PROCESS FOR MANUFACTURING JET FUEL FROM FEEDSTOCKS OF RENEWABLE ORIGIN

Abstract

METHOD FOR PRODUCING A JET FUEL FROM FEEDSTOCKS OF RENEWABLE ORIGIN The invention relates to a method for producing a jet fuel comprising at least the steps of: a) providing fatty acid methyl esters from the reaction of animal fats and / or used cooking oils with methanol in a transesterification reactor, b) providing hydrocarbons of fossil origin, c) preparing a hydrocarbon feedstock containing the hydrocarbons of fossil origin provided by step b) and the fatty acid methyl esters provided by step a) in a content of at most 5% vol relative to the hydrocarbon feedstock, d) subjecting the hydrocarbon feedstock prepared in step c) to hydrotreatment and obtaining a treated hydrocarbon feedstock, e) fractionating the treated hydrocarbon feedstock obtained in step d) and recovering a kerosene fraction as jet fuel having a final boiling point less than or equal to 300°C.

Description

Title of the invention: METHOD FOR MANUFACTURING A JET FUEL FROM RE ORIGINAL CHARGES NEW Technical field

[0001] 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 a jet fuel having a component of biological (or renewable) origin. Background to the invention

[0002] Conventional jet fuels, also known as "jet fuel", "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 cut points of the jet fuel fraction typically vary between 140°C and 240°C.

[0003] A commercial jet fuel is typically obtained by blending different fuel bases. These fuel bases may be crude oil distillation cuts, possibly hydrotreated or sometimes subjected to a sweetening treatment (MEROX process for example). These bases may also be cuts from a hydrocracker effluent or an effluent from a catalytic cracker (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 so that the final properties of the blend meet the desired specifications.

[0004] Due to the scarcity of fossil resources and increasing 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 constitutes a real economic and environmental challenge. In particular, certain countries such as France are implementing incentive taxes relating to the incorporation of renewable energy in transport and in particular for the aviation sector. Prior art

[0005] A solution for obtaining jet fuel with an original component Biological jet fuel production consists of mixing a conventional jet with a paraffinic base from renewable feedstocks as provided for by the D7566-21 standard, thus enabling the production of alternative aviation fuels. The bases for aviation fuel from renewable feedstocks that can be incorporated into fossil jet fuels are: • Synthetic paraffinic kerosenes [SPK], produced by processes such as the Fischer-Tropsch process, the hydrotreatment of esters and fatty acids [HEFA-SPK] or produced by the Alcohol-to-jet route (transformation of alcohol into kerosene) [ATJ-SPK], • Synthetic isoparaffins produced by hydrotreatment from 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 hydrocarbons, esters and hydrotreated fatty acids.

[0006] This solution, however, requires specific processing installations to produce the paraffinic bases which will be mixed with the conventional jet.

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

[0008] Thus, document EP2346962 describes a process for obtaining a kerosene cut, a portion 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 cut. 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.

[0009] Document EP2533895 describes a specific catalyst for producing biodiesel. It describes in particular the use of this catalyst for treating a feedstock which is a mixture of a hydrocarbon of fossil origin (kerosene, diesel, etc.) and a biomass chosen from vegetable or animal oils and fats. The oils and / or fats used are not transesterified. The production of jet is not mentioned.

[0010] Furthermore, document EP3813539 describes a process for producing a purified biodiesel from renewable raw materials (such as fats and oils) containing unsaponifiable matter. The process comprises esterifying vegetable oils or fats to obtain a crude biodiesel which is then subjected to distillation to produce a purified biodiesel and a distillation bottoms. This The latter contains more than 2% by mass of unsaponifiables as well as soaps, phospholipids, proteins, colored compounds, sulfur compounds, high-boiling compounds containing acidic or basic groups, and mono-, di- and triglycerides. This distillation bottoms is then diluted with a fossil-based feedstock of the middle distillate type, before being subjected to a hydrodeoxygenation step in order to produce diesel-type hydrocarbons. Jet production is not mentioned.

[0011] Among the feedstocks of renewable origin available today, feedstocks having the status of animal by-products within the meaning of European Regulation 1069 / 2009 and its implementing acts (EU) 142 / 2011, such as animal fats or used cooking oils (also designated by the acronym UCO for "Used Cooking Oil" in English), are interesting in order to limit the environmental impact of the fuel produced. These feedstocks are however subject to restrictive health regulations. The use of these feedstocks entails traceability constraints and health controls associated in particular with the management of aqueous effluents. Furthermore, the use of these feedstocks having the status of animal by-products requires compliance with the time / temperature and pressure conditions as recommended in European Regulation 1069 / 2009, these conditions not being met by a hydrotreatment step alone.There is therefore a need for a process for manufacturing jet fuel by co-treatment in a hydrotreatment unit, in particular from feedstocks of renewable origin having the status of animal by-products, which makes it possible to overcome the aforementioned problems. Description of the invention

[0012] The invention provides a method for manufacturing a jet fuel comprising at least the steps of:

[0013] a) providing fatty acid methyl esters from the reaction of animal fats and / or used cooking oils with methanol in a transesterification reactor,

[0014] b) supply hydrocarbons of fossil origin,

[0015] c) preparing a hydrocarbon feedstock containing the hydrocarbons of fossil origin provided by step b) and the fatty acid methyl esters provided by step a) in a content of at most 5% vol relative to the hydrocarbon feedstock,

[0016] d) subjecting the hydrocarbon feedstock prepared during step c) to hydrotreatment and obtaining a treated hydrocarbon feedstock,

[0017] e) fractionating the treated hydrocarbon feedstock obtained in step d) and recovering a kerosene fraction as jet fuel, said kerosene fraction having a final boiling point of less than 300°C, measured in particular according to standard ASTM D86-12.

[0018] The process according to the invention thus makes it possible to obtain an aviation fuel of which a part is of renewable origin, also called SAF for “Sustainable Aviation Fuel” in English.

[0019] In particular, the method according to the invention can be implemented in existing hydrotreatment units. Detailed description of the invention

[0020] 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.

[0021] 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.

[0022] Boiling points as mentioned herein 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 DI 160-18 for distillates. Animal fats and used cooking oils

[0023] The animal fats and used cooking oils from which the methyl esters used in the present invention are derived are advantageously animal fats and used cooking oils having the status of animal by-products, in particular within the meaning of Regulation (EC) No. 1069 / 2009 of the European Parliament and of the Council of 21 October 2009 and Regulation (EU) No. 142 / 2011 of the Commission (implementing regulation of Regulation EC No. 1069 / 2009).

[0024] Animal fats having the status of animal by-product are fatty residues of animal origin, other than used cooking oils, originating for example from food industries or rendering plants.

[0025] Used cooking oils with the status of animal by-products are used cooking oils (used cooking oils or UCO), namely residues of fatty substances of vegetable or animal origin used for human consumption, in the food industry, in collective catering or commercial commercial. Step a)

[0026] The fatty acid methyl esters provided in step a) are derived from the reaction of animal fats and / or used cooking oils with methanol in a transesterification reactor.

[0027] In particular, this step a) may thus comprise, or consist of, a step of transesterification of animal fats and / or used cooking oils with methanol to obtain methyl esters of the fatty acids initially contained in the animal fats and / or used cooking oils, and glycerin, followed by a step of separation by distillation, decantation or centrifugation of the methyl esters produced.

[0028] During the transesterification step, the triglycerides contained in animal fats and / or used cooking oils react with methanol to obtain methyl esters of 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 a methanol / oil molar ratio of 3:1 to 15:1 may be used.

[0029] This reaction is for example carried out 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.).

[0030] The transesterification reaction can also be carried out under supercritical conditions can also be used, the reaction being carried out at high pressures of 15-35MPa, and, in some cases, at high temperatures of 250 to 280°C, or even higher (300-350°C). Under these supercritical conditions, the reaction can be carried out in the absence or presence of catalyst.

[0031] The fatty acid methyl esters used in the present invention are therefore free from 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 is advantageously less than or equal to 1% m / m (measured according to standard ISO 3596:2001).

[0032] Advantageously, in particular when they are produced from animal fats and / or used cooking oils which are animal by-products, the me- esters The fatty acid esters provided in step a) 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 0%m to 2%m, of methyl esters of fatty acids whose carbon chain contains 20 to 22 carbon atoms.

[0033] When these esters are produced from animal by-products which are animal fats, the fatty acid methyl esters provided in step a) may comprise at least one of the following characteristics: - at least 20%m, typically from 20%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 25%m to 65%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 20 carbon atoms, - at most 1%m, typically from 0%m to 1%m, of methyl esters of fatty acids whose carbon chain contains 22 carbon atoms.

[0034] Preferably, the content of methyl esters of fatty acids whose carbon chain contains from 20 to 22 carbon atoms will be as low as possible, preferably zero, in order to improve the cold properties and in particular the freezing point.

[0035] Step a) of supplying fatty acid methyl esters may in particular comprise (i) obtaining methanol of renewable origin, (ii) followed by the reaction of animal fats and / or used cooking oils with the methanol obtained in step (i) in a transesterification reactor.

[0036] By methanol of renewable origin is meant methanol obtained from biomass.

[0037] Step (i) can thus comprise: - an optional step of manufacturing synthesis gas comprising CO / H2 comprising one of the following steps: • a biomass gasification stage, • a biomass pyrolysis stage, • a stage of production of biogas containing methane and CO2, optionally by anaerobic digestion of biomass in the presence of one or more microorganisms, followed by partial oxidation of the biogas in the presence of oxygen, - a step of converting a synthesis gas comprising CO / H2 into methanol, especially in the presence of a catalyst.

[0038] Biomass may include, but is not limited to, wood fuels from natural forests and woodlands (e.g., sawdust), agricultural residues (e.g., rice hulls, straw manure), energy crops that are grown exclusively for energy production (e.g., corn and oil palm), municipal waste (e.g., wood waste, rice, straw manure), energy crops that are grown exclusively for energy production (e.g., corn and oil palm), municipal waste (e.g., municipal solid waste and wastewater), and waste-derived biomass fuel (e.g., wood pellets).

[0039] Methanol of renewable origin can in particular be obtained by conversion of a synthesis gas comprising CO / H2, this synthesis gas being derived from biomass. The conversion of a synthesis gas into methanol is well known to those skilled in the art.

[0040] The biomass can for example be gasified to produce a synthesis gas (or "syngas" in English) rich in CO / H2, this synthesis gas then being converted into methanol in the presence of a catalyst. A process of this type is for example described in document WO2018134853A1.

[0041] Synthesis gas suitable for subsequent conversion to methanol can also be obtained by pyrolysis of biomass.

[0042] A synthesis gas suitable for subsequent conversion to methanol can also be obtained by partial oxidation in the presence of dioxygen of a biogas containing methane and CO2, this biogas resulting for example from the anaerobic digestion of biomass in the presence of one or more microorganisms. A process of this type is for example described in document WO2019060988A1. Step b)

[0043] The fossil hydrocarbons usable in the present invention can be chosen from kerosene cuts.

[0044] 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. These kerosene cuts can be:

[0045] - a kerosene cut from the direct distillation of crude oil,

[0046] - a kerosene cut from different conversion processes such as cracking catalytic, hydrocracking and / or visbreaking.

[0047] In the context of hydrotreatment, the hydrocarbons of fossil origin are advantageously a kerosene cut or a mixture of kerosene cuts, preferably originating from the direct distillation of crude oil or from hydrocracking. Step c)

[0048] The hydrocarbon feedstock prepared in step c) contains the hydrocarbons of fossil origin provided by step b) and the fatty acid methyl esters provided by step a) in a content of at most 5% by volume relative to the hydrocarbon feedstock, advantageously at most 0.9% or 0.6% or 0.5% by volume.

[0049] Advantageously, the fatty acid methyl ester content of the hydrocarbon feedstock may be from 0.1% by volume to 1% by volume, preferably from 0.1% by volume to 0.9% by volume, or from 0.1% to 0.6% by volume, more preferably from 0.1% to 0.5% by volume, or in any included range defined by two of these limits.

[0050] This preparation step can be carried out by simple mixing of the constituents of the hydrocarbon feedstock supplied in steps a) and b), in particular upstream of the hydrotreatment step of step d), or during step d).

[0051] It will thus be possible to provide for mixing the constituents of the hydrocarbon feedstock supplied in steps a) and b) upstream of a hydrotreatment reactor in which step d) is carried out, or inside this reactor. Step d)

[0052] Step d) 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.

[0053] In particular, it will be possible to use a reactor of the type usually used for the hydrotreatment of hydrocarbons of fossil origin.

[0054] Advantageously, step d) is 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 a hydrotreatment catalyst and dihydrogen.

[0055] Typically, a liquid hourly space velocity (WH in French, LHSV in English - Liquid Hourly Space Velocity) may be provided: from 0.2 to 9 hr1, preferably 0.5 to 7, and more preferably 0.8 to 1.8, and a dihydrogen ratio: 50 to 1500 Nm3 / m3 of charge, preferably 120 to 250 Nm3 / m3 and more preferably 120 to 200 Nm3 / m3.

[0056] Step d) is typically carried out in a fixed bed reactor, comprising one or more catalyst beds.

[0057] More specifically, step d) 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 a hydrotreatment catalyst and dihydrogen, typically with a dihydrogen content of 120 to 180 Nm3 / m3 of feed. Typically, an hourly space velocity of the liquid of 1 to 1.6 h ' can be provided.

[0058] The hydrotreatment catalyst is a conventional hydrotreatment catalyst. Conventional hydrotreatment catalysts comprise 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 being able to be deposited or not on a support. This support can generally comprise oxides such as silicas, aluminas, alumino-silicates (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 varying from 100 to 250 m2 / g, preferably from 150 to 200 m2 / g.

[0059] Advantageously, the catalyst comprises 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.

[0060] When supported, conventional hydrotreating catalysts typically comprise a metal content of 0.01 to 25% by weight relative to the total mass of the catalyst, preferably 15 to 20% by weight, for example 20% by weight relative to the total mass of the catalyst.

[0061] 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 acidic.

[0062] 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.

[0063] The hydrotreatment step d) produces an effluent containing a liquid fraction containing the kerosene fraction, and a gaseous fraction. Step e)

[0064] The hydrotreated feed obtained at the outlet of step d) 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 even a stripping column.

[0065] After the hydrotreatment step, the effluent leaving the reactor is fractionated, typically by stripping, in order to recover a kerosene cut. This fractionation can be carried out so that the kerosene cut forms a jet fuel, in particular meeting the desired specifications.

[0066] The recovered kerosene fraction has a final boiling point less than or equal to 300°C, particularly measured according to ASTM D86-12.

[0067] 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.

[0068] The recovered kerosene fraction advantageously has 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 at most -47°C (ASTM D5972-16 or IP435), - a flash point of at least 38°C (IP170-21 or ASTM D56-21A).

[0069] 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 Al 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.

[0070] The fractionation step also makes it possible to recover the gas produced, in particular methane, during the hydrotreatment step. Description of figures

[0071] [Fig.l]: simplified diagram of a hydrotreatment unit allowing the implementation of the process according to an embodiment of the invention.

[0072] [Fig.l] represents a simplified diagram of a hydrotreatment unit 1 making it possible to implement the process according to the invention.

[0073] This unit 1 comprises a reactor 2 into which the feedstock to be treated is introduced by means of a line 3. This reactor contains one or more beds of hydrotreatment catalysts.

[0074] The feedstock (C), in the present invention, is a mixture of a kerosene feedstock of fossil origin and methyl esters of fatty acids of renewable origin.

[0075] A line 4 recovers the effluent at the outlet of reactor 2 and leads it to a separation section 5.

[0076] 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.

[0077] 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.

[0078] Downstream of the heat exchanger 6, and upstream of the reactor 2, the charge mixed with the H2-rich gas circulating in the line 3 is heated by a furnace 8.

[0079] Thus, the feedstock is mixed with the hydrogen-rich gas, then brought to the reaction temperature by the heat exchanger 6 and the furnace 8 before entering the reactor 2. It then passes into reactor 2.

[0080] At the outlet of the reactor, the mixture obtained is cooled, then separated in the separation section 5, for example by stripping, which makes it possible to obtain:

[0081] - a gaseous fraction (G), containing in particular water from stripping, gaseous hydrocarbons, an acid gas rich in H2S, part of which is reinjected into the H2-rich gas mixed with the feed, by means of a line 9,

[0082] - a kerosene cut (K).

[0083] The example below illustrates the invention without limiting its scope. Example

[0084] A kerosene cut taken from the outlet of an atmospheric crude distillation unit was mixed with different feedstocks of renewable origin.

[0085] The characteristics of the fossil kerosene cut used, noted “Kero” are presented in table 1 below.

[0086] [Tables 1] Characteristics Unit Method Density at 15°C kg / m3 ASTM D4052-18 0.798 Freezing point °C ASTM D2386-19 / D7153-15el / D5972-16 / IP435 (2016) -52.6 Sulfur ppm According to level (ASTM D2622-21 or ASTM D5453-19a) 126 Nitrogen ppm ASTM D4629-17 0 TBP ASTM D2887-19 ASTM D86-12 Initial point °C 98.2 10% distilled °C 155 20% distilled °c 167.6 30% distilled °c 176.8 40% distilled °c 187.6 50% distilled °c 197 60% distilled °c 208.6 70% distilled °c 219.2 80% distilled °c 234 90% distilled °c 251.8 End point °c 302.8

[0087] The different renewable source charges used are as follows: - Rapeseed oil, noted “Colza”, - Pre-treated animal fat, noted “GA”, - Animal fat methyl ester, noted “EMAG GA”, - UCO methyl ester, noted “EMAG UCO”.

[0088] The main characteristics of these charges are presented in Table 2.

[0089] [Tables2] Analysis Unit Method rapeseed GA EMAG GA EMAG UCO Viscosity at 70°C mm2 / s NF EN ISO 3104-August 1996 15.14 14.91 2.631 2.595 Viscosity at 40°C mm2 / s NF EN ISO 3104-August 1996 35.88 36.89 4.61 4.422 Total nitrogen ppm m ASTM D4629-17 0.59 33.6 93 0.83 Flash point Abel °C IP170-21 >75 >75 >75 >75 Pour point °C ISO 3016:2019 -24 18 15 -12 EM AG - ester %m NF14103-20 96.1 98.2 EM AG - ester saturated %m NF14103-20 43.7 6.9 Sulfur content mg / kg EN ISO 20846:2019 5.7 11.1 14.7 <3 Oleic acid FFA %m ISO 660:2020 0.03 11.33 0.2 0.11 Insoluble impurities %m ISO 663:2017 <0.01 0.01 <0.01 <0.01 Unsapo-nifiable matter %m ISO 3596:2000 1.08 0.89 0.35 0.95 Soaps mg / kg AOCS 17-95:2017 <2 <2 75 <2 PE type polymer mg / kg PE type polymer <50 <50 <50 <50 water %m ISO 8534:2017 0.6 0.5 0.6 1 total chlorine mg / kg ASTM D7536-20 1 10 1 1 As mg / kg ASTM D5185-09 <0.1 <0.1 <0.1 <0.1 P mg / kg ASTM D5185-09 0.1 1.2 <0.1 <0.1 Ni mg / kg ASTM D5185-09 0.2 0.2 0.3 0.1 V mg / kg ASTM D5185-09 <0.1 <0.1 <0.1 <0.1 Cu mg / kg ASTM D5185-09 <0.1 <0.1 0.1 <0.1 Fe mg / kg ASTM D5185-09 1.6 1.5 1.3 1.3 Mg mg / kg ASTM D5185-09 <0.1 0.1 <0.1 <0.1 Na mg / kg ASTM D5185-09 0.4 0.8 0.3 0.7 Pb mg / kg ASTM D5185-09 <0.1 <0.1 <0.1 <0.1 sum of metals ASTM D5185-09 2.3 3.8 2 2.1 chain lengths ISO 5508:1990 C14 %m 0 1 2.5 0.2 C16 %m 5.5 33.8 29 4.8 C18 %m 90.6 62.9 63.9 91.7 C20 %m 2 1 1 2 C22 %m 1 0 0 0.8

[0090] The catalyst used is a CoMo type catalyst. The operating conditions are presented in Table 3.

[0091] [Tables3] 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

[0092] Each charge of renewable origin is tested at two incorporation rates: 0.5%m and 0.3%m in kerosene.

[0093] The freezing point (denoted FP) was determined for the effluents obtained for each load, the results are presented in Table 4 below. Each of these effluents corresponds to the liquid fraction leaving the reactor, after separation of the gases.

[0094] In this table 4, AFP corresponds to the difference (noted) between the freezing point of hydrotreated kerosene alone and in mixture with a charge with the charge of renewable origin considered. AFP thus represents the degradation of the freezing point of the effluent produced for the different charges of renewable origin.

[0095] [Table 4] Freezing Point Measurements (ASTM Method D7153-15) Incorporation rate of renewable source charge (%m) FP (°C) AFP Kero - -51.8 0 Kero + Rapeseed 0.5 -43.4 8.4 0.3 -46.2 5.6 Kero + FAME GA 0.5 -45.6 6.2 0.3 -50.1 1.7 Kero + GA 0.5 -45.1 6.7 0.3 -49.3 2.5 Kero + FAME UCO 0.5 -43.3 8.5 0.3 -47.4 4.4

[0096] The different renewable feedstocks do not all have the same impact on the freezing point: the more the feedstock contains long carbon chains, the more it degrades the cold properties of the product.

[0097] GA EMAG, which contains 29% Cl6, is the most favorable filler since it only degrades the freezing point by 1.7°C at 0.3%m incorporation and by 6.2°C at 0.5%m.

[0098] It is noted that the cold properties of the product are very quickly degraded when fillers of renewable origin are incorporated. However, a compliant jet is obtained by incorporating 0.3%m of GA, GA EMAG and UCO EMAG. On the other hand, rapeseed, which has longer carbon chains, does not allow a compliant jet to be obtained even at 0.3%m of incorporation.

[0099] Table 5 brings together the other properties of the effluents obtained during co-processing with EMAGs, more precisely of the 140°C+ fraction of the effluent leaving the hydrotreatment reactor.

[0100] It is noted that the 140°C+ fractions of the effluents obtained meet most of the specifications of an AL jet.

[0101] [Tables5] Unit Method Spec. Jet Al ASTM D1655-21 Kero Kero +0.3% EMAG GA Kero +0.3% EMAG UCO FP °C ASTM D5972-16 -52.2 -48.7 -46.7 -47max Buckle mm ASTM D5001-10 0.68 0.67 0.61 0.85 max Flash point Abel °C IP170-21 51 51.5 52.5 38 min Sulfur content mg / kg NF EN ISO 20846- October 2019 4.9 <3 3.1 3000 max Copper corrosion 2 hours at 100°C ASTMD130-19 la la la 1 Smoke point mm ASTMD1322-19 24.6 24.7 24.7 18 min Viscosity at -20°C mm2 / s NF EN ISO 3104-August 1996 4.157 4.289 4.293 8 max Viscosity at -40°C mm2 / s NF EN ISO 3104-August 1996 8.815 8.31 8.773 12 max Calorific value PCI MJ / kg ASTM D3338-20 43.328 43.338 43.325 42.8 min Density at 15°C kg / m3 ASTM D4052-18 798.6 798.6 789.4 775-840 Initial point °C ASTM D2887-19 162.1 162.5 167.7 10% recovered at 176.8 178.6 179.2 50% recovered to 197 198.8 197.9 90% recovered to 236.8 238.5 238.4 End point 262.8 265 266.7 300 max Aromatic content by HPLC %vol ASTMD 6379-21 16.7 16.5 17.6 25 max EMAG content mg / kg IP585 / 10 (2015) <4.5 <4.5 <4.5 <10 mg / kg IP583 / 10 (2015) <10 <10 <10 <10

Claims

Claims

1. A method for manufacturing a jet fuel comprising at least the steps of: a) providing fatty acid methyl esters from the reaction of animal fats which are animal by-products with methanol in a transesterification reactor, step a) comprising: (i) obtaining methanol of renewable origin, (ii) followed by the reaction of the animal fats with the methanol obtained in step (i) in a transesterification reactor, and the provided fatty acid methyl esters comprising: - from 20%m to 64%m of fatty acid methyl esters whose carbon chain contains from 12 to 16 carbon atoms, - from 25%m to 65%m of fatty acid methyl esters whose carbon chain contains 18 carbon atoms, b) providing hydrocarbons of fossil origin,c) preparing a hydrocarbon feedstock containing the hydrocarbons of fossil origin provided by step b) and the fatty acid methyl esters provided by step a) in a content of at most 5% vol relative to the hydrocarbon feedstock, d) subjecting the hydrocarbon feedstock prepared during step c) to hydrotreatment and obtaining a treated hydrocarbon feedstock, e) fractionating the treated hydrocarbon feedstock obtained in step d) and recovering a kerosene fraction as jet fuel, said kerosene fraction having a final boiling point less than or equal to 300°C.,

2. Manufacturing process according to claim 1, wherein the fatty acid methyl esters provided in step a) comprise at least one of the following characteristics: - at most 4% m of fatty acid methyl esters whose carbon chain contains 20 carbon atoms, - at most 1% m of fatty acid methyl esters whose carbon chain contains 22 carbon atoms.

3. Manufacturing process according to any one of claims 1 or 2, in which the hydrocarbons of fossil origin provided in step b) are chosen from kerosene cuts.

4. Manufacturing process according to any one of claims 1 to 3, in which, during step (i), a step of converting a synthesis gas comprising CO / H2 into methanol of re- renewable, this synthesis gas being derived from biomass.

5. Manufacturing method according to claim 4, in which the conversion step is preceded by one of the following steps: - a biomass gasification step, - a biomass pyrolysis step, - a biogas production step containing methane and CO2, optionally by anaerobic digestion of biomass in the presence of one or more microorganisms, followed by partial oxidation of the biogas in the presence of oxygen.

6. Manufacturing process according to any one of claims 1 to 5, in which step d) is carried out under a pressure of 15 to 130 bars and at a temperature of 250 and 380°C, in the presence of a hydrotreatment catalyst and dihydrogen.

7. Manufacturing process according to any one of claims 1 to 6, in which the hydrotreatment catalyst comprises 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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