins is increased by the isomerization step by at least 30 percentage points, more preferably by at least 50 percentage points, more preferably by at least 60 percentage points, more preferably by at least 70 percentage points.

[0092] This isomerization step (ii) can be implemented at the end of the hydrotreatment step (i), for example by installing an isomerization catalyst bed downstream of the hydrotreatment catalytic bed(s).

[0093] The effluent produced by hydrotreatment step (i) or isomerization step (ii) may be fractionated to separate a liquid fraction and non-condensable fractions and / or unreacted dihydrogen, which may then be reused.

[0094] In the present invention, it is the diesel fraction from hydrotreatment step (i) or isomerization step (ii) which is used as the renewable component. This diesel fraction typically corresponds to the liquid fraction of the hydrotreated or hydrotreated and isomerized effluent.

[0095] This diesel fraction may typically have an initial boiling point of 80 to 180°C and a final boiling point less than or equal to 360°C, preferably less than or equal to 320°C, in particular measured according to the ASTM D86-12 standard.

[0096] 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 the ASTM D2500-17a standard, or in any interval defined by two of these limits, a C8 to C24 paraffin content, most often from C8 to C20, of 95 to 100% by mass, advantageously at least 97% by mass, at least 98% by mass or at least 99% by mass, or in any interval defined by two of these limits, an iso-paraffins / n-paraffins mass ratio of 1.2 to 4.2, advantageously from 1.3 to 4, or in any interval defined by two of these limits.

[0097] A diesel fraction having one or more of these characteristics, in particular at least the paraffin content and / or at least the aforementioned cloud points and iso-paraffin / n-paraffin mass ratio, may represent 0.1 to 10% by volume of the hydrocarbon feedstock of the present invention, preferably 1 to 5% by volume. Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160°C and a final boiling point according to the ASTM D86-12 standard of 220°C to 300°C.

[0098] In a preferred embodiment, the diesel fraction used in the present invention may have one or more of the following characteristics: a cloud point of -45°C to +10°C, preferably -45°C to +5°C, more preferably -45°C to -5°C, even more preferably -45°C to -10°C or -40°C to -10°C, in particular measured according to ASTM D2500-17a, or in any interval defined by two of these limits, a C8 to C24 paraffin content, most often C8 to C20, of 95 to 100% by mass, preferably 97 to 100% by mass, more preferably 98 to 100% by mass, or in any interval defined by two of these limits, an iso-paraffins / n-paraffins mass ratio of 1.2 to 30, preferably 1, 3 to 30, more preferably 2 to 30, even more preferably 3 to 21, most often 3 to 15, although higher values ​​(e.g. up to 30) are not excluded,or in any interval defined by two of these limits.,

[0099] A diesel fraction having one or more of these characteristics, in particular at least the paraffin content and / or at least the aforementioned cloud points and iso-paraffin / n-paraffin mass ratio, may represent 0.1 to 10% of the volume of the hydrocarbon feedstock of the present invention, preferably 1 to 10% of the volume, more preferably 2 to 10% of the volume, even more preferably 3 to 10% by volume. Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most - 47 °C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47 °C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160 °C and a final boiling point according to the ASTM D86-12 standard of 220 °C to 300 °C.

[0100] The renewable component comprising, or consisting of, 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 less than or equal to 360°C, preferably less than or equal to 320°C, in particular measured according to the ASTM D86-12 standard, 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, in particular measured according to the ASTM D2500-17a standard, or in any interval defined by two of these limits, a C8 to C24 paraffin content, 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 in any interval defined by two of these limits, an iso-paraffins / n-paraffins mass ratio of 1.2 to 4.2, advantageously of 1,3 to 4 or in any interval defined by two of these limits.,

[0101] A component of renewable origin having one or more of these characteristics, in particular at least the paraffin content and / or at least the aforementioned cloud points and iso-paraffin / n-paraffin mass ratio, may represent 0.1 to 10% of the volume of the hydrocarbon feedstock of the present invention, preferably 1 to 5% of the volume. Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160°C and a final boiling point according to the ASTM D86-12 standard of 220°C to 300°C.

[0102] In a preferred embodiment, the renewable component comprising, or consisting of, a diesel fraction of a hydrotreated oil used in the present invention may have one or more of the following characteristics: a cloud point of -45°C to +10°C, preferably -45°C to +5°C, more preferably -45°C to -5°C, even more preferably -45°C to -10°C or -40°C to -10°C, in particular measured according to ASTM D2500-17a, or in any interval defined by two of these limits, a C8 to C24 paraffin content, most often C8 to C20, of 95 to 100% by mass, preferably 97 to 100% by mass, more preferably 98 to 100% by mass, or in any interval defined by two of these limits, a mass ratio iso-paraffins / n-paraffins from 1.2 to 30, preferably from 1.3 to 30, more preferably from 2 to 30, even more preferably from 3 to 21, most often from 3 to 15,although higher values ​​(e.g. up to 30) are not excluded, or in any interval defined by two of these limits.,

[0103] A component of renewable origin having one or more of these characteristics, in particular at least the paraffin content and / or at least the aforementioned cloud points and iso-paraffin / n-paraffin mass ratio, may represent 0.1 to 10% of the volume of the hydrocarbon feedstock of the present invention, preferably 1 to 10% of the volume, more preferably 2 to 10% of the volume, even more preferably 3 to 10% by volume. Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160°C and a final boiling point according to the ASTM D86-12 standard of 220°C to 300°C.

[0104] In particular, in the above each interval given for a characteristic of the diesel fraction or of the component of renewable origin, can be combined with each of the intervals given for one and / or the other characteristic. Preferably, the most general and / or preferred ranges are combined with each other, the narrowest and / or more preferred ranges are combined with each other.

[0105] Renewable component comprising fatty acid alkyl esters

[0106] In one embodiment, the hydrocarbon feedstock may comprise a second component of renewable origin which comprises, or consists of, fatty acid alkyl esters, the second component of renewable origin representing at most 5% of the total volume of the hydrocarbon feedstock, for example from 0.1 to 5% of the total volume of the hydrocarbon feedstock. The content of the hydrocarbon feedstock subjected to step a) in second component of renewable origin may be at most 1% by volume.

[0107] Advantageously, the fatty acid alkyl esters are fatty acid methyl esters, fatty acid methyl esters or mixtures thereof.

[0108] Fatty acid alkyl esters are typically obtained by a step (iii) of transesterification of oil(s) of natural origin with an alcohol, advantageously methanol or ethanol.

[0109] During the transesterification step (iii), the triglycerides contained in the oil(s) of natural origin 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 an acid or basic, homogeneous or heterogeneous 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.

[0110] This reaction is carried out, for example, in the presence of acid catalysts (hydrochloric acid, sulfuric acid, sulfonic acid, boron trifloride, zinc chloride, acid ion exchangers, aluminum trioxide, iron trioxide, etc.) or in the presence of basic catalysts such as alkali metal alcoholates and hydroxides as well as sodium or potassium carbonates (sodium hydroxide, potassium hydroxide, sodium ethanolate, potassium ethanolate, etc.).

[0111] The transesterification reaction can also be carried out under supercritical conditions, where the reaction is carried out 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 conditions and catalysts that can be used are described in "Transesterification in Supercritical Conditions" Somkiat Ngamprasertsith et al, Biodiesel - Feedstocks and Processing Technologies, November 2011, chapter 12, pages 247-268. In the absence of a catalyst, for example, it is possible to operate at temperatures of 280-350°C, pressures of 19 to 35 MPa, an alcohol / oil molar ratio of 24:1 to 42:1 and a reaction time of 5 to 30 min.

[0112] The fatty acid alkyl esters used in the present invention can therefore advantageously be free of impurities such as unsaponifiable compounds, soaps, or other compounds originating from animal fats or used cooking oils used as raw material. In particular, their unsaponifiable content can advantageously be less than or equal to 1% by mass (measured according to standard ISO 3596:2001).

[0113] The oil of natural origin may be as previously described. In a preferred embodiment, this oil of natural origin is chosen from an animal fat and / or a used oil, and in particular from an animal fat and / or a used oil having waste status, which makes it possible to further reduce the environmental impact of the fluids produced by the method 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, less than or equal to 1% by mass.

[0114] 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.

[0115] Preferably, the content of alkyl esters of fatty acids, and in particular methyl or ethyl esters of fatty acids, the carbon chain of which contains from 20 to 22 carbon atoms, will be as low as possible, advantageously less than or equal to 2%m, or even 1% by mass, preferably zero, in order to improve the cold properties and in particular the freezing point.

[0116] Alternatively or in combination, the fatty acid alkyl esters, and in particular the fatty acid methyl or ethyl esters, may 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.

[0117] Advantageously, in particular when produced from animal fats and / or used cooking oils which are animal by-products, the alkyl esters of fatty acids, and in particular the methyl or ethyl esters of fatty acids, may comprise at least one of the following characteristics: at least 9%m, typically from 9%m to 64%m, of methyl esters of fatty acids whose carbon chain contains from 12 to 16 carbon atoms, at least 25%m, typically from 30%m to 98%m, of methyl esters of fatty acids whose carbon chain contains 18 carbon atoms, at most 4%m, typically from 0%m to 2%m, of methyl esters of fatty acids whose carbon chain contains from 20 to 22 carbon atoms.

[0118] When these esters are produced from animal by-products which are animal fats, the fatty acid alkyl esters, and in particular the fatty acid methyl or ethyl esters of fatty acids, may comprise at least one of the following characteristics: at least 20%m, typically from 20%m to 64%m, of fatty acid methyl esters whose carbon chain contains from 12 to 16 carbon atoms, at least 25%m, typically from 25%m to 65%m, of fatty acid methyl esters whose carbon chain contains 18 carbon atoms, at most 4%m, typically from 0%m to 2%m, of fatty acid methyl esters whose carbon chain contains 20 carbon atoms, at most 1%m, typically from 0%m to 1%m, of methyl esters fatty acids whose carbon chain contains 22 carbon atoms.

[0119] The process according to the invention can thus comprise a step of providing alkyl esters of fatty acids, by transesterification of oils of natural origin with an alcohol, preferably with methanol, ethanol or their mixtures.

[0120] 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 gasification of biomass, pyrolysis of biomass, or by fermentation or by anaerobic digestion of biomass in the presence of one or more microorganisms, possibly followed by partial oxidation of the biogas in the presence of oxygen). These processes are well known to those skilled in the art.

[0121] Hydrocarbon charge

[0122] The hydrocarbon feedstock introduced in step a) of the present invention contains a hydrocarbon component of fossil origin and the component of renewable origin comprising (or consisting of) a diesel fraction of a hydrotreated oil (or of a hydrotreated and isomerized oil) in a content of at most 10% by volume, preferably at most 9% or 8% or 7% or 6% or 5% by volume relative to the hydrocarbon feedstock. In one embodiment, the content of this component of renewable origin in the hydrocarbon feedstock may be at most 4%, 3%, 2%, or 1% by volume. Advantageously, the content of this component of renewable origin in the hydrocarbon feedstock may be at least 0.1% by volume, advantageously at least 0.5% by volume.

[0123] In particular, the content of this renewable component of the hydrocarbon feedstock may be included in any interval defined by any two of the aforementioned limits.

[0124] In one embodiment, the content of renewable component of the hydrocarbon feedstock comprising (or consisting of) a diesel fraction of a hydrotreated oil (or of a hydrotreated and isomerized oil) is maximum, in particular close to 10% by volume, for example from 2 to 10% by volume, or even from 3 to 10% by volume, when said renewable component has a low cloud point, for example from -45°C to -5°C, from -45°C to -10°C or from -40°C to -10°C, and / or a high iso-paraffins / n-paraffins mass ratio, for example from 2 to 30 or from 3 to 21, most often from 3 to 15, although higher values ​​(for example up to 30) are not excluded.Preferably, the hydrocarbon component of fossil origin used, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160°C and a final boiling point according to the ASTM D86-12 standard of 220°C to 300°C.

[0125] Advantageously, the content of component of renewable origin comprising alkyl esters of fatty acids, in particular methyl and / or ethyl esters of fatty acids, of the hydrocarbon feedstock may be from 0% by volume to 5% by volume, advantageously from 0 to 1% by volume, for example at most 0.9% or 0.6% or 0.5% by volume, or in any interval defined by two of these limits. When the hydrocarbon feedstock comprises a component of renewable origin comprising (or consisting of) alkyl esters of fatty acids, the content of this second component in the hydrocarbon feedstock may advantageously be at least 0.1% by volume.

[0126] Thus, advantageously, the hydrocarbon feedstock comprises, or is made up of, the hydrocarbon component of fossil origin, the component of renewable origin comprising (or made up of) a diesel fraction of a hydrotreated oil (or of a hydrotreated and isomerized oil), and optionally the second component of renewable origin.

[0127] In particular, provision may be made to adjust the content of renewable component comprising (or consisting of) a diesel fraction of a hydrotreated oil, and optionally the content of renewable component comprising (or consisting of) fatty acid alkyl esters, of the hydrocarbon feedstock in the aforementioned ranges so that the kerosene fraction recovered at the outlet of fractionation step b) has a freezing point of at most - 47°C. Alternatively or in combination, the cutting points of the kerosene fraction recovered during fractionation step b) may be adapted in order to recover a kerosene fraction having a freezing point of at most - 47°C.

[0128] The hydrocarbon feedstock can be prepared by simple mixing of the components, in particular upstream of the hydrotreatment stage a), or during stage a).

[0129] It will thus be possible to provide for mixing the components of the hydrocarbon feedstock upstream of the at least one hydrotreatment reactor in which step a), or inside this at least one reactor, is carried out.

[0130] Step a) Step a) of hydrotreatment of the hydrocarbon feedstock can be carried out in one or more reactors. Any type of reactor normally used for this type of reaction can be used, for example a fixed-bed reactor, an ebullated-bed reactor, a slurry reactor, etc., preferably a fixed-bed reactor.

[0131] In particular, it will be possible to use a reactor of the type normally used for the hydrotreatment of fossil hydrocarbons.

[0132] Advantageously, step a) can be carried out under a pressure of 15 to 130 bars and at a temperature of 250 to 380°C, preferably 280 to 340°C, in the presence of dihydrogen and at least one hydrotreatment catalyst.

[0133] Typically, we can predict a liquid hourly space velocity (WH in French, LHSV in English - Liquid Hourly Space Velocity): from 0.2 to 9 hr 1 , preferably 0.5 to 7 hr 1 , and more preferably 0.8 to 1.8 hr 1 , and a dihydrogen ratio: 50 to 1500 Nm 3 / m 3 load, preferably 120 to 250 Nm 3 / m 3 and more preferably 120 to 200 Nm 3 / m 3 .

[0134] Step a) may typically be carried out in at least one fixed bed reactor, comprising one or more catalyst beds.

[0135] More specifically, step a) can be carried out under a pressure of 15 to 50 bars and at a temperature of 280°C to 340°C, in the presence of dihydrogen and at least one hydrotreatment catalyst, typically with a dihydrogen content of 120 to 180 Nm 3 / m 3 of charge. Typically, we can predict an hourly space velocity of the liquid of 1 to 1.6 h -1 .

[0136] The hydrotreatment catalyst is a conventional hydrotreatment catalyst. Conventional hydrotreatment catalysts include, in particular, an active metal compound such as nickel, platinum, palladium, rhenium, rhodium, nickel tungstate, nickel molybdenate, molybdenum, cobalt molybdenate, nickel molybdenate, this metal compound may or may not be deposited on a support. This support may generally include oxides such as silicas, aluminas, aluminosilicates (in particular zeolites), titanium oxides, or carbon oxides, molecular sieves, salts or alkaline earth metals. When a support is present, it advantageously has a specific surface area ranging from 100 to 250 m 2 / g, preferably 150 to 200 m 2 / g.

[0137] 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 CoNiMo, preferably on an alumina support.

[0138] 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.

[0139] In a preferred embodiment, the catalyst used does not have an isomerizing function or has negligible isomerizing activity under the reaction conditions. In other words, the catalyst does not promote the isomerization of the hydrocarbon compounds present in the feedstock. When a support is present, it is preferably slightly acidic or not at all.

[0140] Thus, a catalyst not having 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, phosphated alumina, borated alumina, phosphated silica alumina, alone or as a mixture.

[0141] In a preferred embodiment, such a catalyst consists of one or more active metal compound(s), preferably one, two or three active metal compounds, said active metal compound being chosen from nickel, cobalt and molybdenum, said metal compound being optionally deposited on a support chosen from alumina, silica alumina, phosphated alumina, borated alumina, phosphated silica alumina, alone or as a mixture, preferably on an alumina support. This catalyst may in particular be chosen from the oxides or sulfides of Ni, Mo, Co, NiMo, CoMo, NiCoMo, as catalytic phase, optionally on a support chosen from alumina, silica alumina, phosphated alumina, borated alumina, phosphated silica alumina, alone or as a mixture, preferably alumina.

[0142] The use of this type of catalyst is particularly advantageous when the component of renewable origin has one or more of the characteristics (i) to (iv) listed below, preferably characteristics (ii) and (iv), or (ii), (iii) and (iv):

[0143] (i) 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,

[0144] (ii) a cloud point of -45°C to +10°C, preferably -45°C to +5°C, more preferably -45°C to -5°C, even more preferably -45°C to -10°C or -40°C to -10°C,

[0145] (iii) a content of C8 to C24 paraffins, most often C8 to C20, of 95 to 100% by mass, preferably 97 to 100% by mass, more preferably 98 to 100% by mass,

[0146] (iv) a mass ratio of iso-paraffins / n-paraffins of 1.2 to 30, preferably of 1.3 to 30, more preferably of 2 to 30, even more preferably of 3 to 21, most often of 3 to 15, although higher values ​​(for example up to 30) are not excluded. Preferably, the hydrocarbon component of fossil origin used in the present invention, in particular when it is a kerosene cut or a mixture of kerosene cuts, then has a freezing point of at most -47°C (measured according to ASTM D5972-23 or IP435), typically from -70 to -47°C, and / or an initial boiling point according to the ASTM D86-12 standard of 130 to 160°C and a final boiling point according to the ASTM D86-12 standard of 220°C to 300°C.

[0147] The use of a non-isomerizing hydrotreatment catalyst is particularly preferred when the renewable component has a low cloud point, for example from -45 °C to -5 °C, from -45 °C to -10 °C or from -40 °C to -10 °C, and / or a high iso-paraffins / n-paraffins mass ratio, for example from 2 to 30 or from 3 to 21, most often from 3 to 15, although higher values ​​(for example up to 30) are not excluded.

[0148] The hydrotreatment step can then be implemented at a lower cost, without requiring the use of expensive catalysts with an isomerizing function comprising expensive metals such as tungsten or platinum. In other words, the hydrotreatment step can be implemented without modification of the implementation conditions, nor modification of the catalyst, compared to an implementation without addition of a renewable component, while making it possible to obtain at the end of fractionation step b) a kerosene cut meeting the desired specifications, for example those of an A1 jet according to standard ASTM D1655-21, in particular at least with regard to the final distillation point and / or the freezing point and / or the flash point.

[0149] The hydrotreatment step a) produces an effluent containing a liquid fraction containing the kerosene fraction, and a gaseous fraction.

[0150] Step b)

[0151] 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.

[0152] After the hydrotreatment stage, the effluent leaving the reactor is fractionated, typically by stripping, in order to recover a kerosene cut. This fractionation can be implemented so that the kerosene cut forms a jet fuel, in particular meeting the desired specifications.

[0153] The recovered kerosene fraction has a final boiling point less than or equal to 300°C, notably measured according to the ASTM D86-12 standard.

[0154] The initial boiling point according to ASTM D86-12 may be 120 to 185°C. The final boiling point according to ASTM D86-12 may be 220 to 300°C. The recovered kerosene fraction may advantageously have one or more of the following properties: a kinematic viscosity at -20°C of 1.2 to 8.0 mm 2 / s (NF EN ISO 3104-August 1996), a density at 15°C of 775 to 840 kg / m 3 (ASTM D4052-18 or IP 365), a freezing point of not more than -47°C (ASTM D5972-23 or IP435), a flash point of not less than 38°C (IP170-21 or ASTM D56-21A).

[0155] In particular, the cutting points of the recovered kerosene fraction may be adapted in order to obtain a kerosene fraction meeting the desired specifications, for example those of an A1 jet according to standard ASTM D1655-21, in particular at least with regard to the final distillation point and / or the freezing point and / or the flash point.

[0156] The fractionation stage also makes it possible to recover the gas produced, in particular methane, during the hydrotreatment stage.

[0157] Description of the single figure

[0158] [Fig. 1] is a simplified diagram of a hydrotreatment unit for implementing the method according to one embodiment of the invention.

[0159] This unit 1 comprises 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 hydrotreatment catalysts.

[0160] 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 a hydrotreated oil. Optionally, the feedstock (C) may also contain another component of natural origin comprising alkyl esters of fatty acids. In the example, the different components of the feedstock (C) are introduced simultaneously, however it could be provided to introduce them separately.

[0161] A line 4 recovers the effluent at the outlet of reactor 2 and leads it to a separation section 5.

[0162] A heat exchanger 6 is placed downstream of the reactor on line 4 in order to heat the load circulating in line 3, upstream of the reactor.

[0163] 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.

[0164] Downstream of heat exchanger 6, and upstream of reactor 2, the feed mixed with the H2-rich gas circulating in line 3 is heated by a furnace 8. Thus, the feed is mixed with the hydrogen-rich gas, then brought to the reaction temperature by heat exchanger 6 and furnace 8 before entering reactor 2. It then passes into reactor 2.

[0165] At the outlet of the reactor, the mixture obtained is cooled, then separated in separation section 5, for example by stripping, which makes it possible to obtain:

[0166] - a gaseous fraction (G), containing in particular water from stripping, gaseous hydrocarbons, an acid gas rich in H2S, part of which is here reinjected into the gas rich in H2 mixed with the feed, by means of a line 9,

[0167] - a kerosene cut (K). The example below illustrates the invention without limiting its scope.

[0168] Example

[0169] Two kerosene cuts taken from the outlet of an atmospheric crude distillation unit were mixed with different components of renewable origin.

[0170] The characteristics of the fossil kerosene cuts used, noted “Kero-1” and “Kero-2” are presented in Table 1 below.

[0171] [Table 1] Characteristics of kerosene cuts Four components of renewable origin were used: “HVO -23.5°C”, “HVO -17°C”, “HVO -11°C”, “HVO +4°C” which are hydrotreated and isomerized oils with cloud points of approximately -23.5°C, -17°C, -11°C and +4°C respectively. The main characteristics of these feedstocks are presented in Tables 2 and 3. The distribution of iso-paraffins and n-paraffins was determined by reversed-phase GCxGC-FID analysis.

[0172] [Table 2] Characteristics of renewable components [Table 3] Characteristics of the renewable component HVO -23.5°C

[0173] The catalyst used is a CoMo type catalyst. The operating conditions are presented in Table 4.

[0174] [Table 4] Hydrotreatment operating conditions The freezing point (denoted FP) was determined for the effluents obtained for each load, the results are presented in Table 5 below. Each of these effluents corresponds to the liquid fraction leaving the reactor, after separation of the gases.

[0175] In this table 5, AFP corresponds to the difference (noted) 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.

[0176] It is observed that the cold properties are little modified when components of renewable origin are incorporated in co-processing. In addition, the quantity of component of renewable origin can be adjusted so that the resulting mixture has a freezing point of at most -47°C. It will be noted that up to 10% by volume of a component of renewable origin can be incorporated, as shown by the freezing points of the mixtures comprising the kerosene cut Kero-1, which remain well below the maximum value of -47°C.

[0177] Tables 6 and 7 bring together the other properties of the effluents obtained during the co-processing of Kero-1 and Kero-2 with the components of renewable origin, more precisely of the 140°C+ fraction of the effluent leaving the hydrotreatment reactor.

[0178] It is noted that the 140°C+ fractions of the effluents obtained meet most of the specifications of an A1 jet.

[0179] [Table 6] Co-processing Kero-1 and components of renewable origin HVO -17°C, HVO -11°C and HVO +4°C

[0180] [Table 7] Coprocessing Kero-2 and components of renewable origin HVO -17°C, HVO -11°C and HVO +4°C

[0181]

Claims

CLAIMS 1. A process 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 process being characterized in that the hydrocarbon feedstock subjected to the hydrotreatment step a) further comprises a component of renewable origin consisting of a diesel fraction of a hydrotreated oil having a C8 to C24 paraffin content of 95 to 100% by mass, 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) in renewable component consisting of a diesel fraction of a hydrotreated oil is at least 0.1% by volume, preferably at least 1% by volume, more preferably at least 2% by volume, even more preferably at least 3% by volume.

3. A manufacturing method according to any one of claims 1 or 2, wherein the renewable component consisting of 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 -45°C to +10°C, preferably of -45°C to +5°C, more preferably of -45°C to -5°C, even more preferably of -45°C to -10°C or of -40°C to -10°C, - a C8 to C24 paraffin content, most often C8 to C20, of 97 to 100% by mass, more preferably 98 to 100% by mass, - an iso-paraffins / n-paraffins mass ratio of 1.2 to 30, preferably of 1.3 to 30, more preferably of 2 to 30, even more preferably of 3 to 21.

4. Manufacturing process according to any one of claims 1 to 3, in which 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 fossil-based hydrocarbon component comprises one or more of the following characteristics: the fossil-based hydrocarbon component is a kerosene fraction or a mixture of kerosene fractions, the fossil-based hydrocarbon component has a freezing point of at most -47°C measured according to ASTM D5972-23, the fossil-based hydrocarbon component 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.

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 catalyst hydrotreatment 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.

10. Manufacturing method according to any one of claims 1 to 9, in which step a) is carried out in the presence of at least one hydrotreatment catalyst consisting of one or more active metal compound(s), preferably one, two or three active metal compounds, said active metal compound being chosen from nickel, cobalt and molybdenum, said metal compound being optionally deposited on a support chosen from alumina, silica alumina, phosphated alumina, borated alumina, phosphated silica alumina, alone or as a mixture.

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