A method for producing intermediate distillates and naphtha from feedstock containing paraffinic and olefinic pyrolysis oil fractions.

Abstract

The present invention relates to a method for producing an intermediate fraction and naphtha from a mixed raw material containing a heavy fraction of fossil hydrocarbons, wherein at least 50% by weight of the heavy fraction is a pyrolysis oil fraction of plastics and / or tires and / or solid recovery fuel, the initial boiling point of the compounds exceeding 300°C and the final boiling point below 700°C, and less than 50% by weight is a pyrolysis oil fraction of plastics and / or tires and / or solid recovery fuels with a paraffinic and olefinic compound content exceeding 60% by weight, and the method comprises the following steps: a) a step of hydrogenating the mixed raw material to obtain a hydrogenated effluent; b) a step of hydrocracking the hydrogenated effluent to obtain a hydrocracking effluent; c) a step of separating the hydrocracking effluent to produce at least one gaseous effluent containing hydrogen and at least one liquid effluent; d) a fractional distillation step for producing a naphtha fraction and an intermediate distillate fraction.

Description

[Technical Field] 【0001】 The present invention relates to a method for producing intermediate distillates and naphtha, comprising a hydrogenation step and a hydrocracking step, characterized by the use of a mixed feedstock comprising a main heavy fraction of fossil hydrocarbons, in particular a heavy fraction of hydrocarbons having an initial boiling point of at least 50% by weight of the compound greater than 300°C and a final boiling point less than 700°C, such as a vacuum gas oil (VGO) fraction, and a small fraction of pyrolysis oil from highly paraffinic and olefinic plastics and / or tires and / or solid recovered fuel (SRF) containing a large amount of impurities. 【0002】 The objective of the method according to the present invention is essentially to produce an intermediate distillate fraction containing a kerosene fraction having initial and final boiling points in the range of about 150 to 250°C and a gas-oil fraction having initial and final boiling points in the range of about 250 to 370°C. The method according to the present invention also makes it possible to produce a naphtha fraction with a boiling point below about 150°C. [Background technology] 【0003】 Methods for producing intermediate distillates, which include the step of hydrocracking heavy petroleum fractions, are now essential in refining and enable the production of lighter fractions, such as gasoline (naphtha), kerosene, and gas oil, from surplus but not easily upgradeable heavy feedstocks, which refiners are seeking to adapt their production to demand. Compared to catalytic cracking (FCC), the advantage of catalytic hydrocracking is that it provides very high-quality intermediate distillates. Conversely, the resulting gasoline (naphtha) often has a low octane rating. 【0004】 In recent years, methods have emerged in the fuels and chemicals sectors to incorporate non-petroleum products, such as products from renewable sources, such as vegetable oils and animal fats, or waste products, such as used tires, plastics, or used oil, in addition to or as substitutes for fossil-derived products. 【0005】 In particular, plastics obtained from collection and sorting channels, and used tires, can undergo a pyrolysis process to obtain pyrolysis oil, among other things. These pyrolysis oils are generally incinerated to generate electricity and / or used as fuel in industrial or urban heating boilers. 【0006】 Pyrolytic oil can also be upgraded through refining methods to produce fuels, such as gasoline or gas oil, and / or chemical products for the production of various polymers in the chemical industry, such as olefins. 【0007】 However, this alternative route for upgrading pyrolysis oils faces problems arising from the specific composition of these oils, particularly the impurities they contain, and the composition of these oils is itself related to the diversity of waste components. 【0008】 Oils resulting from the pyrolysis of plastics, tires, or solid fuel materials (SRF) generally contain many diolefins and impurities, particularly metals, silicon, or halogenated compounds, especially chlorinated compounds, heteroatoms such as sulfur, oxygen, and nitrogen, and insoluble matter, often in high concentrations, which may make them incompatible with a given refining unit, such as a fixed-bed hydrogenation unit. 【0009】 The handling of these oils can present operational problems, particularly issues of corrosion, coking, or catalyst deactivation, or incompatibility with polymer applications. For example, the presence of diolefins very often leads to instability problems in pyrolysis oils, characterized by the formation of gummy deposits. The gummy deposits and insoluble matter that may be present in pyrolysis oils can cause clogging problems in equipment. The presence of chlorine can lead to corrosion problems. 【0010】 One method for removing these impurities contained in pyrolysis oil is to perform hydrogenation in the presence of a catalyst. Such methods are described, for example, in Patent Documents 1 and 2. 【0011】 Patent applications, Patent Documents 3-5, describe a method for treating plastic pyrolysis oil, which in particular includes a step of selective hydrogenation of the pyrolysis oil and a step of fixed-bed hydrogenation of the hydrogenated effluent. The specific separation of the hydrogenated effluent with water, followed by a naphtha fraction resulting from the fraction of the separated hydrocarbon flow, can be sent to a steam cracker or used as a fuel base. According to Patent Documents 4 and 5, these methods incorporate one or two fixed-bed hydrocracking steps after the hydrogenation step to minimize the yield of the heavy fraction and maximize the yield of the naphtha fraction (a fraction generally favorable to steam cracking units) by converting the heavy fraction to a naphtha fraction at least partially by hydrocracking. 【0012】 Other methods involving mixtures of fossil feedstock and pyrolysis oil are also known, for example, Patent Document 6, which describes a method for increasing the production of light compounds of the ethane and propane type by co-treating pyrolysis oil with low aromatic compound content and unspecified hydrocracking feedstock in a hydrocracking process, but the pre-hydrotreatment process is not disclosed. 【0013】 Patent Document 7 describes a method for producing hydrocarbons from a feedstock containing a main fraction of hydrocarbons of the type of vacuum distillate or heavy gas oil of fossil origin and a small fraction of pyrolysis oil, the method including a hydrotreating step and a hydrocracking step. The pyrolysis oil contains 40% to 60% by weight of olefins and less than 20% by weight of aromatic compounds. This document does not describe the use of pyrolysis oil containing a large amount of paraffin as a co-feedstock in the production of middle distillates and naphtha by hydrocracking a vacuum fraction feedstock and its beneficial effects. 【Prior Art Documents】 【Patent Documents】 【0014】 【Patent Document 1】 International Publication No. 2016 / 142808 【Patent Document 2】 International Publication No. 2016 / 142806 【Patent Document 3】 Specification of French Patent Application Publication No. 3107530 【Patent Document 4】 Specification of French Patent Application Publication No. 3113060 【Patent Document 5】 Specification of French Patent Application Publication No. 3113061 【Patent Document 6】 International Publication No. 2015 / 128033 【Patent Document 7】 International Publication No. 2023 / 002092 【Summary of the Invention】 【Means for Solving the Problems】 【0015】 (Objectives and Summary of the Invention) The present invention relates to the field of upgrading heavy feedstocks that are generally difficult to upgrade and contain impurities, such as metals, sulfur, and nitrogen, typically at high levels, for example vacuum distillates, and converting them into lighter products that can be upgraded as fuels, such as gasoline (naphtha), kerosene, and / or diesel. 【0016】 The inventors have surprisingly found that incorporating a small fraction of the pyrolysis oil of plastics and / or tires and / or solid recovered fuels, which have high contents of paraffinic and olefinic compounds and contain large amounts of impurities, into heavy hydrocarbon feedstocks of fossil origin, typically vacuum distillates, which are conventionally treated by hydrocracking methods, can improve the production of fuel bases and / or other hydrocarbons that can be upgraded not only from the perspective of yield but also from the perspective of quality. 【0017】 Indeed, the method according to the present invention makes it possible, on the one hand, to upgrade pyrolysis oils that generally contain large amounts of impurities and are difficult to upgrade, thereby reducing dependence on fossil fuels and creating a circular economy. 【0018】 The method according to the present invention makes it possible to produce middle distillates (especially the kerosene fraction and the gas oil fraction) that meet the specifications required for these fractions, despite the use of pyrolysis oils containing many impurities. Furthermore, it is known that the high content of aromatic compounds in middle distillates can be a problem in order to meet the maximum aromatic compound content allowed according to the specifications. The addition of a small fraction of highly paraffinic and olefinic pyrolysis oil can therefore make it possible to reduce the aromatic compound content and the density in the final product. 【0019】 The method according to the present invention makes it possible to produce a gas oil fraction that meets the specifications for density, sulfur content, cetane number, and cloud point, particularly by controlling the degree of conversion (i.e., 50% to 95% by weight) during the hydrocracking process. In particular, it is possible to improve the cetane number compared to a gas oil fraction obtained from 100% fossil fuels by adding small fractions of highly paraffinic and olefinic pyrolysis oils. The method according to the present invention therefore utilizes the chemical properties of pyrolysis oils used as feedstock, particularly pyrolysis oils having high concentrations of paraffinic and olefinic compounds. 【0020】 The method according to the present invention also makes it possible to produce a kerosene fraction that satisfies the specifications of density, sulfur content, freezing point, and flue point. 【0021】 Another advantage of the present invention is that an increase in the yield of the intermediate distillate (kerosene and gas oil) fraction is observed, in particular, when the degree of conversion in the hydrocracking process is controlled relative to the yield of the pure fossil hydrocarbon feedstock (i.e., less than 85% by weight). In fact, since pyrolysis oils generally contain compounds with boiling points in the intermediate distillate range, it is essentially possible to increase the intermediate distillate yield by adding such feedstock to heavier fossil hydrocarbon feedstock, provided that the degree of conversion is controlled (to avoid over-decomposition). 【0022】 The method according to the present invention therefore makes it possible to upgrade pyrolysis oil by utilizing its chemical properties (high paraffin and olefin content) to produce a fuel base with improved characteristics that meets specifications and increases yield. 【0023】 More specifically, the present invention relates to a method for producing intermediate distillates and naphtha from a feedstock comprising a heavy fraction of fossil hydrocarbons and a fraction of pyrolysis oil from plastics and / or tires and / or solid recovery fuels, wherein the initial boiling point of at least 50% by weight of the compounds in the heavy fraction is greater than 300°C and the final boiling point is less than 700°C, the pyrolysis oil fraction contains paraffinic and olefinic compounds in a proportion of more than 60% by weight relative to the weight of the pyrolysis oil, the pyrolysis oil fraction constitutes less than 50% by weight of the feedstock, and the method comprises the following steps: a) Hydrogenation process; carried out in a hydrogenation reaction section; using at least one fixed-bed reactor having n catalyst beds; n is an integer of 1 or more, each containing at least one hydrogenation catalyst; the hydrogenation reaction section is supplied with at least the feed material and a gas stream containing hydrogen; the temperature when the hydrogenation reaction section is used is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 6.0 h -1 The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L; hydrogenated effluent is obtained; b) Hydrocracking step; carried out in a hydrocracking reaction section; using at least one fixed-bed reactor having n catalyst beds; n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst; the hydrocracking reaction section is fed at least a portion of the hydrogenated effluent from step a) and a gas stream containing hydrogen; the temperature during operation of the hydrocracking reaction section is 200-450°C, the pressure is 2.0-18.0 MPa abs., and the spatiotemporal velocity is 0.1-12.0 h -1 The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L; the hydrocracking effluent is obtained; c) Separation process; at least a portion of the hydrocracking effluent from process b) is fed to the separation section; producing at least one gaseous effluent containing hydrogen and at least one liquid effluent; d) Fractionation process; at least a portion of the liquid effluent from process c) is fed to the fractionation section; producing at least one naphtha fraction, at least one intermediate distillate fraction, and at least one unconverted heavy liquid fraction. 【0024】 According to the modification, the pyrolysis oil fraction constitutes 1% to 45% by weight of the feed material, preferably 2% to 30% by weight, preferably 2% to 25% by weight, and more preferably 3% to 20% by weight of the feed material. 【0025】 According to the modification, the feedstock consists of the pyrolysis oil fraction and the heavy hydrocarbon fraction of fossil origin, wherein the pyrolysis oil fraction constitutes 1% to 45% by weight, preferably 2% to 30% by weight, of the feedstock, and the heavy hydrocarbon fraction constitutes 55% to 99% by weight, preferably 70% to 98% by weight, of the feedstock. 【0026】 According to the modification, the content of aromatic compounds in the pyrolysis oil fraction is less than 30% by weight, preferably less than 25% by weight. 【0027】 According to the modification, the heavy fraction of fossil hydrocarbons is selected from the following: obtained from the direct distillation of crude oil, or from vacuum distillates obtained from hydrotreatment, hydroconversion or hydrocracking methods applied to residues at atmospheric or reduced pressure and operated in fixed bed, moving bed, boiling bed or slurry bed; or fractions obtained from conversion units such as fluid catalytic cracking; or fractions resulting from coking methods; or fractions resulting from screw breaking methods; or fractions obtained from units for extracting aromatic compounds from lubricating oil bases; or fractions resulting from solvent dewaxing of lubricating oil bases; or dewaxed oils resulting from solvent dewaxing of residues; or any mixture of the above feedstocks. 【0028】 According to the deformation, the heavy fraction of fossil-derived hydrocarbons is a vacuum distillate. 【0029】 According to the modification, the pyrolysis oil is selected from pyrolysis oils derived from polyethylene and / or polypropylene. 【0030】 According to the deformation, the pyrolysis oil contains bio-based carbon at a content of 20% to 70% by weight, as defined by ASTM D6866. 【0031】 According to the modification, the feedstock containing the heavy fraction and the pyrolysis oil fraction of fossil hydrocarbons, or only the pyrolysis oil, or only the heavy feedstock of fossil hydrocarbons, is subjected to a pretreatment step, the pretreatment step being performed upstream of step a), and including an adsorption step and / or a filtration step and / or a centrifugation step and / or a sedimentation step and / or an electrostatic separation step and / or a washing step using an aqueous solution and / or a gas stripping step. 【0032】 According to the modification, the filter plate is integrated upstream of the first catalyst bed at the inlet of step a). 【0033】 According to the modification, the method includes a separation step in the separation section between the hydrogenation step a) and the hydrocracking step b), separating part or all of the hydrogenated effluent to produce at least two fractions, mainly consisting of a heavy fraction that boils at temperatures of 370°C or higher. 【0034】 According to the modification, the separation section of step c) and / or the separation section between the hydrogenation step a) and the hydrocracking step b) include means for washing the separated fraction by contact with an aqueous solution. 【0035】 According to the deformation, the degree of conversion in the hydrocracking process b) is 50% to 95% by weight. 【0036】 According to the modified version, the method also includes a second hydrocracking step carried out in a hydrocracking reaction section, using at least one fixed-bed reactor having n catalyst beds, where n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst, the hydrocracking reaction section being fed at least a portion of the unconverted heavy fraction and / or intermediate distillate fraction produced from fractionation step d) and a gas stream containing hydrogen, the temperature during operation of the hydrocracking reaction section being 200-450°C, the pressure being 2.0-18.0 MPa abs., and the spatiotemporal velocity being 0.1-12.0 h -1 The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, and a second hydrocracking effluent is obtained. 【0037】 In a modified form, the present invention also relates to the products obtained by this method. 【0038】 According to the modification, the product contains bio-based carbon at a concentration of 0.1% to 15% by weight, as defined by ASTM D6866. 【0039】 For the purposes of the present invention, the various embodiments presented may be used individually or in combination with each other, and there are no restrictions on the combinations. 【0040】 For the purposes of the present invention, various ranges of parameters for a given process, such as pressure ranges and temperature ranges, may be used individually or in combination. For example, for the purposes of the present invention, a preferred range of pressure values ​​may be combined with a preferred range of temperature values. 【0041】 According to the present invention, pressure is absolute pressure, also denoted as abs., and unless otherwise specified, it is given in absolute pressure MPa (or MPa abs.). 【0042】 For the remainder of this text, the groups of chemical elements are given according to the CAS classification (CRC Handbook of Chemistry and Physics, published by CRC Press, editor-in-chief DRLide, 81st edition, 2000–2001). For example, Group VIII (or Group VIIIB) according to the CAS classification corresponds to the metals from columns 8, 9, and 10 of the new IUPAC classification, and Group VIB corresponds to the metals from column 6. 【0043】 The metal content is measured by X-ray fluorescence. 【0044】 In the remainder of this text, unless otherwise specified, the term "pyrolysis oil" is understood to mean the oil resulting from the pyrolysis of plastics and / or tires and / or SRF. Also, for simplicity, unless otherwise specified, the term "heavy hydrocarbon fraction" in the feedstock refers to fossil-based heavy hydrocarbon fractions. 【0045】 In the remainder of this text, the expressions "of between ... and ..." and "between ... and ..." are equivalent, meaning that the limit of the span falls within the range of values ​​stated. If not, and if the limit does not fall within the range stated, such details are provided by this invention. 【0046】 In this specification, the term "to comprise" is synonymous with "to include" and "to contain" (meaning the same thing), and is inclusive or non-exclusive, and does not exclude other elements that may not be described. The term "to comprise" is understood to include the exclusive and closed term "to consist of". [Modes for carrying out the invention] 【0047】 (List of drawings) Figure 1 schematically shows an embodiment of the hydrogenation conversion method according to the present invention. 【0048】 (Detailed explanation) (fossil feedstock) The feedstock processed in the method according to the present invention includes a heavy fraction of fossil hydrocarbons. 【0049】 The heavy fraction of fossil hydrocarbons is a fraction in which at least 50% by weight of the compound has an initial boiling point greater than 300°C, preferably greater than 320°C, and a final boiling point less than 700°C, preferably less than 550°C. 【0050】 The aforementioned fractions of fossil-derived heavy hydrocarbons are advantageously obtained from direct distillation of crude oil (straight-run vacuum gas oil type feedstock) or by other methods, particularly VGO (vacuum gas oil) obtained from hydrogenation, hydroconversion, or hydrocracking methods applied to atmospheric or vacuum residues operated in fixed bed, moving bed, boiling bed, or slurry bed; or fractions from conversion units such as fluid catalytic cracking (FCC), e.g., light fractions (LCO or light cycle oil), heavy fractions (HCO or heavy cycle oil), FCC residues. ;or fractions resulting from coking methods, in particular light gas oil fractions (CGO or coker gas oil), heavy gas oil fractions (HCGO or heavy coker gas oil); or fractions resulting from screw breaking methods; or fractions from units for extracting aromatic compounds from lubricating oil bases (supply materials of the aromatic extract oil type); or fractions from solvent dewaxing of lubricating oil bases; or dewaxed oil (DAO) originating from solvent dewaxing of residues (from direct distillation or inversion methods); or any mixture of the above supply materials may be selected. 【0051】 The heavy fraction of fossil hydrocarbons does not contain very heavy hydrocarbon fractions, such as vacuum residues (i.e., those containing at least 50% by weight, or even more than 80% by weight, of which have a boiling point of at least 450°C, preferably at least 500°C, and more preferably at least 540°C). 【0052】 Preferably, the heavy fraction is a vacuum distillate. More preferably, the heavy fraction is a mixture of a vacuum distillate obtained from the distillation of crude oil and a vacuum distillate obtained from a residue conversion method. 【0053】 The nitrogen content of the heavy fraction of fossil origin treated in the method according to the present invention is usually 500 ppm by weight or more, preferably 500 to 10,000 ppm by weight, more preferably 700 to 4,000 ppm by weight, and even more preferably 1,000 to 4,000 ppm by weight. The sulfur content of the heavy fraction of fossil origin is usually 0.01% to 5% by weight, preferably 0.2% to 4% by weight, and even more preferably 0.5% to 3% by weight. 【0054】 The heavy fraction of fossil origin may sometimes contain metals. The total content of nickel and vanadium in the heavy fraction of fossil origin is preferably less than 20 ppm by weight, and preferably less than 10 ppm by weight. 【0055】 The heavy fraction of fossil origin may sometimes contain asphaltene. The asphaltene content of the heavy fraction of fossil origin is generally less than 4000 ppm by weight, preferably less than 1000 ppm by weight, and more preferably less than 200 ppm by weight. 【0056】 The content of metals, sulfur, nitrogen, and asphaltenes is expressed as a weight percentage of the total weight of the heavy fraction of hydrocarbons in the feedstock. 【0057】 (pyrolysis oil feedstock) The feedstock processed in the method according to the present invention also includes a small fraction of pyrolysis oil from plastics and / or tires and / or solid recovery fuels, which contains paraffinic and olefinic compounds at a content of more than 60% by weight relative to the weight of the pyrolysis oil. 【0058】 Pyrolytic oil can be pyrolytic oil derived from plastics, tires, and / or solid recovery fuels. 【0059】 Plastic waste is generally a mixture of several polymers, and can include polyethylene (low-density and / or high-density), polypropylene, polyethylene terephthalate, polyvinyl chloride, and polystyrene, either alone or in mixtures. Furthermore, depending on the application, plastics may contain other compounds in addition to polymers, such as plasticizers, pigments, dyes, or residues of polymerization catalysts. Plastic waste may also contain small amounts of biomass, such as biomass derived from household waste. 【0060】 Regarding tires, they primarily consist of rubber (a mixture of cross-linked synthetic rubber and natural rubber-type elastomers with additives such as silica, resin, sulfur, zinc oxide, and carbon black) for their elastic properties, and textiles and metal fibers for their reinforcing properties. 【0061】 Solid recovered fuel (SRF), also known as refuse-derived fuel (RDF), is a solid, non-hazardous waste prepared with the aim of improving energy quality, regardless of whether it originates from household waste and similar waste, waste from economic activities, or waste from construction and / or demolition. SRF is generally a mixture of all combustible waste, such as used tires, food by-products (fat, animal feed, etc.), viscose and wood waste, light fragments resulting from shredders (e.g., used cars, electrical and electronic waste (WEEE)), household and commercial waste, and residues from the recycling of various types of waste (including, among others, designated municipal waste, plastic waste, textile waste, or wood waste). SRF commonly contains plastic waste. 【0062】 Pyrolytic oils can be produced from thermal or catalytic pyrolysis treatments, or prepared by hydrothermal decomposition (pyrolysis in the presence of a catalyst and hydrogen). They can also be the result of hydrothermal conversion. Pyrolytic oils are advantageously in liquid form at ambient temperature. 【0063】 The pyrolysis oil is a fraction of the compound in which at least 50% by weight has an initial boiling point greater than 100°C, preferably greater than 150°C, and a final boiling point less than 1000°C, preferably less than 650°C. 【0064】 The pyrolysis oil contains, in particular, paraffinic and olefinic compounds in a content of more than 60% by weight, preferably more than 70% by weight, and especially preferably more than 80% by weight, relative to the weight of the pyrolysis oil. The term “paraffinic compounds” is understood to mean any paraffinic compounds, including n- and iso-paraffinic compounds. The term “olefinic compounds” is understood to mean any olefinic compounds, including mono- and / or diolefins. The content of paraffinic and olefinic compounds in the pyrolysis oil is generally 60% to 90% by weight, preferably 65% ​​to 85% by weight, relative to the weight of the pyrolysis oil. Preferably, the olefin content is less than 40% by weight, relative to the weight of the pyrolysis oil. Other compounds, such as naphthenes or aromatic compounds, are also generally present in the pyrolysis oil. In particular, depending on the origin of the pyrolysis oil, it may contain up to 25% by weight, preferably 1% to 25% by weight, of naphthalene and up to 30% by weight, preferably 1% to 25% by weight, of aromatic compounds relative to the weight of the pyrolysis oil, and the sum of paraffin, naphthene, olefin and aromatic compounds is equal to 100% by weight of hydrocarbon compounds, and it is understood that the pyrolysis oil contains paraffinic and olefinic compounds in a content of more than 60% by weight. According to a variation, the pyrolysis oil preferably contains naphthene in a content of less than 20% by weight, preferably 1% to 20% by weight, relative to the weight of the pyrolysis oil. According to a variation, the pyrolysis oil preferably contains aromatic compounds in a content of less than 30% by weight, preferably less than 25% by weight, and preferably less than 20% by weight, relative to the weight of the pyrolysis oil. 【0065】 The pyrolysis oil may contain, in at least a portion, a bio-based compound, such as tire pyrolysis oil derived from natural rubber elastomers. Depending on the origin of the pyrolysis oil, this may contain bio-based carbon at a concentration of 20% to 70% by weight, preferably 30% to 60% by weight, relative to the total weight of the pyrolysis oil (according to ASTM D6866). 14 (By isotopic radiocarbon analysis). This makes it possible to incorporate bio-based compositions into the hydrocracking products. The production of biokerosene, also known as SAF ("Sustainable Aviation Fuel"), is particularly needed to decarbonize both the civilian and military aviation sectors. 【0066】 Pyrolytic oils particularly suitable for the method according to the present invention are pyrolytic oils derived from plastics with a high paraffinic and olefinic content, such as oils derived from polyethylene and / or polypropylene, either alone or in mixtures with other plastics. Preferably, the pyrolytic oil fraction used in the method according to the present invention is a pyrolytic oil derived from plastic, in particular polyethylene and / or polypropylene. 【0067】 Pyrolytic oils may contain diolefins. The diolefin content is generally determined indirectly as the maleic anhydride value (MAV). This method is based on the Diels-Alder addition reaction between conjugated diolefins and maleic anhydride. A method for determining MAV is described by C. Loepez-Garcia et al. in Near Infrared Monitoring of Low Conjugated Diolefins Content in Hydrotreated FCC Gasoline Streams, Oil & Gas Science and Technology - Rev. IFP, Vol. 62 (2007), No. 1, pp. 57-68. MAV is expressed as mg (mg / g) of maleic anhydride reacted with 1 g of sample. MAV preferably ranges from 5 to 100 mg / g in the pyrolytic oil. 【0068】 The density of pyrolysis oil is measured at 15°C according to the ASTM D4052 method and is generally 0.70 g / cm³. 3 ~1.05 g / cm³ 3 Preferably 0.75 g / cm³ 3 ~0.98g / cm 3 That is the case. 【0069】 Pyrolysis oil may, and usually does, further contain impurities, such as metals, particularly iron, silicon, or halogenated compounds, particularly chlorinated compounds. These impurities may be present in high concentrations, for example, up to 500 ppm by weight, or up to 700 ppm by weight, or even up to 1,000 ppm by weight, and halogenated elements (particularly chlorine, but also including bromine, fluorine, and iodine) contributed by halogenated compounds up to 5,000 ppm by weight, generally containing 1 to 1,000 ppm by weight, or 1 to 700 ppm by weight, or 1 to 500 ppm by weight. Pyrolysis oil may also contain chlorine elements contributed by chlorinated compounds up to 500 ppm by weight, or up to 700 ppm by weight, or even up to 1,000 ppm by weight, or even up to 5,000 ppm by weight, generally containing 1 to 1,000 ppm by weight, or 1 to 700 ppm by weight, or 1 to 500 ppm by weight. 【0070】 Pyrolysis oil may contain up to 200 ppm by weight, and even up to 1500 ppm by weight, of metallic or metalloid elements, generally between 1 and 1500 ppm by weight or 1 and 200 ppm by weight. Alkali metals, alkaline earth metals, transition metals, post-transition metals, and metalloids can be placed in the same category as metallic contaminants called metallic or metalloid elements. In particular, metallic or metalloid elements include silicon, iron, or both of these elements. Pyrolysis oil may contain, among other things, up to 200 ppm by weight or up to 1000 ppm by weight of silicon, generally between 1 and 1000 ppm by weight or 1 and 500 ppm by weight or 1 and 200 ppm by weight of silicon. Pyrolysis oil may contain, among other things, up to 50 ppm by weight or up to 100 ppm by weight of iron, generally between 1 and 100 ppm by weight or 1 and 50 ppm by weight of iron. Pyrolytic oils may also contain phosphorus, sodium, calcium, potassium, and magnesium. 【0071】 The pyrolysis oil may also contain heteroatoms, particularly those contributed by other impurities such as sulfur compounds, oxygen compounds, and / or nitrogen compounds, generally in amounts of less than 40,000 ppm by weight, preferably less than 15,500 ppm by weight, and generally between 1 and 40,000 ppm by weight or 1 and 15,500 ppm by weight. 【0072】 Sulfur compounds are generally present in concentrations of less than 15,000 ppm by weight, preferably less than 10,000 ppm by weight, and generally between 1 and 15,000 ppm by weight or between 1 and 10,000 ppm by weight. 【0073】 Oxygen compounds are generally present in concentrations of less than 15,000 ppm by weight, preferably less than 10,000 ppm by weight, and generally between 1 and 15,000 ppm by weight or between 1 and 10,000 ppm by weight. 【0074】 Nitrogen compounds are generally present in concentrations of less than 10,000 ppm by weight, preferably less than 8,000 ppm by weight, and generally between 1 and 10,000 ppm by weight or between 1 and 8,000 ppm by weight. 【0075】 The content of sulfur compounds, oxygen compounds, and / or nitrogen compounds often depends on the origin of the oil. Therefore, tire pyrolysis oils generally contain more heteroatoms, particularly sulfur compounds, than plastic pyrolysis oils. 【0076】 The pyrolysis oil may also contain other impurities, such as heavy metals, such as mercury, arsenic, zinc, and lead, in amounts of up to 500 ppb by weight, generally 1 to 300 ppb by weight, or 1 to 200 ppb by weight, such as mercury or arsenic. 【0077】 According to an essential aspect of the present invention, the feedstock comprises a heavy fraction of fossil-derived hydrocarbons and a small fraction of pyrolysis oil of plastics and / or tires and / or SRF, wherein the content of paraffinic and olefinic compounds is greater than 60% by weight relative to the weight of the pyrolysis oil. 【0078】 The fraction of pyrolysis oil for plastics and / or tires and / or SRF shall constitute less than 50% by weight of the feedstock (total weight of the feedstock), preferably 1% to 45% by weight of the feedstock, more preferably 2% to 30% by weight of the feedstock, even more preferably 2% to 25% by weight of the feedstock, and even more preferably 3% to 20% by weight of the feedstock. 【0079】 The heavy hydrocarbon fraction can constitute more than 50% by weight of the feedstock (total weight of the feedstock), preferably 55% to 99% by weight of the feedstock, preferably 70% to 98% by weight of the feedstock, more preferably 75% to 98% by weight of the feedstock, even more preferably 80% to 97% by weight of the feedstock, even more preferably 80% to 95% by weight of the feedstock, or even more preferably 85% to 95% by weight of the feedstock. 【0080】 According to a preferred embodiment, the feedstock consists of the small fraction of pyrolysis oil and a heavy fraction of fossil-derived hydrocarbons. 【0081】 According to this embodiment, the pyrolysis oil fraction constitutes 1% to 45% by weight, preferably 2% to 30% by weight, of the feedstock, and the heavy hydrocarbon fraction constitutes 55% to 99% by weight, preferably 70% to 98% by weight, of the feedstock. 【0082】 According to one or more embodiments, the feedstock of the method according to the present invention may contain, in a low percentage, typically 1% to 20% by weight, or even 1% to 10% by weight, or 1% to 5% by weight of the feedstock, plant and / or animal fat fractions, and / or hydrocarbon fractions resulting from methods for the thermal and / or catalytic conversion of lignocellulosic biomass, for example, oils resulting from lignocellulosic biomass by various liquefaction methods, e.g., hydrothermal liquefaction or pyrolysis, which are then co-treated with pyrolysis oils of plastics and / or tires and / or SRF, and heavy fractions of fossil-derived hydrocarbons. 【0083】 Fats and oils of plant and / or animal origin contain triglycerides and / or free fatty acids and / or esters. Vegetable oils may be advantageously crude or fully or partially refined and may be derived from the following plants: rapeseed, sunflower, soybean, palm, palm kernel, olive, coconut, jatropha (physic nut), castor oil plant, cotton, peanut, flax, or rugosa, but this list is not limiting. Algal oils or fish oils are also relevant. Fats and oils of plant and / or animal origin may be used fats, e.g., used cooking oils. Animal fats may consist of porcine fat or residues from the food industry or be selected from fats resulting from the catering industry. 【0084】 Oils and fats of plant and / or animal origin are generally very paraffin-rich. These paraffins have low density and a good cetane number. By adding such feedstocks to the feedstocks of the method (fossil fractions and / or very (and excessively) aromatic pyrolysis oil fractions), it is possible to achieve the density specifications for the desired product of the method. Similarly, by adding such feedstocks, it is possible to improve the cetane number of gas oil fractions. 【0085】 The term "lignocellulosic biomass" refers to compounds derived from plants or their by-products, and includes components selected from the group formed by cellulose, hemicellulose (carbohydrate polymers), and / or lignin (aromatic polymers). 【0086】 According to one or more embodiments, the feedstock for the method according to the present invention does not include plant and / or animal fat fractions, or hydrocarbon fractions resulting from methods for the thermal and / or catalytic conversion of lignocellulosic biomass, such as biomass pyrolysis oils. 【0087】 (Preprocessing (optional)) The feedstock, which comprises the heavy fraction and the pyrolysis oil fraction of fossil hydrocarbons, or pyrolysis oil alone, or heavy feedstock of fossil hydrocarbons alone, may be advantageously pretreated in an optional pretreatment step prior to the hydrogenation step a), to obtain pretreated mixed feedstock, pretreated pyrolysis oil, or pretreated fossil feedstock, which is then supplied to step a). 【0088】 According to the modification, this optional pretreatment step makes it possible to reduce the amount of contaminants and solid particles. In particular, this optional pretreatment step makes it possible to remove sediment that may be formed as a result of the unstable nature of the pyrolysis oil and / or compatibility issues between two different feedstocks. 【0089】 The optional pretreatment steps can be carried out by any method known to those skilled in the art that allows for a reduction in the amount of contaminants. This may include, among other things, adsorption steps and / or filtration steps and / or centrifugation steps and / or sedimentation steps and / or electrostatic separation steps and / or washing with aqueous solutions and / or gas stripping steps. 【0090】 The temperature at which the optional pretreatment step is advantageous is 20°C to 400°C, preferably 40°C to 350°C, and the pressure at that time is 0.15 to 10.0 MPa abs., preferably 0.2 to 7.0 MPa abs. 【0091】 According to the modification, the optional pretreatment step is carried out in an adsorption section operated in the presence of at least one adsorbent. The adsorbent can be selected from zeolite, activated carbon, clay, silica, or alumina. Advantageously, the adsorbent contains less than 1% by weight of metallic elements, and preferably does not contain metallic elements. The expression “metallic elements in the adsorbent” should be understood to mean elements of Group VIB, Group VIIB, and Group VIII. In cases where the heavy fraction of fossil origin contains metal and / or resin and / or asphaltene type compounds, it is advantageous to pre-pass the feedstock containing the heavy fraction of fossil origin through a bed of catalyst or adsorbent other than a catalyst for hydrotreatment or hydrocracking, for example, a bed of a hydrodemetallation catalyst. Adsorption may be carried out with the pyrolysis oil feedstock alone or with a mixed feedstock. 【0092】 According to another variation, the optional pretreatment step is carried out in a section for washing with an aqueous solution, such as water, or an acidic or basic solution. This washing section may include equipment that allows the mixed feedstock or pyrolysis oil or fossil feedstock to come into contact with an aqueous solution to separate the phases, thereby obtaining, on the one hand, the mixed feedstock or pyrolysis oil or pretreated feedstock, and on the other hand, an aqueous solution containing impurities. These devices may include, for example, a stirred reactor, a decanter, a mixer decanter, and / or a parallel or countercurrent washing column. 【0093】 In another variation, the optional pretreatment step is carried out by filtration. The filtration step makes it possible to remove inorganic solids, sediments and / or particulate matter, in particular metals, metal oxides and metal chlorides, contained in the mixed feedstock or pyrolysis oil or fossil feedstock. Filters are commonly used, with pore sizes (e.g., diameter or equivalent diameter) of less than 50 μm, preferably 30 μm or less. Filters with pore sizes of 5 μm or less may also be used. A series of filters with different pore sizes may be used, in particular a series of filters with pore sizes decreasing in the direction of feedstock flow. These filtration media are well known for industrial applications. For example, cartridge filters or self-cleaning filters are suitable. 【0094】 According to another variation, the optional pretreatment step may also be carried out by centrifugal separation, sedimentation, or electrostatic separation. 【0095】 According to another variation, the optional pretreatment step is carried out by gas stripping, thereby reducing the oxygen content in the feedstock. Gas extraction can remove oxygen (O2) that may be dissolved in the mixed feedstock or pyrolysis oil or fossil feedstock, thereby reducing the probability of free radical formation that leads to polymerization in downstream processes. This method generally involves contacting the feedstock with an extraction gas (e.g., H2, N2, or a mixture thereof) to transfer at least some of the dissolved oxygen in the feedstock to the extraction gas, and then separating the extraction gas from the mixed feedstock or pyrolysis oil or fossil feedstock. Given that the hydrogenation step is generally carried out downstream, any dissolved H2 remaining in the mixed feedstock or pyrolysis oil or fossil feedstock after the gas extraction step is not a problem. 【0096】 The aforementioned optional preprocessing steps generally include one or more, preferably several, of the above-mentioned processes. 【0097】 Therefore, the optional pretreatment step makes it possible to obtain a pretreated feed material containing the pyrolysis oil fraction or pretreated pyrolysis oil, or a pretreated fossil feed material, which can then be supplied to the hydrogenation step a). 【0098】 The two fractions of the feedstock may be preheated individually or together beforehand by any heating device known to those skilled in the art to ensure that they are in a liquid state before entering the hydrogenation reactor. Alternatively, if the pyrolysis oil fraction is liquid and can be pumped at ambient temperature, it may be possible to preheat only the heavy hydrocarbon fraction. The temperature at which preheating is generally performed is 50 to 150°C, preferably 60 to 100°C. 【0099】 After an optional step of preheating at least one of the two fractions, heating may be carried out by any means known to those skilled in the art before entering the hydrogenation reactor. Heating may be carried out on the fossil fraction alone, or the pyrolysis oil fraction alone, or a mixture of the two fractions. According to a modification, the pyrolysis oil fraction may be indirectly heated by mixing it with a preheated heavy hydrocarbon fraction (i.e., heat exchange between the two fractions by bringing the two fractions having different temperatures into contact), limiting the formation of gums and / or coking of the heating equipment. 【0100】 According to one possibility, the pyrolysis oil fraction may be pre-mixed with a preheated heavy hydrocarbon fraction of the feedstock before entering the hydrogenation reactor. Another possibility is the separate injection of the pyrolysis oil fraction and the heavy hydrocarbon fraction into the hydrogenation reactor. This injection mode may also be preferred to avoid any problems associated with chemical incompatibility between the two fractions (e.g., the risk of phase separation or the risk of asphaltene precipitation) or to prevent fouling acceleration that may occur in the heating oven (if the pyrolysis oil has a high diolefin and olefin content, a gummy substance may form). 【0101】 Before it is introduced into the hydrotreating reaction section, the feedstock undergoes a pressurization step to suit the pressure at which it is operated in the hydrotreating process. This pressurization step is preferably carried out before the heating step. 【0102】 (Hydrotreating process a)) According to the present invention, the method includes a hydrotreating process a) carried out in a hydrotreating reaction section, using at least one fixed-bed reactor having n catalyst beds, where n is an integer of 1 or more, each containing at least one kind of hydrotreating catalyst. The hydrotreating reaction section is fed at least the feedstock and a gas stream containing hydrogen. When the hydrotreating reaction section is in use, the temperature is 200 - 450 °C, the pressure is 2.0 - 18.0 MPa abs., and the space velocity is 0.1 - 6.0 h -1 and the amount of hydrogen introduced therein is such that the volume ratio of hydrogen volume (liter) / hydrocarbon volume (liter) is 100 - 3000 nL / L, obtaining a hydrotreated effluent. 【0103】 Advantageously, process a) performs a hydrotreating reaction well-known to those skilled in the art. More specifically, it performs hydrotreating reactions such as hydrogenation of aromatic compounds, hydrodesulfurization and hydrodenitrogenation, hydrogenation of olefins and halogen compounds, and hydrodemetallization. 【0104】 Preferably, when the hydrotreating process according to the present invention is carried out, the temperature is 200 °C - 450 °C, preferably 250 °C - 450 °C, most preferably 300 °C - 430 °C, the pressure is 2.0 - 18.0 MPa abs., preferably 3 - 16 MPa abs., and the space velocity is 0.1 - 6.0 h -1 , preferably 0.2 - 5 h -1 , most preferably 0.5 - 2 h -1 and the amount of hydrogen introduced is such that the volume ratio of hydrogen volume (liter) / hydrocarbon volume (liter) is 100 - 3000 nL / L, preferably 300 - 1500 nL / L. 【0105】 According to the present invention, the “temperature” of the reaction section corresponds to the weight-average bed temperature (WABT) as is well known to those skilled in the art. Unless otherwise specified, the “average temperature” of the reaction section is given under cycle initiation conditions. 【0106】 The space-spatiotemporal velocity (HSV) is defined here as the ratio of the hourly volumetric flow rate of optionally pre-treated feedstock to the volume of one or more catalysts. 【0107】 Hydrogen coating is defined as the ratio at 15°C of the volumetric flow rate of hydrogen obtained under standard temperature and pressure conditions to the volumetric flow rate of the feedstock to be treated, i.e., the feedstock that is sometimes pre-treated and does not take recycling into account (volume of feedstock (m³) 3 ) Standard H2 m 3 (Nm 3 (This is how it is written.)) 【0108】 Advantageously, the hydrogenation process is carried out in a hydrogenation reaction section comprising at least one, preferably 1 to 5, fixed-bed reactors having n catalyst beds, where n is an integer of 1 or more, preferably 1 to 10, and preferably 2 to 5, and each of the one or more beds contains at least one, and preferably 10 or fewer, hydrogenation catalysts. 【0109】 A hydrogenation reaction section using at least one fixed-bed reactor can be operated with downward or upward flow of gas and liquid. 【0110】 The hydrogen-containing gas stream supplied to the hydrogenation reaction section may consist of supply hydrogen and / or recycled hydrogen. The hydrogen-containing gas stream may be obtained from fossil sources or renewable sources, such as from the gasification of plastic waste or generated by electrolysis. 【0111】 Preferably, an additional gas stream containing hydrogen is advantageously introduced at the inlet of each reactor, particularly at the inlet of each reactor operating in series, and / or at the inlet of each catalyst bed from the second catalyst bed onward in the reaction section. These additional gas streams are also called cooling streams. They allow for control of the temperature inside the reactor, as the reaction being carried out is generally very exothermic. 【0112】 Preferably, step a) may use at least one guard bed upstream of one or more hydrogenation catalysts, containing an adsorbent and / or catalyst of the type alumina, silica-alumina, zeolite and / or activated carbon, which may optionally contain metals from Group VIB and / or Group VIII. A series of guard beds (catalysts) with particles of different diameters may be used, in particular a series of guard beds where the diameter decreases in the direction of feed flow (also called "grading"). The main role of the guard beds is to protect the catalyst in the main reactor of downstream step a) by performing some demetallation and by filtering out particles contained in the feed that could lead to clogging. The catalyst may contain at least one carrier comprising a porous refractory oxide, at least one Group VIB metal, and at least two Group VIII metals. The content of one or more Group VIB metals in these catalysts is 2% to 9% by weight of the trioxides of one or more Group VIB metals relative to the total mass of the catalyst, and the total content of Group VIII metals is 0.3% to 2% by weight of the oxides of Group VIII metals relative to the total mass of the catalyst. 【0113】 According to the modification, the feedstock passes through a filtration and distributing plate, consisting of a single or two consecutive steps, at the inlet of each guard zone, the plate located upstream of the catalyst bed, preferably upstream of each catalyst bed. This filtration and distributing plate, described, for example, in reference US2009177023, allows for the capture of clogging particles contained in the feedstock by a specific distributing plate containing a filtration medium. Thus, the filtration plate makes it possible to increase the cycle time savings in the method according to the present invention. The filtration plate also makes it possible to distribute the gas phase (hydrogen and the gaseous portion of the feedstock) and the liquid phase (the liquid portion of the feedstock) to be fed into the reactor while simultaneously performing a filtration function against impurities contained in the feedstock. Similarly, the filtration plate ensures a more uniform distribution of the mixture across the entire surface of the catalyst bed and limits the problem of misdistribution of the phase due to clogging of the plate itself. 【0114】 More precisely, the filtration plate is a filtration distribution device comprising a plate located upstream of the catalyst bed, the plate consisting of a substantially horizontal base plane, the base plane being integral with the reactor wall, and substantially vertical risers mounted thereon, opening at their upper ends for gas inflow and opening at their lower ends for discharge of a liquid-gas mixture intended to be fed to the catalyst bed located downstream, the risers being penetrated over specific portions of their height by continuous lateral slots or lateral orifices for liquid inflow, the plate supporting a filtration bed surrounding the risers, the filtration bed consisting of at least one layer of particles no larger than or equal to the size of the particles in the catalyst bed, the filtration bed consisting of particles that are generally inert but may also include at least one layer of catalyst that is identical or belongs to the same family as the catalyst in the catalyst bed. Modifications of this make it possible to reduce the volume of the catalyst bed in the reactor. 【0115】 The filtration distributor plate may comprise two steps and may consist of two consecutive plates: the first plate supports a guard bed consisting of internal particles and at least one layer of catalyst identical to or belonging to the same family as the catalyst of the catalyst bed. This plate is described in reference US2009177023. The bed is arranged on a grid, and the liquid phase flows through the guard bed, while the gas flows through risers that pass through the guard bed and the first plate. Once the blockage is cleared, the liquid and gas flow simultaneously through the risers, allowing the second plate to continue performing its distribution function. The second plate performs the function of distributing the gas and liquid: it may consist of risers with lateral perforations for the passage of liquid, or it may consist of bubble caps. 【0116】 Conventional hydrogenation catalysts may be used advantageously in supported or unsupported form, and preferably contain at least one amorphous support and at least one hydrogenation-dehydrogenation element selected from at least one non-precious metal element from Group VIB and Group VIII, and usually contain at least one element from Group VIB (either molybdenum or tungsten alone or in a mixture) and at least one non-precious metal element from Group VIII (either nickel or cobalt alone or in a mixture). Preferably, the hydrogenation catalyst contains a support selected from alumina, silica, silica-alumina, magnesia, clay and mixtures thereof, and a hydrogenation-dehydrogenation functional element containing either at least one element from Group VIII and at least one element from Group VIB, or at least one element from Group VIII. The reaction section of the hydrogenation process includes, for example, a hydrogenation catalyst on an amorphous support, preferably an alumina support, which comprises 0.5% to 12% by weight of nickel or cobalt, preferably 0.9% to 10% by weight of nickel or cobalt (expressed as oxide NiO or CoO relative to the weight of the catalyst) and 1% to 30% by weight of molybdenum and / or tungsten, preferably 3% to 20% by weight of molybdenum and / or tungsten (expressed as oxide MoO3 or WO3 relative to the weight of the catalyst). The hydrogenation catalyst may contain phosphorus. If phosphorus is present, its concentration is less than 10% by weight relative to the weight of the catalyst (expressed as P2O5), and advantageously at least 0.001% by weight relative to the total weight of the catalyst. 【0117】 Preferably, the amorphous carrier is alumina or silica-alumina. 【0118】 Suitable catalysts are selected from NiMo, NiW, NiMoW, or CoMo catalysts supported on alumina, and NiMo, NiW, or NiMoW catalysts supported on silica-alumina. 【0119】 According to another aspect of the present invention, the hydrogenation catalyst further comprises one or more organic compounds containing oxygen and / or nitrogen and / or sulfur. Such catalysts are often referred to in the term “additized catalyst.” Generally, the organic compounds are selected from compounds containing one or more chemical functional groups selected from functional groups of carboxylic acids, alcohols, thiols, thioethers, sulfones, sulfoxides, ethers, aldehydes, ketones, esters, carbonates, amines, nitriles, imides, oximes, ureas, and amides, or compounds containing furan rings, or sugars. 【0120】 Advantageously, the hydrogenation process a) allows for the hydrogenation of at least 80%, preferably all, of olefins (mono- and diolefins) and halogen compounds, as well as at least partial conversion of other impurities present in the feedstock, such as aromatic compounds, metallic compounds, sulfur compounds, nitrogen compounds, and oxygen compounds. 【0121】 Preferably, the nitrogen content at the outlet of step a) is 5 to 500 ppm by weight, preferably 10 to 40 ppm by weight. 【0122】 Preferably, the sulfur content at the exit of step d) is less than 200 ppm by weight, preferably less than 150 ppm by weight. 【0123】 Step a) makes it possible to reduce the content of contaminants, such as metals, and especially silicon. Preferably, the metal content at the exit of step a) is less than 10 ppm by weight, preferably less than 2 ppm by weight, and the silicon content is less than 5 ppm by weight. 【0124】 Preferably, the halogen element content at the exit of step a) is less than 2 ppm by weight. 【0125】 (Optional intermediate separation process) The method according to the present invention may, advantageously, include a separation step between the hydrogenation step and the hydrocracking step. 【0126】 According to one or more preferred embodiments, the method according to the present invention also includes a separation step, which separates part or all of the hydrogenated effluent to produce at least two fractions, one of which is a heavy fraction that boils at a temperature of 370°C or higher. 【0127】 One or more other fractions are one or more light intermediate fractions. The light fractions thus separated mainly contain gases (H2, HCl, H2S, NH3, and C1-C4), naphtha (or gasoline, fractions that boil at temperatures below 150°C), kerosene (fractions that boil at 150°C to 280°C), and at least a portion of gas oil (fractions that boil at 280°C to 370°C). The light fractions may then be sent to a fractionation unit, at least in part, where light gases are extracted from the light fraction, for example, by passing through an expansion vessel. This fractionation unit may be a fractionation unit described later (in section d of the separation process). 【0128】 The hydrogen gas recovered in this manner may be sent to purification and compression equipment, and, advantageously, may be recycled to a hydrogenation process a), a hydrocracking process b), and / or a second hydrocracking process, if such processes are performed. The recovered hydrogen gas may be used in other refinery equipment. 【0129】 This separation process is advantageous when the pyrolysis oil in the feedstock contains a large amount of chlorine. The most problematic impurities contained in pyrolysis oil are often halides, more specifically chlorine. This is because chlorine is generally a limiting contaminant when processing pyrolysis oil in existing units of a refinery. Even at low concentrations (e.g., <5 ppm by weight), chlorine can cause corrosion (in the form of HCl) that can occur in existing units, and its metallurgy is generally not designed to withstand even lower levels of chlorine. Another problem associated with the presence of halides, particularly chlorine, in pyrolysis oil is the formation of ammonium chloride salts, which are formed by the reaction between chloride ions released in the form of HCl by hydrodechlorination and ammonium ions generated in the form of NH3 by the hydrogenation of nitrogen compounds (hydrodenitrification) during the hydrogenation process. These ammonium chloride salts precipitate at relatively low temperatures (e.g., below 280°C) and are known to cause clogging problems, particularly in transfer lines and / or downstream sections of the hydrogenation process. 【0130】 This separation process (under high-temperature conditions) makes it possible to particularly remove halogens (chlorine) in the form of hydrogen halides (especially HCl) formed by the reaction of hydrogen ions and halide ions released by the hydrogenation of halogen compounds during the hydrogenation process, and also prevents the precipitation of ammonium chloride salts that may be formed by the reaction between chloride ions and ammonium ions and dissolved in the aqueous solution. The separation process therefore makes it possible to recover the heavy fraction that boils mainly at temperatures of 370°C or higher for hydrocracking, and removes the most common impurities, such as chlorine, as well as H2S and NH3 formed during the hydrogenation process. 【0131】 Another advantage of the separation process is that at least a portion of the naphtha, kerosene, and gas oil (primarily derived from pyrolysis oil) can be extracted before the hydrocracking process, thus avoiding excessive cracking into naphtha fraction and gas, especially when the goal is to maximize the kerosene and gas oil fractions. 【0132】 An optional separation step is performed in a separation section, which includes any separation means known to those skilled in the art. The separation section may comprise one or more expansion vessels arranged in series, and / or one or more steam and / or hydrogen stripping columns, and / or atmospheric distillation columns, and / or vacuum distillation columns, and preferably consists of a single expansion vessel, commonly referred to as a "hot separator." 【0133】 The optional separation process is generally carried out at high temperature and high pressure, operating at a pressure of 8 to 25 MPa and a temperature of 200°C to 450°C, preferably 250°C to 350°C. 【0134】 The separation section may include means for washing at least one separated fraction, in particular a light fraction mainly containing gas, by contact with an aqueous solution. 【0135】 According to a preferred embodiment, an optional separation step includes a hot separator operated at a temperature of 300°C or higher, or even 350°C or higher, to avoid the formation of ammonium chloride salts in the liquid phase. The gas phase of the hot separator, or at least one of the phases resulting from the subsequent separation of the gas phase of the hot separator, is advantageously contacted with water or a basic aqueous solution (e.g., a sodium hydroxide solution, one or more amines) for the purpose of removing at least a portion of the hydrogen chloride (HCl) and / or dissolving at least a portion of the ammonium chloride salts. The separation apparatus or separation vessel may be provided with a zone at the bottom for the separation and sedimentation of the aqueous fraction containing the hydrocarbon fraction and the chloride salt, or may be provided with a column for washing the gas by contact with water or a basic solution. 【0136】 In another embodiment, the method according to the present invention does not include a separation step between the hydrogenation step and the hydrocracking step. 【0137】 (Hydrocrack process b)) According to the present invention, the method includes a hydrocracking step b) carried out in a hydrocracking reaction section, using at least one fixed-bed reactor having n catalyst beds, where n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst, the hydrocracking reaction section is fed at least a portion of the hydrogenated effluent from step a) and a gas stream containing hydrogen, the temperature during operation of the hydrocracking reaction section is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 12.0 h -1 The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, and hydrocracking effluent is obtained. 【0138】 Advantageously, step b) carries out a hydrocracking reaction well known to those skilled in the art, more specifically enabling the conversion of heavy compounds, such as compounds with boiling points above 370°C contained in the hydrogenated effluent obtained from step a). Other reactions, such as hydrogenation, hydrometallation, hydrodesulfurization, hydrodenitrification of olefins or aromatic compounds, may also be carried out. 【0139】 Preferably, the temperature during the hydrocracking step according to the present invention is 200°C to 450°C, preferably 250°C to 450°C, and most preferably 300°C to 430°C, the pressure at which time is 2 to 18 MPa abs., preferably 3 to 16 MPa abs., and the spatiotemporal velocity at which time is 0.1 to 12.0 h. -1 Preferably 0.4 to 10 hours -1 , preferably 0.8 to 3 hours -1The amount of hydrogen introduced is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, preferably 300 to 1500 nL / L. 【0140】 The definitions of mean temperature (WABT), HSV, and hydrogen coverage correspond to the definitions above. 【0141】 These operating conditions used in the hydrocracking process generally make it possible to achieve a conversion rate per pass to a product with a boiling point below 340°C, more preferably below 370°C, of ​​more than 15% by weight, more preferably 50% to 95% by weight, relative to the feedstock introduced into the hydrocracking process. 【0142】 The degree of conversion can be adjusted according to the desired product. 【0143】 If the goal is to promote the formation of the naphtha fraction, the degree of conversion is preferably 80% by weight or more, preferably 80% to 95% by weight. 【0144】 If the goal is to promote the formation of intermediate distillate fractions, such as kerosene fractions or gas oil fractions, the degree of conversion is preferably less than 90% by weight, preferably 50% to 85% by weight. In fact, since the feedstock is a mixture of heavy feedstock of fossil origin and lighter feedstock of high paraffin and olefin pyrolysis oil (and therefore contains compounds with boiling points in the intermediate distillate range), the degree of conversion in the hydrocracking process must be moderate in order to avoid over-cracking and thus the formation of compounds lighter than the intermediate distillate fraction. 【0145】 Advantageously, step b) is carried out in a hydrocracking reaction section comprising at least one, preferably 1 to 5, fixed-bed reactors having n catalyst beds, where n is an integer of 1 or more, preferably 1 to 10, and preferably 2 to 5, and each of the beds comprises at least one, and preferably 10 or fewer, hydrocracking catalysts. 【0146】 A hydrocracking section using at least one fixed-bed reactor can be operated with downward or upward flows of gas and liquid. 【0147】 The hydrogenation and hydrocracking processes can, advantageously, be carried out in the same reactor or in different reactors. In the case where they are carried out in the same reactor, the reactor comprises several catalyst beds, the first catalyst bed comprising one or more hydrogenation catalysts, and the subsequent catalyst beds comprising one or more hydrocracking catalysts. 【0148】 The one or more types of hydrocracking catalysts used in the hydrocracking process are conventional hydrocracking catalysts known to those skilled in the art, and are of a dual-function type combining acid function with hydrodehydrogenation function, and may include at least one binder matrix. The acid function is due to a high surface area (generally 150-1000 m²) that exhibits surface acidity. 2 The hydrogenation-dehydrogenation function is provided by a support (g), for example, halogenated (especially chlorinated or fluorinated) alumina, combinations of aluminum and boron oxides, amorphous silica-alumina and zeolites, preferably alumina or silica-alumina, either alone or in mixtures. 【0149】 Preferably, the hydrocracking catalyst comprises a support selected from alumina halides, a combination of aluminum and boron oxides, amorphous silica-alumina, and zeolites, and a hydrodehydrogenating functional metal comprising at least one metal from Group VIB selected from chromium, molybdenum, and tungsten, preferably individually or in a mixture of molybdenum and tungsten, and / or at least one metal from Group VIII selected from iron, cobalt, nickel, ruthenium, rhodium, palladium, and platinum, preferably from cobalt and nickel. Hydrodehydrogenating functional metals of the type NiMo, NiMoW, or NiW are preferred. 【0150】 Preferably, the content of Group VIII metals in one or more types of hydrocracking catalysts is advantageously 0.5% to 15% by weight, preferably 1% to 10% by weight, and the percentage is expressed as the weight percentage of oxides (e.g., NiO or CoO) relative to the total weight of the catalyst. 【0151】 Preferably, the content of group VIB metals in one or more types of hydrocracking catalysts is advantageously 5% to 35% by weight, more preferably 10% to 30% by weight, and the percentage is expressed as the weight percentage of oxides (e.g., MoO3 or WO3) relative to the total weight of the catalyst. 【0152】 One or more types of hydrocracking catalysts may optionally contain at least one promoter element, which is deposited on the catalyst and is selected from the group formed by phosphorus, boron and silicon, optionally at least one element from group VIIA (chlorine and fluorine are preferred), optionally at least one element from group VIIB (manganese is preferred), and optionally at least one element from group VB (niobium is preferred). 【0153】 One type of conventional hydrocracking catalyst is based on moderately acidic amorphous oxides, such as silica-alumina. These systems are used to produce high-quality intermediate distillates and, in some cases, oil bases. The drawback of these amorphous support-based catalysts is their low activity. 【0154】 Catalysts containing, for example, Y-zeolite or beta-zeolite exhibit higher catalytic activity than silica-alumina for some of their components, but generally exhibit lower selectivity for intermediate distillates (jet fuel and diesel). 【0155】 Preferably, one or more types of hydrocracking catalysts may include, in some cases, a zeolite selected from Y zeolite, preferably USY zeolite, either alone or in combination with other zeolites from beta, ZSM-12, IZM-2, ZSM-22, ZSM-23, SAPO-11, ZSM-48, or ZBM-30 zeolites, either alone or in a mixture. 【0156】 In cases where the catalyst contains zeolite, the zeolite content in one or more types of hydrocracking catalysts is advantageously 0.1% to 80% by weight, preferably 3% to 70% by weight, and the percentage is expressed as the percentage of zeolite relative to the total weight of the catalyst. 【0157】 A suitable catalyst comprises, and preferably consists of, at least one metal from Group VIB and optionally at least one non-precious metal from Group VIII, at least one promoter element, preferably phosphorus, at least one Y zeolite, and at least one alumina binder. 【0158】 Even more preferred catalysts include, and preferably consist of, nickel, molybdenum, phosphorus, USY zeolite, and optionally beta zeolite and alumina. 【0159】 Other preferred catalysts include, and preferably consist of, nickel, tungsten, alumina, and silica-alumina. 【0160】 Other preferred catalysts include, and preferably consist of, nickel, tungsten, USY zeolite, alumina, and silica-alumina. 【0161】 The hydrogenocrack catalyst is, for example, in the form of an extruded product. 【0162】 According to another aspect of the present invention, the above-described hydrocracking catalyst also includes one or more organic compounds containing oxygen and / or nitrogen and / or sulfur. Such catalysts are often referred to in the term “additive catalyst.” Generally, the organic compounds are selected from compounds containing one or more chemical functional groups selected from functional groups of carboxylic acids, alcohols, thiols, thioethers, sulfones, sulfoxides, ethers, aldehydes, ketones, esters, carbonates, amines, nitriles, imides, oximes, ureas, and amides, or compounds containing furan rings, or sugars. 【0163】 The preparation of the catalysts in steps a) and b) is known and generally involves impregnation of a support with metals from Group VIII and Group VIB, if present, and optionally phosphorus and / or boron, followed by a drying step, and then optionally a calcination step. In the case of additive catalysts, the preparation is generally carried out by simply drying without calcination after the introduction of the organic compound. The term “calcination” is understood here to mean heat treatment under air or an oxygen-containing gas at a temperature of 200°C or higher. Prior to their use in the steps of this method, the catalysts are generally subjected to sulfidation to form active entities. 【0164】 Advantageously, the hydrocracking step b) allows for the conversion of remaining impurities in the hydrotreated effluent, such as aromatic compounds, metallic compounds, sulfur compounds, nitrogen compounds, and oxygen compounds. 【0165】 Preferably, the nitrogen content at the outlet of step b) is less than 300 ppm by weight, preferably less than 100 ppm by weight, and preferably less than 50 ppm by weight. 【0166】 (Separation step c)) According to the present invention, the method includes a separation step c), to which at least a portion, preferably all, of the hydrocracking effluent from step b) is fed to a separation section to produce at least one gaseous effluent containing hydrogen and at least one liquid effluent. 【0167】 The purpose of separation, or at least one of the two or more separations, is to separate a liquid effluent containing hydrocarbons from a gaseous effluent containing unreacted hydrogen, thereby upgrading / continuing the treatment of hydrocarbons and, where appropriate, enabling the recycling of unreacted hydrogen. In this case, the gaseous effluent containing hydrogen (unreacted) may need to be treated for recycling. This includes, among other things, purification and washing with amines. 【0168】 The separation means can be operated under high pressure, and a series of high-pressure separator containers operating at 2 to 25 MPa can be used as the separation means. 【0169】 Those goals are to produce the following: - Hydrogen stream: Preferably recycled via a compressor to at least one of steps a) and b) (or to the second hydrocracking step if the method is a two-step hydrocracking type in another variation), or to other facilities in the refinery; and - The liquid effluent generated in step b) hydrocracking; this is preferably sent to a steam stripping step, which is operated at a pressure of 0.5 to 2 MPa, to separate the hydrogen sulfide (H2S) dissolved in the liquid effluent. 【0170】 Step c) thus enables the generation of a liquid hydrocarbon effluent, which can then be sent to step d). This series of separator vessels and stripping columns can be realized according to the teachings of patent EP 3 184 607, which uses a high-pressure hot separator vessel, a high-pressure cold separator vessel, a compression zone, a low-pressure hot separator vessel, and a stripping column; reference may be made to the said patent for more details. 【0171】 The separation section may also include means for washing at least one separated fraction by contact with an aqueous solution. 【0172】 According to one preferred embodiment, the separation step includes a hot separator operated at a temperature of 300°C or higher, or even 350°C or higher, to avoid the formation of ammonium chloride salts in the liquid phase; the gas phase of the hot separator, or at least one of the phases resulting from the subsequent separation of the gas phase of the hot separator, and at least a portion of the liquid phase of the hot separator, or at least one of the phases resulting from the subsequent separation of the liquid phase of the hot separator, are advantageously placed in contact with water or a basic aqueous solution (e.g., a sodium hydroxide solution or a solution of one or more amines) to at least partially remove hydrogen chloride (HCl) and / or at least partially dissolve the ammonium chloride salts. This alternative is of particular interest if separation is not completed even after optional washing between the hydrogenation step and the first hydrocracking step. The separation apparatus or separation vessel may have a zone at the bottom for the separation and sedimentation of the aqueous fraction containing the hydrocarbon fraction and the chloride salts, or may have a column for washing the gas by contact with water or a basic aqueous solution. 【0173】 (Fractional process d)) According to the present invention, the method includes a fractionation step d), to which at least a portion, preferably all, of the liquid effluent from step c) is fed to a fractionation section to produce at least one naphtha fraction, at least one intermediate distillate fraction, and at least one unconverted heavy liquid fraction. 【0174】 The fractionation step d) is carried out in at least one distillation column. 【0175】 The distillation column is operated at an absolute pressure of 0.1 to 0.4 MPa. 【0176】 The distillation fractionation step d) makes it possible to extract, in particular, the following: - Optional gaseous fraction, - At least one naphtha fraction, - At least one intermediate distillate fraction, and - Unconverted heavy liquid fraction with a boiling point above 370°C; the fraction is drawn out at the level of the lower end of the column. 【0177】 The term "naphtha fraction" is generally understood to refer to a hydrocarbon fraction containing compounds with boiling points below 150°C, particularly between 80 and 150°C. 【0178】 The term "intermediate distillate fraction" is generally understood to mean a hydrocarbon fraction containing compounds with boiling points between 150 and 370°C. Intermediate distillate fractions generally include kerosene fractions with boiling points between 150°C and below 250°C and / or gaseous oil fractions with boiling points between 250 and 370°C. 【0179】 The term "unconverted heavy liquid fraction" is understood to mean a hydrocarbon fraction containing compounds with a boiling point above 370°C, which also includes some unconverted feedstock (also known as UCO, which stands for Unconverted Oil). 【0180】 Those skilled in the art will adjust the fractionation point in the separation and / or distillation operation depending on the destination or use of the fraction obtained from the fractionation process. For example, it may be necessary to adjust the endpoint of the naphtha fraction to 125, 150, 175, 180, or 200°C. 【0181】 The naphtha fraction, kerosene fraction, and / or gas oil fraction may be sent to conventional fuel storage units derived from petroleum supply raw materials, such as naphtha storage units, kerosene storage units, or gas oil storage units. 【0182】 The product obtained by this method may therefore be a naphtha fraction, an intermediate distillate fraction (kerosene fraction and / or gas oil fraction), or an unconverted heavy liquid fraction, and may contain biobase carbon according to ASTM D6866 in a content of 0.1% to 15% by weight. 【0183】 According to the modification, at least a portion, preferably all, of the kerosene fraction and / or gas oil fraction is sent to their respective fuel pools. 【0184】 The addition of small fractions of highly paraffinic and olefinic pyrolysis oils can lead to an increase in the yield of the products (naphtha, kerosene, and gas oil) and can also improve the quality of the gas oil fraction; • The cetane number increases compared to gas oil fractions derived 100% from fossil fuels. • The density is lower compared to gas oil fractions derived 100% from fossil fuels. • The sulfur content is lower compared to gas oil fractions derived 100% from fossil fuels. 【0185】 The aromatic compound content in the intermediate distillate fraction (kerosene fraction or gas oil fraction) is relatively high due to the properties of the fossil heavy feedstock, and since oil preferably does not contain aromatic compounds, it generally decreases after the addition of pyrolysis oil to the feedstock. 【0186】 The specifications for density, sulfur content, cetane number, and cloud point of the gas oil fraction are met. The same applies to the specifications for density, sulfur content, freezing point, and smoke point of the kerosene fraction. 【0187】 According to another variation, a portion of the kerosene fraction and / or fuel oil fraction may be sent to a steam cracking unit. 【0188】 According to another modification, at least a portion of the naphtha fraction can be sent to a steam decomposition unit, where olefins may be (re)formed at the end to participate in polymer formation. 【0189】 The unconverted heavy liquid fraction can be recycled in part to a hydrogenation step a) and / or a hydrocracking step b) and / or a second hydrocracking step. Furthermore, it has a higher viscosity index than in the case of 100% fossil fuels. 【0190】 (Second hydrocracking step (optional)) The method according to the present invention may include a second step of hydrocracking at least a portion of the unconverted heavy fraction and / or intermediate distillate fraction resulting from fractionation step d) in the presence of hydrogen and at least one hydrocracking catalyst, to obtain a second hydrocracking effluent. 【0191】 If it is desired to promote the generation of an intermediate distillate fraction, such as a kerosene fraction or a gas-oil fraction, the second hydrocracking step is fed at least a portion of the unconverted heavy fraction. 【0192】 If it is desired to promote the formation of the naphtha fraction, the second hydrocracking step is fed at least a portion of the intermediate distillate fraction, and possibly at least a portion of the unconverted heavy fraction. 【0193】 The second hydrocracking step is carried out in a manner similar to that described for the first hydrocracking step (b). This applies particularly to the operating conditions, the equipment used, the supported porous hydrogenation catalyst used, and the degree of conversion. 【0194】 In this second hydrocracking step, the operating conditions may be the same as or different from those in the first hydrocracking step. 【0195】 The hydrocracking catalyst used in the second hydrocracking step may be the same as or different from the one used in the first hydrocracking step b), and is preferably different. 【0196】 The second hydrocracking effluent is preferably sent to separation step c) at least in part. 【0197】 According to the present invention, the second hydrocracking step is carried out in a hydrocracking reaction section, using at least one fixed-bed reactor having n catalyst beds, where n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst, the hydrocracking reaction section is fed at least a portion of the unconverted heavy fraction and / or intermediate distillate fraction produced from fractionation step d) and a gas stream containing hydrogen, the temperature during operation of the hydrocracking reaction section is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 12.0 h -1 The amount of hydrogen introduced is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, and a second hydrocracking effluent is obtained. 【0198】 Preferably, the temperature during the second hydrocracking step according to the present invention is 200°C to 450°C, preferably 250°C to 450°C, and most preferably 300°C to 430°C, the pressure is 2 to 18 MPa abs., preferably 3 to 16 MPa abs., and the spatiotemporal velocity is 0.1 to 12.0 h. -1 Preferably 0.4 to 10 hours -1 , preferably 0.8 to 3 hours -1 The amount of hydrogen introduced is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, preferably 300 to 1500 nL / L. 【0199】 Figure 1 shows a diagram of a specific embodiment of the method of the present invention, and includes the following: - Optional step (1); pre-treat the pyrolysis oil (2); for example, by filtration and / or nitrogen stripping; to obtain the pre-treated oil (3); - Step a); A feedstock containing a small fraction of pre-treated pyrolysis oil (3) and a heavy fraction (5) of fossil hydrocarbons is hydrogenated (4) in the presence of hydrogen-rich gas (6); carried out in at least one fixed-bed reactor containing at least one hydrogenation catalyst; hydrogenated effluent (7) is obtained; - Hydrocracking (8) is carried out in the presence of at least some hydrogen (9) of the hydrogenated effluent (7) obtained from step b); step a); carried out in at least one fixed-bed reactor containing at least one hydrocracking catalyst; to obtain hydrogenated effluent (10); - Step c); Separation (11) of the hydrocracking effluent (10); optionally performed in the presence of an aqueous washing solution (12), to obtain at least one gaseous effluent (13) containing hydrogen, at least one liquid effluent (14), and optionally an aqueous effluent (15) containing dissolved salts; - Step (16); fractionate the liquid effluent (14); making it possible to obtain at least a naphtha fraction (17), a kerosene fraction (18), a gas oil fraction (19), and an unconverted heavy liquid fraction (20) having a boiling point above 370°C. 【0200】 Optionally, an unconverted heavy liquid fraction (20) having a boiling point above 370°C can be recycled to a hydrogenation step a) and / or a hydrocracking step b) (not shown). 【0201】 Optionally, an unconverted heavy liquid fraction (20) having a boiling point above 370°C may be sent to a second hydrocracking step (21), which is carried out in at least one fixed-bed reactor containing at least one hydrocracking catalyst and supplied with hydrogen (22). The second hydrocracking effluent (23) is sent to separation step c)(11). 【0202】 Only the main processes are shown in Figure 1 along with the main flow, enabling a better understanding of the present invention. It is clear that all the equipment necessary for the operation (vessels, pumps, exchangers, furnaces, columns, etc.) is present, even if they are not shown in the figure. It is also understood that the hydrogen-rich gas stream (supply or recycle) may be injected into the inlet of each reactor or catalyst bed, or between two reactors or two catalyst beds, as described above. Means well known to those skilled in the art for hydrogen purification and recycling may also be employed. 【0203】 (Examples) The following examples are intended to demonstrate specific performance qualities of the method according to the present invention. 【0204】 These examples illustrate the possibility of co-treating plastic pyrolysis oil in a method for producing intermediate distillates and naphtha, which includes a hydrotreatment step and a hydrocracking step. Further demonstrated is the ability of catalysts present in the hydrotreatment and hydrocracking steps to capture impurities present in the pyrolysis oil, and thus obtain products that meet specifications. 【0205】 Example 1 is a comparative example illustrating the performance quality of a method that includes a hydrogenation process and a hydrocracking process for a standard feed stock (vacuum distillate) that does not contain plastic pyrolysis oil. 【0206】 Example 2 illustrates the performance quality of a method according to the present invention, which includes a hydrogenation step and a hydrocracking step, using a feedstock containing a fraction of plastic pyrolysis oil and a fraction of the standard feedstock used in Example 1 (vacuum distillate). The mixture was used in a pre-process (optional step) prior to media homogenization. 【0207】 (Feed material) The feedstock fraction (I) is a "straight-run" vacuum distillate (VGO-SR) directly derived from crude oil distillation. The feedstock fraction (II), plastic pyrolysis oil, is a pyrolysis oil obtained from a mixture of plastics and contains high levels of impurities. 【0208】 The main characteristics of these two fractions of the raw materials are shown in Table 1 below. 【0209】 Analytical methods and / or standards used to determine the characteristics of various flows, particularly the feedstocks to be processed and the resulting effluents, are known to those skilled in the art. These are listed below, in particular, for informational purposes. Other equivalent methods may also be used, including, among others, equivalent IP, EN, or ISO methods. 【0210】 [Table 1] 【0211】 (Operating conditions) The raw materials are injected into the preheating process, and then into the first hydrogenation reactor. The operating conditions are summarized in Table 2 below. 【0212】 [Table 2] 【0213】 The hydrogenation treatment of the alumina feedstock with a NiMo hydrogenation catalyst is carried out under operating conditions that enable a nitrogen content of 16 ppm to be obtained in the hydrogenated feedstock, i.e., at the inlet of the hydrogenation catalyst bed. 【0214】 All of the hydrogenated effluent from the hydrogenation section is then sent directly to the hydrocracking section without an intermediate separation step. The temperature of the hydrocracking catalyst is controlled to achieve 370°C and a total conversion of 69% by weight of the fraction. 【0215】 The operating conditions for the hydrocracking process are summarized in Table 3 below. 【0216】 [Table 3] 【0217】 (Overall results and performance quality) By treating with a mixture of 90% VGO and 10% plastic pyrolysis oil, it is possible to lower the temperature of the hydrotreatment section by 4°C and the temperature of the hydrocracking section by 2°C compared to treating with 100% VGO. In other words, this allows for a slight reduction in cycle time. 【0218】 The yield obtained at the end of the series of hydrogenation and hydrocracking processes is expressed as a mass percentage relative to the fresh feedstock and is shown in Table 4 below. 【0219】 [Table 4] 【0220】 With an equiconversion rate of 69%, a feedstock consisting of a mixture of 90% VGO by volume and 10% plastic pyrolysis oil resulted in yield increases of 0.5% by weight in the naphtha fraction, 1.3% by weight in the kerosene fraction, and 0.5% by weight in the gas oil fraction compared to a test using 100% VGO by volume. 【0221】 The properties of the naphtha fraction (C5-150℃) are described in detail in Table 5 below. 【0222】 [Table 5] 【0223】 The naphtha fraction obtained from a mixture of 90% VGO by volume and 10% plastic pyrolysis oil by volume contains more paraffinic compounds than the naphtha fraction obtained from a feedstock of 100% VGO by volume. This fraction is therefore more suitable for being sent to a steam cracking unit to convert the paraffinic components into olefinic components (mainly ethylene and propylene) for the production of various polymers in the chemical industry. 【0224】 The characteristics of the kerosene fraction (150-250°C) are detailed in Table 6 below. 【0225】 [Table 6] 【0226】 Kerosene obtained from a feedstock mixture consisting of 90% VGO and 10% plastic pyrolysis oil meets JET A1 specifications in terms of properties such as density, sulfur content, aromatic compound and naphthalene content, and freezing point and smoke point. Compared to the kerosene fraction obtained in the case of 100% VGO, the kerosene fraction obtained by mixing 90% VGO and 10% plastic pyrolysis oil is better in terms of density, smoke point, and aromatic compound content. 【0227】 The characteristics of the gas oil fraction (250-370°C) are detailed in Table 7 below. 【0228】 [Table 7] 【0229】 The gas oil produced from a feedstock mixture consisting of 90% VGO by volume and 10% plastic pyrolysis oil by volume meets the specifications in terms of sulfur content, density, cetane number, cloud point, and filterability temperature. Compared to the gas oil fraction obtained in the case of 100% VGO by volume, the gas oil fraction obtained by mixing 90% VGO by volume and 10% plastic pyrolysis oil is better in terms of density and cetane number. 【0230】 Table 8 refers to the viscosity characteristics of the unconverted oil (fraction 370+°C). 【0231】 [Table 8] 【0232】 Unconverted oil resulting from a mixture (90 / 10% vol / vol) of plastic pyrolysis oil with VGO (370+℃) shows a 4-point increase in viscosity index compared to the case of 100% vol VGO due to the paraffinic properties of the plastic pyrolysis oil. Furthermore, the viscosity of the unconverted oil resulting from the mixture is lower than the viscosity from 100% vol VGO. [Brief explanation of the drawing] 【0233】 [Figure 1] An embodiment of the hydrogenation conversion method according to the present invention is shown schematicly.

Claims

[Claim 1] A method for producing intermediate distillates and naphtha from a feedstock comprising a heavy fraction of fossil hydrocarbons and a fraction of pyrolysis oil from plastics and / or tires and / or solid recovery fuels, wherein at least 50% by weight of the compounds in the heavy fraction have an initial boiling point greater than 300°C and a final boiling point less than 700°C, the pyrolysis oil fraction contains paraffinic and olefinic compounds in a proportion of more than 60% by weight relative to the weight of the pyrolysis oil, the pyrolysis oil fraction constitutes less than 50% by weight of the feedstock, and the method comprises the following steps: a) Hydrogenation process; carried out in a hydrogenation reaction section; using at least one fixed-bed reactor having n catalyst beds; n is an integer of 1 or more, each containing at least one hydrogenation catalyst; at least the feed material and a gas stream containing hydrogen are supplied to the hydrogenation reaction section; the temperature when using the hydrogenation reaction section is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 6.0 h －１ The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L; hydrogenated effluent is obtained; b) Hydrocracking step; carried out in a hydrocracking reaction section; using at least one fixed-bed reactor having n catalyst beds; n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst; at least a portion of the hydrogenated effluent from step a) and a gas stream containing hydrogen are supplied to the hydrocracking reaction section; the temperature during operation of the hydrocracking reaction section is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 12.0 h －１ The amount of hydrogen introduced at that time is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L; the hydrocracking effluent is obtained; c) Separation process; feeding at least a portion of the hydrocracking effluent from process b) to a separation section; producing at least one gaseous effluent containing hydrogen and at least one liquid effluent; d) Fractionation step; feeding at least a portion of the liquid effluent from step c) to a fractionation section; producing at least one naphtha fraction, at least one intermediate distillate fraction, and at least one unconverted heavy liquid fraction. [Claim 2] The method according to claim 1, wherein the pyrolysis oil fraction constitutes 1% to 45% by weight of the supply raw material. [Claim 3] The method according to claim 1 or 2, wherein the supply material consists of the pyrolysis oil fraction and the heavy hydrocarbon fraction of fossil origin, the pyrolysis oil fraction constitutes 1% to 45% by weight of the supply material, and the heavy hydrocarbon fraction constitutes 55% to 99% by weight of the supply material. [Claim 4] The method according to any one of claims 1 to 3, wherein the content of aromatic compounds in the pyrolysis oil fraction is less than 30% by weight. [Claim 5] The method according to any one of claims 1 to 4, wherein the heavy fraction of fossil hydrocarbons is selected from a heavy fraction of fossil origin obtained from the direct distillation of crude oil, or from a vacuum distillate obtained from a hydrotreatment, hydroconversion or hydrocracking method applied to a residue at atmospheric pressure or under reduced pressure and operated in a fixed bed, moving bed, boiling bed or slurry bed; or from a conversion unit such as fluid catalytic cracking; or from a coking method; or from a vis-breaking method; or from a unit for extracting aromatic compounds from a lubricating oil base; or from a fraction obtained from solvent dewaxing of a lubricating oil base; or from dewaxed oil obtained from solvent dewaxing of a residue; or from any mixture of the above-mentioned feedstocks. [Claim 6] The method according to claim 5, wherein the heavy fraction of fossil-derived hydrocarbons is a vacuum distillate. [Claim 7] The method according to any one of claims 1 to 6, wherein the pyrolysis oil is selected from pyrolysis oils derived from polyethylene and / or polypropylene. [Claim 8] The method according to any one of claims 1 to 7, wherein the pyrolysis oil contains bio-based carbon according to ASTM D6866 in a content of 20% to 70% by weight. [Claim 9] The method according to any one of claims 1 to 8, wherein the feed material containing the heavy fraction and the pyrolysis oil fraction of fossil hydrocarbons, or only the pyrolysis oil, or only the heavy feed material of fossil hydrocarbons, is subjected to a pretreatment step, the pretreatment step is performed upstream of step a), and includes an adsorption step and / or a filtration step and / or a centrifugation step and / or a sedimentation step and / or an electrostatic separation step and / or a washing step using an aqueous solution and / or a gas stripping step. [Claim 10] The method according to any one of claims 1 to 9, wherein the filter plate is integrated upstream of the first catalyst bed at the inlet of step a). [Claim 11] The method according to any one of claims 1 to 10, wherein the separation step in the separation section is included between the hydrogenation step a) and the hydrocracking step b), and part or all of the hydrogenated effluent is separated to produce at least two fractions mainly consisting of a heavy fraction that boils at a temperature of 370°C or higher. [Claim 12] The method according to any one of claims 1 to 11, wherein the separation section of step c) and / or the separation section between the hydrogenation step a) and the hydrocracking step b) includes means for washing the separated fraction by contact with an aqueous solution. [Claim 13] The method according to any one of claims 1 to 12, wherein the degree of conversion in step b) is 50% by weight to 95% by weight. [Claim 14] The process also includes a second hydrocracking step carried out in the hydrocracking reaction section, and uses at least one fixed-bed reactor having n catalyst beds, where n is an integer of 1 or more, each containing at least one type of hydrocracking catalyst, and feeds the hydrocracking reaction section with at least a portion of the unconverted heavy fraction and / or intermediate distillate fraction produced from fractionation step d) and a gas stream containing hydrogen, and the temperature when operating the hydrocracking reaction section is 200 to 450°C, the pressure is 2.0 to 18.0 MPa abs., and the spatiotemporal velocity is 0.1 to 12.0 h. －１ The method according to any one of claims 1 to 13, wherein the amount of hydrogen introduced is such that the volume ratio of hydrogen volume (liters) / hydrocarbon volume (liters) is 100 to 3000 nL / L, and a second hydrocracking effluent is obtained. [Claim 15] A product obtained by the method according to any one of claims 1 to 14. [Claim 16] The product according to claim 15, comprising a bio-based carbon content of 0.1% to 15% by weight according to ASTM D6866.

Images