Process for producing atmospheric distillates from heavy oil fractions obtained from the solvolysis of used elastomers.

Abstract

A process for producing atmospheric distillate from spent elastomer solvolysis oil comprises the following steps: an elastomer solvolysis step under specific conditions to obtain a first gaseous effluent and a first liquid effluent containing carbon black; liquid / solid separation and fractionation steps of the first liquid effluent to recover carbon black on the one hand, and various liquid fractions including a heavy hydrocarbon fraction with an initial boiling point between 340°C and 440°C; a catalytic cracking step of said heavy hydrocarbon fraction obtained in a fluidized bed reactor in the presence of a solid catalyst, at a temperature between 500°C and 700°C, a pressure between 0.1 and 0.6 MPa to obtain an atmospheric distillate composed of at least a gasoline fraction and a diesel fraction. [Fig. 1] to be published for the abstract

Description

Title of the invention: Process for producing atmospheric distillates from heavy oil fractions obtained from the solvolysis of used elastomers. Scope of the invention

[0001] The present invention relates to the recycling of used elastomers by a process of solvolysis of used elastomers and to the valorization of the solvolysis oil in atmospheric distillates. State of the art

[0002] Elastomers are chemically cross-linked polymers of natural or synthetic rubber. Due to their chemical bonds, they do not melt but begin to decompose at high temperatures. Natural rubber is primarily composed of polyisoprene, a natural polymer found in the rubber tree (Hevea brasiliensis) and guayule. Synthetic rubbers are either general-purpose or specialty rubbers and are created by combining different polymers, monomers, and laminates.Common synthetic rubbers include (but are not limited to) styrene-butadiene copolymer (SBR), polybutadiene (BR), isobutylene-isoprene copolymer (IIR, CIIR, BIIR), ethylene-propylene-diene monomer (EPDM), polychloroprene (CR), acrylonitrile-butadiene copolymer (NBR, HNBR), chlorosulfonated polyethylene (CSM), fluoroelastomer (FKM), polyacrylate rubber (ACM), epichlorohydrin rubber (ECO), and silicone rubber (VMQ).

[0003] These materials are used to manufacture various objects such as tires for light vehicles, heavy goods vehicles, two-wheelers or any type of special equipment, treads in conveyor systems, vehicle door seals, but also objects such as shoe soles or rubber boots.

[0004] At the end of their life, these elastomer-rich objects undergo, to facilitate their material recovery, for example, a granulation treatment to isolate the elastomer-rich parts of the objects in question and to eliminate the majority of the other constituents (such as, for example, the metallic or synthetic fabrics and fibers often incorporated into the elastomers to enhance their properties) and to form granules generally smaller than 25 mm. Granulation generally consists of a series of grinding and separation steps and makes it possible to obtain a resulting material composed of the elastomer and the reinforcing fillers incorporated with the elastomer, such as carbon black or silica, for example.

[0005] Carbon black (or CB, as it is known in English) is used in tire formulations to improve their resistance (in terms of strength and lifespan), to limit tire deformation during use, and to facilitate heat transfer between the tires and the road surface. It is generally obtained by the incomplete combustion of hydrocarbons or vegetable oils, and more than 35 grades are commercially available and used as fillers (primarily in tire compound formulations). Their quality varies according to their intrinsic properties.

[0006] Processes for converting used elastomers by thermal decomposition generally aim to produce gaseous, liquid, and solid fractions of interest for recovery. In the case of used tires, the tire is generally initially shredded to obtain either tire shreds still containing some of the textile fibers or metal wires contained in the tire (typically pieces of 10 cm) or granules (generally smaller than 5 mm) free of textile fibers or metal wires. These prepared materials can then be reacted by exposing them to temperature to decompose the used tire and recover a gaseous fraction, a liquid fraction, and a solid fraction. To achieve tire decomposition, it is generally necessary to expose the tire to a fairly high temperature, usually between 300°C and 900°C, for reaction times ranging from 30 minutes to several hours.

[0007] Numerous technologies exist for implementing these reactions. For example, tires can be exposed to temperature in rotating furnaces (Lewandowski et al., Journal of Analytical and Applied Pyrolysis, 140, 2019, 25-53), or in moving beds (EP2661475). These technologies are robust but generally require working at fairly high temperatures, typically averaging over 500°C.In these processes, carbon black, generally present in the feedstock at a level of 25-40% by weight and initially composed of very fine sub-micrometer or micrometer particles / agglomerates, tends to agglomerate in the presence of decomposed gum, which forms a coke binding these structures at different scales. The solid often exits the reactor in the form of blocks several millimeters / centimeters in size, which must then be finely ground in order to reuse this solid as carbon black, a process requiring significant energy expenditure. In these processes, temperature conditions are high, and the reactor contains primarily gaseous and solid fractions. The liquids produced result from the condensation of the gaseous products downstream of the reactor. These high temperature conditions also tend to favor polycondensation and coking reactions to form polyaromatic structures from reactions of [missing information]. Cyclization involving the aromatic and olefinic structures present (MF Laresgoiti, BM Caballero, I. de Marco, A. Torres, MA Cabrero, MJ Chomôn. J. Anal. Appl. Pyrolysis 71 (2004) 917-934) or coke. The higher the temperature, the greater the levels of polyaromatic structures formed and the amount of coke produced. However, while aromatic molecules are good solvents and have numerous applications, particularly as petrochemical bases, polyaromatic structures, on the other hand, are detrimental to the quality of the liquid formed and very difficult to refine or convert. They are also precursors of ideal coke. Therefore, it is advantageous to try to limit polycondensation reactions as much as possible to produce a minimum of polyaromatic structures while preserving the existing monoaromatic structures.

[0008] To improve the quality of the solid phase and limit coke formation on carbon black, it is possible to lower the hydrocarbon partial pressure by injecting steam during the cracking reactions. However, these reactions require a high temperature above 500°C to carry out the cracking under essentially gas-solid conditions (US2016 / 0083657). These gas-solid processes generally induce very high levels of non-condensable gas production under atmospheric conditions, ranging from 10 to 25% by weight relative to the tire charge entering the reactor. However, the recovery of reaction gases is locally complex. These gases are therefore generally used to produce the heat required to carry out the reactions, but this is done at the expense of the quantity of easily recoverable liquid products, which is thus limited.

[0009] An alternative method involves bringing the tire particles into contact with a liquid, heating the liquid, and dissolving and converting the tire particles into a homogeneous liquid phase in which the tire particles are agitated and gradually disappear. An example of this implementation is given in US 3,978,199 and US 3,704,108. This type of process allows the recovery of carbon black in liquid phase after filtration without agglomeration of these particles or coke deposition on their surface, as occurs in reactions operating in the gas-solid phase. Furthermore, implementing the process at temperatures below 450°C limits the polycondensation reactions of aromatics, the formation of coke on the surface of the carbon black particles, and the formation of gas, which is generally between 1% and 7% by weight of the incoming particle.The use of a solvent containing aromatic fractions, preferably mono-aromatic, is advantageous and allows for better dissolution of the feed in the reactor.

[0010] In most elastomer recycling units using the methods mentioned above, the liquid products are recovered as a high-sulfur fuel oil with low commercial value if recovered as is. These products can They can also be sent to refining and petrochemical complexes and processed in blends with hydrocarbon fractions from petroleum. The biogenic carbon content of the liquid fractions resulting from elastomer processing (related to the natural rubber content in the elastomers) increases the renewable nature of the resulting hydrocarbon fractions.

[0011] Fluid catalytic cracking (FCC) units are present in nearly one out of every two refineries. They allow the conversion of heavy hydrocarbon feedstocks, whose initial boiling point is generally above 340°C, into lighter hydrocarbon fractions, particularly middle distillates, by cracking the molecules of the heavy feedstock in the presence of an acid catalyst.

[0012] E. Rodriguez et al. (Production of Non-Conventional Fuels by Catalytic Cracking of Scrap Tires Pyrolysis Oil Ind. Eng. Chem. Res. 2019, 58, 5158-5167) demonstrates the possibility of utilizing pyrolysis oil in a catalytic cracking process. However, the article highlights the formation of polyaromatics that do not convert to gasoline or diesel fuel and lead to the formation of more coke compared to a traditional petroleum feedstock. The formation of polyaromatics limits the gasoline or diesel fuel yield in the catalytic cracking process. Objects of the invention

[0013] The Applicant has developed a new process for recovering value from solvolysis oils into atmospheric distillate (gasoline and diesel). Said process combines a reaction step of solvolysis of used elastomers, preferably based on used tires, a step of fractionation of the solvolysis oil, and a step of conversion of the heavy fraction of the solvolysis oil in order to recover an atmospheric distillate, with an improved yield compared to prior art processes using traditional petroleum fractions, and reduced coke formation.

[0014] The process consists of recycling a batch of spent elastomers by contacting said batch with a solvent consisting of at least one hydrocarbon fraction comprising a high content of aromatic compounds, a low content of C40+ compounds (vacuum residues), and a moderate content of C5-C10 hydrocarbon compounds (gasoline), said solvent being able to be produced from the process itself (recycled). The operating conditions and the composition of the hydrocarbon fraction, as defined, allow for:

[0015] - maximize the production of recovered carbon black via improved dissolution / decomposition of the solid charge while limiting the presence of carbonaceous residues in the final recovered carbon black;

[0016] - minimize gas production and therefore maximize the oils of interest;

[0017] - to generate higher quality oils, whose aromatic compounds are essentially monoaromatic and diaroaromatic, significantly limiting the proportion of polyaromatics formed during the recycling of elastomers.

[0018] Indeed, the solvolysis oil produced, and in particular the heavy fraction of the oil with a boiling point above 340°C, possesses interesting properties and characteristics (predominantly mono-aromatic structure, limited polyaromatic content). Treating this heavy fraction of solvolysis oil by catalytic cracking improves the performance of this unit and increases the yield of atmospheric distillates without promoting additional coke formation. This therefore presents considerable interest and value for the refiner due to the biogenic content of the hydrocarbons resulting from the recycling of elastomers.

[0019] The invention relates to a process for producing atmospheric distillates from a solid feed based on spent elastomers, said process comprising at least the following steps:

[0020] a) a solid charge based on used elastomers is sent into a reaction zone in the presence of a liquid solvent comprising aromatic compounds to dissolve at least part of said solid charge and thermally decompose said at least partially dissolved solid charge at a temperature below 400°C and at a pressure below 2 MPa in order to obtain a first gaseous effluent and a first liquid effluent comprising carbon black, the mass ratio between the liquid solvent and the solid charge being greater than 3 weight / weight;

[0021] b) the first liquid effluent obtained in step a) is sent to a separation zone in order to obtain a carbon black cake and a second liquid effluent;

[0022] c) at least part of said first gaseous effluent obtained at the end of step a) and at least part of the second liquid effluent obtained at the end of step b) are sent to a fractionation zone to obtain at least one light hydrocarbon cut having a final boiling point below 260°C and at least one intermediate hydrocarbon cut comprising an aromatic compound content exceeding 30% by weight relative to the total weight of said intermediate hydrocarbon cut, and further comprising:

[0023] - a C5-C10 hydrocarbon compound content of less than 20% by weight per ratio to the total weight of the hydrocarbon cutting; and

[0024] - a C40+ hydrocarbon compound content of less than 5% by weight relative to to the total weight of said hydrocarbon cutting;

[0025] - a C40+ hydrocarbon compound content of less than 5% by weight relative to to the total weight of said hydrocarbon cutting;

[0026] and a heavy hydrocarbon cut whose initial boiling point is between 340°C and 440°C;

[0027] d) at least a portion of said light hydrocarbon cut and at least a portion of said intermediate hydrocarbon cut obtained at the end of step c) are sent into the reaction zone as liquid solvent of step a), characterized in that the mass ratio between said intermediate hydrocarbon cut and the liquid solvent is between 0.2 and 0.95 weight / weight;

[0028] e) at least a portion of said heavy hydrocarbon cut obtained in step d) is sent to a catalytic cracking zone in a fluidized bed reactor in the presence of a solid catalyst, at a temperature between 500°C and 700°C, a pressure between 0.1 and 0.6 MPa to obtain a catalytic cracking effluent;

[0029] f) the catalytic cracking effluent obtained at the end of step e) is distilled to obtain an atmospheric distillate composed of at least one gasoline cut and one diesel cut.

[0030] Advantageously, the heavy hydrocarbon cut comprises a mass percentage of polyaromatics less than 20% by weight relative to the total aromatics of said heavy hydrocarbon cut.

[0031] Preferably, the heavy hydrocarbon cut comprises a mass percentage of polyaromatics less than 15% by weight relative to the total aromatics of said heavy hydrocarbon cut.

[0032] Advantageously, the heavy hydrocarbon cut comprises a Conradson Carbon of less than 3.

[0033] Preferably, the heavy hydrocarbon cut comprises a Conradson Carbon of less than 2.

[0034] Advantageously, the heavy hydrocarbon cut comprises a total aromatics content greater than 50% by weight relative to said heavy hydrocarbon cut.

[0035] Advantageously, the heavy hydrocarbon cut comprises a mass percentage of monoaromatics greater than 40% by weight relative to the total aromatics.

[0036] Advantageously, the heavy hydrocarbon cut comprises a mass percentage of monoaromatics greater than 50% by weight in relation to the total aromatics of said heavy hydrocarbon cut.

[0037] Advantageously, the heavy hydrocarbon cut comprises a mass percentage of diaromatics greater than 10% by weight relative to the total aromatics of said heavy hydrocarbon cut.

[0038] Advantageously, the heavy hydrocarbon cut represents between 20% and 75% by weight of the total solvolysis oil.

[0039] Advantageously, said heavy hydrocarbon cut obtained in step d) is mixed with a petroleum fossil feedstock of distillate type under vacuum (360°C+) and then sent to the catalytic cracking zone.

[0040] Advantageously, the light hydrocarbon cut comprises a total aromatics content greater than 3% by weight relative to said light hydrocarbon cut, a mass percentage of monoaromatics greater than 60% by weight relative to the total aromatics of the light cut and a mass percentage of polyaromatics less than 10% by weight relative to the total aromatics of said light cut.

[0041] Advantageously, the intermediate hydrocarbon cut comprises a total aromatics content greater than 40% by weight relative to said intermediate hydrocarbon cut, a mass percentage of monoaromatics greater than 50% by weight relative to the total aromatics of said intermediate hydrocarbon cut and a mass percentage of polyaromatics less than 15% by weight relative to the total aromatics of said intermediate hydrocarbon cut.

[0042] Advantageously, the catalytic cracking catalyst implemented in step e) comprises a ZSM-Y zeolite.

[0043] Advantageously, step a) comprises the following substeps:

[0044] a) said solid charge and said liquid solvent are sent into a first stirred reactor (20) to dissolve at least part of said solid charge;

[0045] a2) said solid charge obtained at the end of is sent at least partially dissolved step a1) in a second stirred reactor to thermally decompose said solid feed at a temperature less than or equal to 400°C and obtain a liquid effluent containing suspended carbon black particles. List of figures

[0046] [Fig-1] Fig. 1 is a schematic representation of one embodiment of Production of middle distillates from used elastomers according to the invention. Detailed description of the invention

[0047] 1. Definitions

[0048] By hydrocarbon Cn cut, we mean a cut comprising hydrocarbons with n carbon atoms.

[0049] By Cn+ cut, we mean a cut comprising hydrocarbons with at least n carbon atoms.

[0050] Unless otherwise specified, pressure is defined as absolute pressure and expressed in MPa.

[0051] The term C / O designates the mass ratio between the mass flow rate of catalyst of the catalytic cracking unit and the mass flow rate of the feed being treated.

[0052] The term atmospheric distillate refers to a distillation interval cut between an initial temperature at ambient temperature and a final boiling point between 340°C and 440°C. It comprises a gasoline cut with a distillation interval between ambient temperature and a final boiling point between 220°C and 260°C, and a diesel cut with a distillation interval between an initial temperature between 220°C and 260°C and a final boiling point between 340°C and 440°C.

[0053] Ambient temperature (“Tamb”) is typically understood to be 20°C ± 5°C.

[0054] The term residual cut refers to a distillation interval cut greater than 340°C.

[0055] Liquefied Petroleum Gas or LPG refers to two gases in liquid form: propane and butane. They have the advantage of liquefying under a lower pressure than other gases (notably methane): between 1.5 and 7 bar.

[0056] Conrardson Carbon (CCR): Standardized laboratory test allowing evaluation by combustion of the propensity of a hydrocarbon feedstock to produce coke which is harmful to refining operations (distillation, catalysis) because it forms solid deposits (fouling phenomenon).

[0057] Biogenic or pMC: This refers to the carbon contained in bio-based materials. This carbon is derived from the transformation of carbon dioxide (CO2) by the photosynthesis reaction during plant growth. On land, this CO2 is captured or fixed by plant life (for example, agricultural crops or forest materials). In the oceans, CO2 is captured or fixed by photosynthetic bacteria or phytoplankton. For example, a bio-based material has a 14C / 12C isotopic ratio greater than 0. Conversely, a material of fossil origin has a 14C / 12C isotopic ratio of approximately 0. The terms "renewable" or "derived from renewables" may also be used.To determine whether a material / product / compound is bio-based or derived from renewable resources, its modern carbon (or percent modern carbon, pMC) or biogenic carbon content is measured according to ASTM D 6866-21 (“Determination of Bio-based Content of Natural Range Materials by Radiocarbon and Isotope Ratio Mass Spectrometry Analysis”). The method in this standard measures the 14C / 12C isotope ratio in a sample and compares it to the 14C / 12C isotope ratio of a standard bio-based reference to obtain the percentage of bio-based content of the sample, the reference. resulting in a radiocarbon content approximately equivalent to the atmospheric radiocarbon fraction in 1950. The pMC (or biogenic carbon) of the standard bio-based reference material is therefore 100%. The pMC (or biogenic carbon) of a fossil-based material is approximately 0%. A current bio-based material may therefore also potentially have a pMC greater than 100%.

[0058] The total, monoaromatic, diaromatic, and polyaromatic aromatic content of the solvolysis oil and its various fractions is determined by UV spectroscopy according to the Burdett method (Burdett RA, Taylor LW, and Jones LC, Journal of Molecular Spectroscopy, Rept. Conf., Inst. Petroleum, London 1954, 30-41, 1955). Polyaromatics are defined as aromatics containing three or more aromatic rings.

[0059] .

[0060] 2. Description

[0061] The present invention relates to a process for producing atmospheric distillates from a solid feed based on spent elastomers, said process comprising at least the following steps:

[0062] a) a solid charge (100) based on used elastomers is sent into a reaction zone (80) in the presence of a liquid solvent (760) comprising aromatic compounds to dissolve at least part of said solid charge and thermally decompose said at least partially dissolved solid charge at a temperature below 400°C and at a pressure below 2 MPa in order to obtain a first gaseous effluent (310) and a first liquid effluent (320) comprising carbon black, the mass ratio between the liquid solvent (760) and the solid charge (100) being greater than 3 weight / weight;

[0063] b) the first liquid effluent (320) obtained in step a) is sent into a separation zone (40) in order to obtain a carbon black cake (420) and a second liquid effluent (410);

[0064] c) at least part of said first gaseous effluent (310) obtained at the end of step a) and at least part of the second liquid effluent (410) obtained at the end of step b) are sent to a fractionation zone (70) to obtain at least one light hydrocarbon cut (720) having a final boiling point below 260°C and at least one intermediate hydrocarbon cut (730) comprising an aromatic compound content exceeding 30% by weight relative to the total weight of said intermediate hydrocarbon cut (730), and further comprising:

[0065] - a C5-C10 hydrocarbon compound content of less than 20% by weight per ratio to the total weight of the hydrocarbon cutting; and

[0066] - a C40+ hydrocarbon compound content of less than 5% by weight relative to to the total weight of said hydrocarbon cutting;

[0067] - a C40+ hydrocarbon compound content of less than 5% by weight relative to to the total weight of said hydrocarbon cutting;

[0068] and a heavy hydrocarbon cut (740) whose initial boiling point is between 340°C and 440°C;

[0069] d) at least a portion of said light hydrocarbon cut (720) and at least a portion of said intermediate hydrocarbon cut (730) obtained at the end of step c) are sent into the reaction zone (80) as liquid solvent (760) of step a), characterized in that the mass ratio between said intermediate hydrocarbon cut (730) and the liquid solvent (760) is between 0.2 and 0.95 weight / weight;

[0070] e) at least a portion of said heavy hydrocarbon cut (740) obtained in step d) is sent into a catalytic cracking zone (20) in a fluidized bed reactor in the presence of a solid catalyst, at a temperature between 500°C and 700°C, a pressure between 0.1 and 0.6 MPa to obtain a catalytic cracking effluent (220);

[0071] f) the catalytic cracking effluent (220) obtained at the end of step e) is distilled to obtain an atmospheric distillate composed of a gasoline cut (920) and a diesel cut (930). The charge

[0072] The solid charge (100) used in the context of the present invention is advantageously based on used elastomers which can come from any source, from tires of light vehicles (LV) or heavy goods vehicles (HGV), two wheels or any type of special machinery, vehicle door seals, but also objects such as shoe soles or rubber boots.

[0073] Said solid filler can advantageously be in the form of elastomer granules, i.e. in the form of particles of sizes less than 25mm containing more than 80% elastomers and reinforcing filler (carbon black, silica, ...), from the treatment of end-of-life waste and containing large quantities of elastomers.

[0074] Thus, according to a preferred embodiment of the invention, the solid feed (100) is sent to a pretreatment unit (10) in order to remove textile fibers and metal wires (110) from the solid feed (100). Such a pretreatment unit is well known to those skilled in the art and can consist of crushers of different types (i.e., a rotary shear, a shredder, a granulator, a refiner), a magnetic separator, or even a vibrating screen or a separation table. Step a)

[0075] According to step a) of the conversion process, the gum contained in the solid filler (100) is sent to a reaction zone (80) to be dissolved upon contact with the liquid solvent (760) and then thermally decomposed. The origin and composition of the liquid solvent (760) will be described in detail below. Step a) is preferably carried out at a temperature below 400°C, preferably between 365°C and 395°C, and even more preferably between 380°C and 395°C, and at a pressure below 1.5 MPa absolute, preferably between 0.2 MPa and 1.2 MPa absolute.At the end of step a), at least one gaseous effluent (310) and a first liquid effluent (320) are obtained, comprising carbon black and possibly solid material residues (210) contained in used elastomers, particularly in used tires, such as metal wires or textile fibers, which are released and separated from the liquid effluent (320) obtained at the end of this step. The mass ratio between the liquid solvent (760) and the solid feed (100) is greater than or equal to 3 weights / weights, preferably between 3 weights / weights and 10 weights / weights, more preferably between 4 weights / weights and 7 weights / weights.

[0076] Advantageously, the residence time in the reaction zone (80) is between 0.5 hours and 4 hours.

[0077] According to one or more embodiments, step a) comprises the following substeps:

[0078] a) said solid charge and said liquid solvent are sent into a first stirred reactor to dissolve at least part of said solid charge; with a residence time between 30 minutes and 2 hours, at a temperature less than or equal to 300°C;

[0079] a2) the liquid effluent obtained at the end of step a1) is sent to a second agitated reactor to thermally decompose at a temperature less than or equal to 400°C (residence time between 30 minutes and 2 hours) said solid feed and obtain a liquid effluent containing suspended carbon black particles. Step b)

[0080] The first liquid effluent (320) containing the carbon black is then sent to a separation zone (40) to recover a carbon black cake (420) and a second liquid effluent (410). This separation step can be carried out by filtration or centrifugation, preferably by centrifugation. Those skilled in the art can use any type of centrifuge technology, including a plate centrifuge or a decanter centrifuge. Centrifugation can be carried out, for example, at a centrifugal force of between 1000 G and 16000 G for a duration of between 30 seconds and 30 minutes.

[0081] Step b) is advantageously followed by a step b') of conduction drying of the centrifuged carbon black cake (420) obtained at the end of step b), which can, for example, be carried out at a temperature between 150°C and 350°C, a vacuum pressure between 0.0001 MPa and 0.01 MPa absolute, under agitation between 2 rpm and 150 rpm for a period between 1 hour and 8 hours to obtain the recovered dry carbon black.

[0082] The second liquid effluent (410) preferably consists of more than 40% by weight of the first liquid effluent (320), more preferably more than 60% by weight of the first liquid effluent (320). It may advantageously incorporate the hydrocarbon effluents resulting from the drying of carbon black. Step c)

[0083] At least part of said first gaseous effluent (310) obtained at the end of step a) and at least part of the second liquid effluent (410) obtained at the end of step b) are sent to a fractionation zone (70) to obtain at least one light hydrocarbon cut (720) having a final boiling point below 260°C and at least one intermediate hydrocarbon cut (730) comprising an aromatic compound content exceeding 30% by weight relative to the total weight of said intermediate hydrocarbon cut (730), and further comprising:

[0084] - a C5-C10 hydrocarbon compound content of less than 20% by weight per ratio to the total weight of the hydrocarbon cutting; and

[0085] - a C40+ hydrocarbon compound content of less than 5% by weight relative to to the total weight of said hydrocarbon cutting;

[0086] and a heavy cup (740), whose initial boiling temperature is preferably between 340°C and 440°C.

[0087] Advantageously, the light cut (720) comprises at least a content of hydrocarbon compounds in CIO- greater than 60% by weight relative to the total weight of the light cut (720).

[0088] Advantageously, the light cut (720) has a final boiling point below 240°C, preferably below 220°C.

[0089] Advantageously, the light cut (720) comprises a total aromatics content greater than 3% by weight, preferably greater than 5% by weight, and more preferably greater than 10% by weight relative to the total weight of the light hydrocarbon cut (720).

[0090] Advantageously, the light cut (720) comprises a mass percentage of monoaromatics greater than 60% by weight, preferably greater than 70% by weight, and more preferably greater than 80% by weight relative to the total aromatics of the light cut (720).

[0091] Advantageously, the light cut (720) comprises a mass percentage of diaromatics greater than 5% by weight, preferably greater than 10% by weight relative to the total aromatics of the light cut (720).

[0092] Advantageously, the light cut (720) comprises a mass percentage of polyaromatics less than 10% by weight, preferably less than 5% by weight, and more preferably less than 1% relative to the total aromatics of the light cut (720).

[0093] Advantageously, the fractionation zone (70) also allows the obtaining of non-condensable gases (710).

[0094] Advantageously, the intermediate hydrocarbon cut (730) also comprises a content of C10-C20 hydrocarbon compounds of between 20% by weight and 65% by weight relative to the total weight of the hydrocarbon cut, preferably between 30% by weight and 65% by weight, and even more preferably between 45% by weight and 65% by weight.

[0095] Advantageously, the intermediate hydrocarbon cut (730) also comprises a content of C20-C40 hydrocarbon compounds of between 30% by weight and 80% by weight relative to the total weight of the hydrocarbon cut, preferably between 30% by weight and 70% by weight, and even more preferably between 30% and 55% by weight.

[0096] Advantageously, the intermediate hydrocarbon cut (730) has an initial boiling temperature between 200°C and 260°C, and a final boiling temperature between 350°C and 520°C, preferably between 340°C and 440°C.

[0097] Advantageously, the intermediate hydrocarbon cut (730) comprises a total aromatics content greater than 40% by weight compared to the intermediate hydrocarbon cut (730), preferably greater than 50% compared to the intermediate hydrocarbon cut (730).

[0098] Advantageously, the intermediate hydrocarbon cut (730) comprises a mass percentage of monoaromatics greater than 50% by weight, preferably greater than 60% by weight, and more preferably greater than 70% by weight relative to the total aromatics of the intermediate hydrocarbon cut (730).

[0099] Advantageously, the intermediate hydrocarbon cut (730) comprises a mass percentage of diaromatics greater than 5% by weight, preferably greater than 10% by weight relative to the total aromatics of the intermediate hydrocarbon cut (730).

[0100] Advantageously, the intermediate hydrocarbon cut (730) comprises a mass percentage of polyaromatics of less than 15% by weight, preferably less than 10% by weight, and more preferably less than 5% relative to the total aromatics of the intermediate hydrocarbon cut (730).

[0101] Advantageously, the heavy cut (740) comprises a content of C40+ hydrocarbon compounds greater than 60% by weight relative to the total weight of the heavy cut (740).

[0102] The heavy hydrocarbon cut (740) represents between 20% and 75% by weight, preferably between 30% and 50% by weight, of the total solvolysis oil. Said total solvolysis oil being composed of the light cut (720), the intermediate hydrocarbon cut (730), and the heavy cut (740).

[0103] The heavy hydrocarbon cut (740) comprises a total aromatics content greater than 50% by weight, preferably greater than 60% by weight, and more preferably greater than 70% by weight compared to the heavy hydrocarbon cut (740).

[0104] The heavy hydrocarbon cut (740) comprises a mass percentage of monoaromatics greater than 40% by weight, preferably greater than 50% by weight, and more preferably greater than 60% by weight relative to the total aromatics of the heavy hydrocarbon cut (740).

[0105] The heavy hydrocarbon cut (740) comprises a mass percentage of diaromatics greater than 10% by weight, preferably greater than 20% by weight relative to the total aromatics of the heavy hydrocarbon cut (740).

[0106] The heavy hydrocarbon cut (740) comprises a mass percentage of polyaromatics of less than 20% by weight, preferably less than 15% by weight, and more preferably less than 10% relative to the total aromatics of the heavy hydrocarbon cut (740).

[0107] The heavy hydrocarbon cut (740) comprises a Conradson Carbon of less than 3, preferably less than 2, more preferably less than 1.

[0108] This specific percentage of monoaromatics compared to total aromatics in the heavy hydrocarbon cut (740) makes it possible to increase the yield in atmospheric distillates without promoting the additional formation of coke in the catalytic cracking unit of step e). Step d)

[0109] According to the invention, at least part of a fraction of the light hydrocarbon cut (720) and at least part of the fraction of the intermediate hydrocarbon cut (730) are sent to the reaction zone (80) of step a) as a liquid solvent (760), the other parts (750) and (770) being advantageously sent out of the process according to the invention as a valuable product. The mass ratio between the liquid solvent (760) and the flow rate of the solid feed (100) injected into the reaction zone (80) is greater than or equal to 3 wt / wt, preferably between 3 wt / wt and 10 wt / wt, more preferably between 4 wt / wt and 7 wt / wt. Indeed, one of the characteristics of the liquid solvent (760) is that it contains an aromatics content exceeding 30% by weight relative to the total weight of said liquid solvent (760), allowing it to effectively dissolve the solid charge (100) and to effectively reduce The viscosity of the reaction medium in the reaction zone (80). Another advantage of the process according to the invention is that the use of such a solvent allows it to remain in liquid form while limiting the pressure in the reactors to a level below 2 MPa. The fine optimization of the liquid solvent composition (760), the liquid solvent (760) to solid feed ratio (100), and the reactor pressure also makes it possible to target a carbon black concentration in the reactor outlet effluent, enabling proper management of this flow and the conditions suitable for carbon black separation.

[0110] During the start-up of the installation, in the absence of production of a stabilized intermediate cut, i.e., the intermediate hydrocarbon cut (730), it is possible to temporarily use an imported solvent which will preferably consist of an aromatic molecule content exceeding 40% by weight relative to the total weight of the cut. This cut could therefore consist, for example, of conversion effluents from the FCC (Fluid Catalytic Cracking) process, diesel fuel, or heavy diesel fuel, for example. Step e)

[0111] At least a portion of said heavy hydrocarbon fraction (740) obtained in step d) is sent to a catalytic cracking zone (20) comprising at least one fluidized bed reactor (FCC) in the presence of a solid catalyst, at a temperature between 500°C and 700°C, preferably below 650°C, and a pressure between 0.1 and 0.6 MPa. The gas surface velocity is advantageously between 3 and 30 m / s. The contact time is advantageously less than 2 seconds. The C / O ratio is advantageously between 3 and 50.

[0112] In a preferred embodiment of the invention, said heavy hydrocarbon cut (740) obtained in step d) is mixed with a petroleum fossil feedstock of residue type (360°C+) in the catalytic cracking zone (20).

[0113] The addition of said heavy hydrocarbon cut (740) from solvolysis which has a Carbon Conradson lower than a residue type feed (360°C+) (generally CCR between 3 and 6) makes it possible to lower the coke yield of the units compared with a catalytic cracking unit operating with 100% of a petroleum fossil residue type feed (360°C+) thus making it possible to increase the catalyst circulation and by a synergistic effect a better atmospheric distillate yield (gasoline and diesel).

[0114] Indeed, in the catalytic cracking process, the coke formed on the catalyst is burned in the regeneration section, which leads to a temperature rise in the catalyst. The latter returns to the reaction zone at a higher temperature. A high temperature allows for the necessary heat to be supplied for feed conversion. Thus, the more coke formed, the hotter the catalyst will return. Since the reaction zone temperature is fixed to limit the formation of cracked gases (C1 / C2), it is more advantageous to have a catalyst regenerated at a lower temperature because reaching the target temperature will require a higher catalyst flow rate. In catalytic reactions, it is understood that the higher the catalyst-to-feed ratio (C / O), the more selectively the system can convert the treated feed.

[0115] The present invention is compatible with all catalytic cracking reactor technologies, whether it be an upward solid gas flow technology (called "riser" in Anglo-Saxon terminology), or a downward flow technology (called "dropper" or "downer" in Anglo-Saxon terminology).

[0116] The catalytic cracking unit implemented in the present process can be configured in several ways; with a single reactor or several reactors, each reactor being able to operate in upward or downward flow. Most often, both reactors will have the same flow mode.

[0117] The catalyst is a solid catalyst. The size and shape of the catalyst are known to those skilled in the art and will not be further described. According to one or more embodiments, the catalyst contains a matrix made of clay, alumina, silica, or silica-alumina, a binder, and zeolite, for example, 15% to 50% by weight of zeolite relative to the weight of the catalyst, preferably a Y zeolite and / or a ZSM-5 zeolite. According to one or more embodiments, the catalyst comprises a ZSM-5 zeolite. According to one or more embodiments, the grain density of the catalyst is between 1000 kg / m³ and 2000 kg / m³. According to one or more embodiments, the grain density of the catalyst is between 1250 kg / m³ and 1750 kg / m³. The catalyst of the FCC reactor consists of particles with an average diameter generally between 40 and 140 micrometers (1 micron = 10⁻⁶ meters), and preferably between 50 and 120 micrometers.

[0118] The spent catalyst stream from the FCC reactor is separated from the cracking effluents by any gas-solid separation system known to those skilled in the art and regenerated in a regeneration zone.

[0119] Passing said heavy hydrocarbon fraction (740) through the catalytic cracking zone (20) under the conditions described above yields a catalytic cracking effluent (220) with boiling points lower than that of the feedstock. The conversion on said solid catalyst of heavy products (with boiling points greater than or equal to 340°C) into light products (with boiling points less than 340°C) being greater than or equal to 40% by weight, preferably greater than 75%. Step f) Distillation of the cracking effluent

[0120] The effluent from the catalytic cracking reactor (220) is sent to a fractionation zone (90) to produce several cuts, including a diesel cut (930) with a distillation range advantageously between 220°C and 360°C. A gasoline cut (920) with a distillation range advantageously between 70°C and 220°C, light gases (910), and advantageously a heavy cut (940) with a boiling point above 360°C are also generally recovered.

[0121] This type of fractionation unit is well known to those skilled in the art. Examples

[0122] Example 1: (according to the invention) Production of a solvolysis oil from spent elastomers

[0123] The method used to illustrate the invention conforms to that described in [Fig. 1].

[0124] In this example, the solvolysis oil of spent elastomers is produced according to the steps a) to d) of the invention. The waste elastomer charge consists of 100% waste tires.

[0125] Used tire granules (solid feed (100)), produced by granulators using crushers, are used. These granules come from heavy-duty tires, and the resulting granules have a size of approximately 4 millimeters. The tire granules (100) are obtained from a pretreatment unit (10) and are free of textile and metallic fibers. The granules (100) are then continuously fed into a dissolution reactor (step a1a) where they are mixed with the liquid solvent from the intermediate hydrocarbon fraction (730) recycled from the fractionation zone (70). The mixture is then sent to the conversion reactor (80) (step a2). A portion of the hydrocarbon fractions (720) and (730), the yields of which are shown in Table 1 below, serves as the liquid solvent (760) below. The mass ratio of solvent (760) / granule (100) is equal to 5 wt / wt.In reactor (80), the temperature is maintained at 280°C for dissolution (step a1), which allows the aggregates (100) to dissolve, and at 400°C for conversion (step a2). The residence time in reactor (80) is 1 hour. The pressure of the dissolution reactor is 0.9 MPa. At the outlet of reactor (30), a first liquid effluent (320) and a gaseous effluent (310) are recovered. The latter is sent entirely to the fractionation zone (70), which allows the recovery of, in particular, the light hydrocarbon fraction (720), the intermediate hydrocarbon fraction (730), and the heavy fraction of the solvolysis oil (740), the composition of which is given in Table 3 of Example 4.

[0126] Table 1 presents the yield structure obtained by solvolysis under the conditions of Example 1. For comparison, the solvolysis process leads to less gas, 2% (of little value) and much more total oil fraction of interest 63% by weight than a pyrolysis process for which the liquid oil fraction is about 40% by weight (cf. MF Laresgoiti, BM Caballero, I. de Marco, A. Torres, MA Cabrero, MJ Chomôn, Characterization of the liquid products obtained in tire pyrolysis, J. Anal. Appl. Pyrolysis 71, 917-934, 2004).

[0127] [Tables] Example 1 (according to the invention) Gas % wt 2(310) rCB (carbon black) % wt 35(420) Total solvolysis oil % wt 63 (720)+(730)+(740) Composition of the total solvolysis oil PI-220°C % wt 15.9 (720) 220°C-340°C % wt 31.8 (730) 340°C+ % wt 52.3 (740)

[0128] Table 2 shows the aromatic composition of the heavy cut (740), the light cut (720) and the intermediate cut (730). The Conradson carbon is also given for the heavy cut (740).

[0129] [Tables2] Heavy cut of tire solvolysis oil 340°C+ (7 40) Light cut of tire solvolysis oil PI-220°C (720) Intermediate cut of tire solvolysis oil 220-340°C (730) Composition by weight of aromatics (% wt) (UV spectroscopy) Monoaromatics 53 13 40 Diaromatics 14 2 11 Polyaromatics 7 0 2 Total Aromatics 74 15 53 Conradson carbon (% wt) 0.84 Monoaromatics / Total Aromatics % 71.6 86.6 75.5 Diaromatics / Total Aromatics % 18 13.3 20.7 Polyaromatics / Total Aromatics % 9.4 0 3.8 Biogenic 50%

[0130] The heavy hydrocarbon cut (740) comprises a total aromatics content of 74% relative to the heavy hydrocarbon cut (740). The heavy hydrocarbon cut (740) comprises a significant mass percentage of monoaromatics of 71.6% wt. relative to the total aromatics. The heavy hydrocarbon cut (740) comprises a mass percentage of diaromatics of 18.9% wt. relative to the total aromatics and a mass percentage of polyaromatics of only 9.4% wt. relative to the total aromatics.

[0131] The heavy hydrocarbon cut (740) includes a Conradson Carbon of 0.84.

[0132] The low polyaromatic content is a strong marker of the quality of the oil resulting from the conversion of tires by the Solvolysis route compared to pyrolysis oil (see the article E. Rodriguez et al., Production of Non-Conventional Fuels by Catalytic Cracking of Scrap Tires Pyrolysis Oil Ind. Eng. Chem. Res. 2019, 58, 5158-5167 and the article MF Laresgoiti, BM Caballero, I. de Marco, A. Torres, MA Cabrero, MJ Chomôn, Characterization of the liquid products obtained in tyre pyrolysis, J. Anal. Appl. Pyrolysis 71, 917-934, 2004).

[0133] This is explained by the use of an internal solvent in the solvolysis process, which allows the material to be converted at a lower temperature (400°C) compared to 600-700°C for pyrolysis, thus promoting oil selectivity and minimizing gas production. The quality of the oil produced is therefore improved, with a lower total aromatic content, particularly polyaromatics, resulting in a lower CCR (here less than 1). The valorization as FCC is thus significantly enhanced, since this process converts the material without the addition of hydrogen, which results in coke production. The quantity of coke in FCC will therefore be significantly lower in the case of products from solvolysis, thus allowing for better selectivity in valuable products, i.e., atmospheric distillate.

[0134] Example 2 (comparative): Supplying a distillate under vacuum

[0135] The vacuum distillate is a heavy petroleum cut (360°C+) conventionally used as a catalytic cracking feedstock; it is of Arabian Light origin. The main characteristics in terms of viscosity, density, CHONS, simulated distillation curve, and aromatic distribution given by UV spectroscopy are given in Table 3.

[0136] [Tables3] DSV Density at 15°C, g / cm³ 0.9211 Kinematic viscosity m² / s 70°C 19.14 100°C 8.17 CHONS (% wt) C 85.8 H 12.3 0 0.4 N 0.1 S 1.535 Simulated distillation ASTMD7169 Initial Boiling Point (0.50%) 10% 373 20% 402 50% 454 80% 508 95% 561 Composition by weight of aromatics (% wt) Monoaromatics 24 Diaromatics 11 Polyaromatics 11 Total Aromatics 46

[0137] Example 3: Fluidized bed catalytic cracking test conditions

[0138] Fluidized bed cracking tests are carried out in a pilot unit using the test of Short Contact Time Resid Test (SCT-RT) which allows the simulation of reactions occurring during the catalytic cracking of hydrocarbons in a fluidized bed and to study the phenomena occurring during the vaporization of the feed in the reactor in contact with the catalyst.

[0139] The FCC feedstock is injected into the reactor bottom for one second at a low temperature of 100°C. After contact with the catalyst, which is heated to 600°C and fluidized with nitrogen, the feedstock vaporizes and is transformed into lighter products. The reaction products are conducted in a condenser cooled to -12°C, where the liquid product is separated from the gaseous mixture (composed of the fluidizing nitrogen and the lighter cracking products). The liquid and gaseous products are then quantified. Samples are taken for analysis. The SCT-RT reactor operates at low pressure (1.2 bar) with a C / O ratio of 6. The Y-based zeolite FCC catalyst has a Sauter diameter of 60 micrometers.

[0140] Example 4: Catalytic cracking of 100% DSV (comparative)

[0141] In Example 4, the feed treated in the SCRT fluidized bed catalytic cracking pilot unit under the conditions of Example 3 is a petroleum fossil feed composed of 100% by mass of vacuum distillate (Example 2) under the conditions of Example 2.

[0142] Example 5: catalytic cracking of a feed composed of 10% mass fraction of solvolysis oil (740) (according to the invention) and 90% DSV.

[0143] In Example 5, the feed treated in the SCRT fluidized bed catalytic cracking pilot unit under the conditions of Example 3 is a feed composed of 90% by mass of vacuum distillate (see Example 2) and 10% by mass of heavy fraction of solvolysis oil (740) (see Example 1) under the conditions of Example 2.

[0144] Example 6: yield structure in catalytic cracking

[0145] The yield results in different cuts and coke of examples 4 and 5 are shown in Table 4.

[0146] [Tables4] 100% DSV (example 4) 90% DSV & 10% heavy oil Solvol yse 340°C+ (example 5) Dry gas (including H2S) % wt 3.0 2.3 LPG % w ds 28.4 27.1 (910) Gasoline % w ds 40.6 42.2 (920) Diesel % w ds 18.0 18.9 (930) Residue % w ds 6.4 6.3 (940) Coke % w ds 3.5 3.2 Total % w ds 100 100

[0147] Replacing 10% by mass of the DSV charge with the 340C°+ cut from tire solvolysis (example 1) allows a very significant gain in products of interest, namely in atmospheric distillate cut (gasoline and diesel), leading, in the end, to the production of gasoline and diesel after dedicated conventional hydrotreatments.

[0148] This cut also makes it possible to significantly reduce the gases produced which have no economic interest.

[0149] These gains are also accompanied by a reduction in the production of undesired coke and heavy cut (residue).

[0150] If we start on a production basis of a catalytic cracking unit of 966 kta (kilotonnes per year), the 340°C+ cut from solvolysis (740) containing about 50% wt of biogenic carbon leads to the production of 24 kta of additional fuel (gasoline and diesel), compared to a DSV feed of which 12 kta of the additional production is from biogenic source.

[0151] Example 7: Heat balance of the catalytic cracking unit

[0152] As described previously, if less coke is produced, the temperature of the regenerated catalyst will be lower (less heat released by coke combustion due to its smaller quantity), and to target the same temperature in the riser, the catalyst flow rate will be increased, leading to a higher C / O ratio. Regarding In a catalytic process, the higher the catalyst-to-C / O feed ratio, the greater the conversion of the feed into the product of interest.

[0153] The results of the heat balance at the regenerator level, calculated with coke with a hydrogen content of 5 wt%, expressed in terms of regeneration temperature, catalyst ratio on C / O charge, and % residue of examples 4 and 5 are shown in Table 5.

[0154] [Tables5] 100% DSV (example 4) 90% DSV & 10% heavy solvolysis oil 340°C+ (example 5) % wt of residue 100 90 Coke yield % wt 7.3 6.7 Regenerator temperature (°C) 740 705 C / O 8.0 9.0 Triser temperature (°C) 530 530 Gain in charge conversion at 340°C- Reference Reference + 4

[0155] Thus, replacing part of the residual charge with the 340°C+ cut from tire solvolysis results in a reduction of the coke yield leading to a decrease in the regeneration temperature of 35°C and an increase in the C / O ratio from 8 to 9.

[0156] For the same riser temperature of 530°C, this increase in C / O translates into an increase in the conversion of the charge to cutting 340°C of 4 points.

[0157] Thus, the introduction of the 340°C+ feedstock from solvolysis into a catalytic cracking process improves the yield of atmospheric distillate (gasoline and diesel) but also, through a more favorable heat balance, improves the conversion of the feedstock to 340°C by 4 percentage points. The catalytic cracking process is indeed a method for recovering value from solvolysis oils as atmospheric distillate.

Claims

1. Demands A process for producing atmospheric distillates from a solid feedstock based on spent elastomers, said process comprising at least the following steps: a) a solid charge (100) based on used elastomers is sent into a reaction zone (80) in the presence of a liquid solvent (760) comprising aromatic compounds to dissolve at least part of said solid charge and thermally decompose said at least partially dissolved solid charge at a temperature below 400°C and at a pressure below 2 MPa in order to obtain a first gaseous effluent (310) and a first liquid effluent (320) comprising carbon black, the mass ratio between the liquid solvent (760) and the solid charge (100) being greater than 3 weight / weight; b) the first liquid effluent (320) obtained in step a) is sent to a separation zone (40) in order to obtain a carbon black cake (420) and a second liquid effluent (410); (c) at least part of said first gaseous effluent (310) obtained at the end of step (a), and at least part of the second liquid effluent (410) obtained at the end of step (b), are sent to a fractionation zone (70) to obtain at least one light hydrocarbon cut (720) having a final boiling point below 260°C and at least one intermediate hydrocarbon cut (730) comprising an aromatic compound content exceeding 30% by weight relative to the total weight of said intermediate hydrocarbon cut (730), and further comprising: - a content of C5-C10 hydrocarbon compounds of less than 20% by weight in relation to the total weight of the hydrocarbon cut; and - a content of C40+ hydrocarbon compounds of less than 5% by weight in relation to the total weight of said hydrocarbon cut; and a heavy hydrocarbon cut (740) whose initial boiling point is between 340°C and 440°C; d) at least a portion of said light hydrocarbon fraction (720) and at least a portion of said intermediate hydrocarbon fraction (730) obtained at the end of step c) are sent into the reaction zone (80) as liquid solvent (760) of step a), characterized in that the mass ratio between said fraction intermediate hydrocarbon (730) and liquid solvent (760) being between 0.2 and 0.95 wt / wt; e) at least a portion of said heavy hydrocarbon cut (740) obtained in step d) is sent to a catalytic cracking zone (20) comprising at least one fluidized bed reactor in the presence of a solid catalyst, at a temperature between 500°C and 700°C, a pressure between 0.1 and 0.6 MPa to obtain a catalytic cracking effluent (220); f) the catalytic cracking effluent (220) obtained at the end of step e) is distilled to obtain an atmospheric distillate composed of at least one gasoline cut (920) and one diesel cut (930).

2. A process according to claim 1, wherein the heavy hydrocarbon cut (740) comprises a mass percentage of polyaromatics less than 20% by weight relative to the total aromatics of said heavy hydrocarbon cut.

3. A process according to claim 1, wherein the heavy hydrocarbon cut (740) comprises a mass percentage of polyaromatics less than 15% by weight relative to the total aromatics of said heavy hydrocarbon cut.

4. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a Conradson Carbon of less than 3.

5. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a Conradson Carbon of less than 2.

6. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a total aromatics content exceeding 50% by weight relative to said heavy hydrocarbon cut.

7. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a mass percentage of monoaromatics exceeding 40% by weight relative to the total aromatics.

8. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a mass percentage of monoaromatics greater than 50% by weight relative to the total aromatics of said heavy hydrocarbon cut.

9. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) comprises a mass percentage of diaromatics greater than 10% by weight relative to the total aromatics of said heavy hydrocarbon cut.

10. A process according to any one of the preceding claims, wherein the heavy hydrocarbon cut (740) represents between 20% and 75% by weight of the total solvolysis oil.

11. Process according to any one of the preceding claims, said heavy hydrocarbon cut (740) is mixed with a petroleum fossil feedstock of distillate type under vacuum (360°C+) and then sent to the catalytic cracking zone (20).

12. A process according to any one of the preceding claims, wherein the light hydrocarbon cut (720) comprises a total aromatics content greater than 3% by weight relative to said light hydrocarbon cut, a mass percentage of monoaromatics greater than 60% by weight relative to the total aromatics of said light cut and a mass percentage of polyaromatics less than 10% by weight relative to the total aromatics of said light cut.

13. A process according to any one of the preceding claims, wherein the intermediate hydrocarbon cut (730) comprises a total aromatics content greater than 40% by weight relative to said intermediate hydrocarbon cut, a mass percentage of monoaromatics greater than 50% by weight relative to the total aromatics of said intermediate hydrocarbon cut and a mass percentage of polyaromatics less than 15% by weight relative to the total aromatics of said intermediate hydrocarbon cut.

14. A method according to any one of the preceding claims, wherein the catalytic cracking catalyst implemented in step e) comprises a ZSM-Y zeolite.

15. A method according to any one of the preceding claims, wherein step a) comprises the following substeps: a) said solid feed (100) and said liquid solvent (760) are sent into a first stirred reactor (20) to dissolve at least part of said solid feed (100); a2) said solid charge obtained at the end of step a1) is sent into a second stirred reactor (30) to thermally decompose said solid charge at a temperature less than or equal to 400°C and obtain a liquid effluent containing suspended carbon black particles.

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