Production of synthetic fuels from carbon monoxide and carbon dioxide

Abstract

The present invention relates to a method for converting a hydrocarbon feedstock, comprising producing a synthesis gas (14), separating CO (16) and CO2 (17) from the synthesis gas, producing methanol (19) and then aromatics (23) from the CO2, alkylating the aromatics with ethanol (36) to produce an alkylation effluent (38), converting the CO in a Fischer-Tropsch reaction unit (7) to produce an FT effluent (29) comprising paraffins, separating and post-treating the FT effluent to produce at least one hydrocarbon cut (34), and mixing the hydrocarbon cut with the alkylation effluent to produce a synthetic fuel. The present invention also relates to a device for converting a hydrocarbon feedstock and a synthetic fuel formulation.

Description

Title of the invention: Production of synthetic fuels from carbon monoxide and carbon dioxide Technical field

[0001] The present invention relates to the production of synthetic fuels, namely gasoline, kerosene, diesel, and / or other hydrocarbon products, such as naphtha, or lubricating bases, of very high quality (essentially free of sulfur, aromatics, nitrogen). More particularly, an object of the present invention is to produce synthetic fuels from carbon monoxide (CO), carbon dioxide (CO2) and hydrogen (H2).

[0002] The fuel bases produced by means of the invention are particularly suitable for use as kerosene for air transport. Indeed, the invention makes it possible to produce a kerosene composition containing both paraffinic compounds and aromatic compounds, the composition of which can be adapted to meet the specifications and other constraints of use for air transport.

[0003] Advantageously, the present invention makes it possible to use biomass as raw material, and thus produce entirely bio-sourced kerosene. Prior art

[0004] Pyrolysis of biomass allows the production of aromatic compounds, carbon monoxide and carbon dioxide. The aromatic compounds produced by pyrolysis can be sent to an aromatic complex to produce benzene and paraxylene as described in patent application FR3112773.

[0005] Pyrolysis of biomass leads to the production of CO and CO2 as by-products, the latter can be used to produce an additional quantity of aromatic compounds. In particular, CO2 can be transformed directly into aromatics as described in patent application FR3114597, said aromatic compounds are then introduced into the aromatic complex to produce an additional quantity of benzene and paraxylene.

[0006] Other patents report the use of CO to alkylate aromatic compounds as described in patent application FR3112966.

[0007] The chemical conversion of CO2 into methanol is a known process. Thus, the publication Renewable Energy 146 (2020) 1192-1203 illustrates the possibility of converting CO2 into methanol. Patent US5631302 describes a process flowsheet for converting CO2 into methanol, where two reactors are implemented: the first reactor operates in an adiabatic regime and the second reactor is multi-tubular cooled with a stream of liquid water which changes state, the catalyst contains 50 to 75% of CuO, 15 to 35% of ZnO and 5 to 20% of Al2O3 by mass. Other processes for the synthesis of methanol from CO2 or a CO+CO2 mixture have been proposed (see for example patents US5827901, US4238403, and US5063250).

[0008] Thus, the technology for synthesizing methanol from CO2 using heterogeneous catalysts has reached a relatively high level of maturity corresponding to demonstration units (a demonstration plant in Iceland already produces 4000 tonnes of methanol annually from CO2).

[0009] Methanol can be converted into aromatic compounds for petrochemicals. Examples of catalysts for the aromatization of methanol are described in Journal of Catalysis, 394 (2021), 416-428, and in Catalysis Today, 233 (2014), 8-13. The articles ACS Catal. 11 (2021), 7780-7819 and Catalysis Today 233 (2014) 8-13 illustrate the possibility of carrying out the aromatization of methanol in a fluid bed reactor with one or two reaction sections, and in the presence of a Zn / ZSM-5-based catalyst. The article Chinese Journal of Chemical Engineering 46 (2022) 134-141 shows that methanol can be converted into aromatic compounds and provides a comparison with the use of naphtha to produce said aromatics.

[0010] The Fischer-Tropsch (FT) synthesis process allows the conversion of synthesis gas (CO+H2) into a mixture of paraffins (alkanes), and / or olefins (alkenes) depending on the catalyst and operating conditions. In the case where paraffins are produced, it is preferable to improve certain properties to make them usable for transport applications.

[0011] Sequences of unit operations have been the subject of patent applications, these sequences of unit operations aim to convert carbon dioxide into a base for fuels, often known as e-fuels according to Anglo-Saxon terminology.

[0012] For example, patent application US2010 / 0280135 A1 may be cited, which describes a renewable Fischer-Tropsch synthesis process for producing hydrocarbons and alcohols from wind energy, residual carbon dioxide and water. The process comprises the following unit operations: electrolysis of water to produce hydrogen and oxygen, a RWGS reactor for the production of synthesis gas, a Fischer-Tropsch synthesis in a high-temperature multi-tubular reactor. Various recycling options are described (e.g. recycle after separation of unconverted carbon dioxide from RWGS, recycle ex-FT carbon dioxide to RWGS, recycle unconverted H2 and CO ex-FT to FT).

[0013] Patent application US2007 / 0142481 A1 describes a process for synthesizing hydrocarbons comprising introducing hydrogen and carbon monoxide into a first Fischer-Tropsch reaction stage allowing the hydrogen and carbon monoxide to partially react catalytically to form hydrocarbons. At least a portion of a tail gas which comprises unreacted hydrogen and carbon monoxide obtained from the first reaction stage is introduced into a second Fischer-Tropsch reaction stage which is a two-phase high-temperature catalytic Fischer-Tropsch reaction stage. The hydrogen and carbon monoxide can at least partially react catalytically in the second reaction stage to form gaseous hydrocarbons. This patent application is characterized by the presence of two Fischer-Tropsch reactors in series, the second treating the unconverted synthesis gas from the first.There is no recycling of carbon dioxide or recycling of water.

[0014] On the other hand, these documents do not provide any information relating to the possibility of integrating a set of unit operations making it possible, from biomass, to recover both the CO and the CO2 resulting from a process of pyrolysis of said biomass into a mixture of paraffins and aromatics so as to produce a fuel particularly suitable for aeronautical use. Summary of the invention

[0015] In the context previously described, a first object of the present description is to overcome the problems of the prior art and to provide a method and a device for producing paraffins and aromatics for aircraft fuel use making it possible to convert (for example all) of the carbon monoxide, i.e., CO, and carbon dioxide, i.e., CO2, into paraffinic and aromatic compounds.

[0016] The invention is based on the arrangement of several units for converting CO2 into aromatic compounds in two stages: in a methanol synthesis reactor and then in a methanol aromatization reactor. The invention is also based on the alkylation with ethanol of the aromatic compounds resulting from the conversion of CO2 so as to improve their characteristics for use as aviation fuel.

[0017] The invention also relates to obtaining and converting a CO+H2 synthesis gas into synthetic hydrocarbons by the Fischer-Tropsch reaction. The characteristics of the effluents from the Fischer-Tropsch synthesis can then be adjusted by a post-treatment process (“upgrading” according to English terminology; known to those skilled in the art) so that they are compatible with use for aviation fuels, and optionally land and / or maritime fuels. The gases produced at the outlet of the Fischer-Tropsch reactor can also be recovered into synthetic methane (e-methane), synthetic natural gas SNG (e-SNG) or LPG (e-LPG).

[0018] According to a first aspect, the aforementioned objects, as well as other advantages, are obtained by a process for converting a hydrocarbon feedstock, comprising the following steps: - treat the hydrocarbon feedstock in a CO and CO2 production unit adapted to produce at least one synthesis gas comprising at least CO and CO2; - treat the synthesis gas in a first separation unit suitable for separating CO and CO2; - treat CO2 in a methanol synthesis reaction unit to produce methanol; - treat methanol in a methanol aromatization unit to produce aromatic compounds; - treating at least in part the aromatic compounds with ethanol in an alkylation reaction unit to produce an alkylation effluent, preferably to specifications for transport applications (e.g. air); - convert CO in a Fischer-Tropsch reaction unit to produce a Fischer-Tropsch (FT) effluent comprising paraffins; - treating at least in part the FT effluent in a second separation unit to produce: a hydrocarbon effluent, water optionally recycled at least in part to the inlet of a water electrolysis unit, and a gaseous effluent optionally recycled at least in part to the inlet of the Fischer-Tropsch reaction unit; - treat the hydrocarbon effluent in a hydrogen reaction unit (hydrotreatment and / or hydrocracking and / or hydroisomerization unit) to produce at least one hydrocarbon cut, preferably to specifications for transport applications (e.g. air); and - mixing at least in part the hydrocarbon cut and the alkylation effluent in a mixing unit to produce a formulation for synthetic fuel (preferably a synthetic fuel) preferably comprising proportions adapted to the specifications for transport applications (e.g. air).

[0019] One of the advantages of the present invention is in particular to be able to recover the entire hydrocarbon feedstock, such as biomass, to produce a fuel particularly suitable for aeronautical use, comprising a mixture of paraffins and aromatics.

[0020] According to one or more embodiments, the method comprises providing a supply of hydrogen in the CO t / or the CO2, downstream of the first separation unit, by means of make-up lines, preferably arranged (directly) upstream of the methanol synthesis reaction unit and upstream of the Fischer-Tropsch reaction unit.

[0021] According to one or more embodiments, the hydrocarbon feedstock is a mixture of hydrocarbon compounds having an elemental oxygen content at least greater than 1% by weight, preferably 3% by weight, very preferably 5% by weight relative to the total weight of said hydrocarbon feedstock 12, preferably the hydrocarbon feedstock 12 comprises or consists of lignocellulosic biomass or one or more constituents of lignocellulosic biomass chosen from the group formed by cellulose, hemicellulose and lignin.

[0022] Advantageously, the hydrogen produced by electrolysis of water can be used for the conversion of carbon dioxide, Fischer-Tropsch synthesis and post-treatment (hydrotreatment and / or hydrocracking and / or hydroisomerization). Thus, the process according to the invention may not require an external supply of hydrogen, for example produced by steam reforming of natural gas. The electrolyzer preferably operates with low-carbon electricity, which contributes to the renewable nature of the fuels and gases produced. In addition, the water used for the production of hydrogen can come at least in part from the recycling of the water produced in the different stages of the process, which has the advantage of limiting the external supply of water.

[0023] According to one or more embodiments, the method comprises treating methanol in a purification unit to separate water and produce purified methanol.

[0024] According to one or more embodiments, the purification unit is adapted to separate a recycle gas comprising unconverted CO2, and recycle the recycle gas to the inlet of the methanol synthesis reaction unit.

[0025] One of the advantages of the present invention is in particular to be able, by means of recycling, to convert all of the CO2.

[0026] According to one or more embodiments, the method comprises treating the aromatic compounds in a third separation unit to separate water and a light gas purge comprising hydrogen and C1-C2 hydrocarbon compounds, and producing an effluent enriched in aromatic compounds (25) sent to the alkylation reaction unit.

[0027] According to one or more embodiments, the third separation unit (6) is suitable for: - separating a recycled effluent comprising at least one of the following compounds: C3-C4 hydrocarbon compounds, C5-C10 non-aromatic hydrocarbon compounds, benzene, toluene; and

[0028] - recycle the effluent from the recycler to the inlet of the aromatization reaction unit (5).

[0029] One of the advantages of the present invention is in particular to be able, by means of recycling, converting non-aromatic hydrocarbon compounds into aromatics. One of the advantages of the present invention is in particular to be able, through recycling, to alkylate benzene and toluene into xylenes.

[0030] According to one or more embodiments, the method comprises treating the alkylation effluent (38) in a fourth separation unit to separate a cut enriched in alkylated aromatic compounds and optionally recycling a cut containing C6-C8 paraffinic compounds to the inlet of the methanol aromatization reaction unit, the cut enriched in alkylated aromatic compounds being mixed at least in part with the hydrocarbon cut (in place of the alkylation effluent).

[0031] According to one or more embodiments, the CO and CO2 production unit comprises at least one unit selected from a pyrolysis unit, an oxycombustion unit, a gasification unit, a steam reforming unit, a partial oxidation unit, an autothermal reforming unit, a combined reforming unit and a dry reforming unit, an ethanol production unit. According to one or more embodiments, the CO and CO2 production unit comprises at least one unit selected from a pyrolysis unit, an oxycombustion unit and a gasification unit. According to one or more embodiments, the CO and CO production unit comprises or consists of a pyrolysis unit.

[0032] According to one or more embodiments, the CO and CO2 production unit comprises or consists of a pyrolysis unit adapted to produce at least one pyrolysis effluent comprising hydrocarbon compounds of 6 to 10 carbon atoms and to send the pyrolysis effluent to the alkylation reaction unit.

[0033] According to one or more embodiments, the CO and CO2 production unit comprises a pyrolysis unit comprising at least one reactor used in at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 0.5 MPa and WH between 0.01 h 1 and 10 h *, preferably between 0.01 h 1 and 5 h *, and very preferably between 0.1 h 1 and 3 h1, the WH is the ratio of the volume flow rate of charge to the volume of catalyst used; - temperature between 400°C and 1000°C, preferably between 400°C and 650°C, preferably between 450°C and 600°C and preferably between 450°C and 590°C; - zeolite catalyst comprising and preferably consisting of at least one zeolite chosen from ZSM-5, ferrierite, Beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-11 and preferably the catalyst is a catalyst comprising only ZSM-5.

[0034] According to one or more embodiments, the CO and CO2 production unit comprises an oxycombustion unit comprising at least one reactor used in at least one of the following operating conditions: - a reactor operating in a fluidized bed; - temperature between 500°C and 1000°C; - pressure between 0.1 MPa and 3 MPa, preferably between 0.1 MPa and 1 MPa.

[0035] According to one or more embodiments, the methanol synthesis reaction unit comprises at least one reactor used under at least one of the following operating conditions: - temperature between 200°C and 450°C, preferably between 220°C and 400°C, and even more preferably between 250°C and 350°C; - pressure between 1 MPa and 12 MPa, preferably between 2 MPa and 10 MPa, and more preferably between 5 MPa and 10 MPa; - hydrogen to COX molar ratio in which COX represents CO and CO2, between 3 and 10, preferably between 3 and 7, very preferably between 3 and 5; - space velocity of the gas at the reactor inlet between 0.2 g / gcata / h and 1 g / gcata / h;

[0036] According to one or more embodiments, the aromatization reaction unit comprises at least one reactor used in at least one of the following operating conditions - temperature between 250°C and 500°C, preferably between 300°C and 450°C, and even more preferably between 350°C and 420°C; - pressure between 0.1 MPa and 1 MPa, preferably between 0.2 MPa and 0.8 MPa, and more preferably between 0.4 MPa and 0.5 MPa; - gas space velocity at the reactor inlet between 0.2 g / gcata / h and 1 g / gcata / h.

[0037] According to one or more embodiments, the alkylation reaction unit comprises at least one alkylation reactor used under the following operating conditions: - temperature between 20°C and 400°C; - pressure between 1 and 10 MPa; - benzene / ethanol molar ratio between 3 and 15; - PPH between 0.5 and 50 h1.

[0038] According to one or more embodiments, the alkylation reactor is operated in the presence of a catalyst comprising a zeolite.

[0039] According to one or more embodiments, the Fischer-Tropsh reaction unit comprises at least one reactor used under at least one of the following operating conditions: - temperature between 170°C and 280°C, preferably between 190°C and 260°C and preferably between 210°C and 240°C; - absolute pressure between 1.0 MPa and 6.0 MPa, preferably between 1.5 MPa and 3.5 MPa and preferably between 2.0 MPa and 3.0 MPa; - catalyst comprising cobalt or iron, preferably cobalt, the catalyst optionally comprising a support, for example based on alumina, silica, silica-alumina, alumina-silica or titanium.

[0040] According to one or more embodiments, the hydrogen reaction unit comprises at least one reactor used under at least one of the following operating conditions: - temperature between 250°C and 450°C, more preferably between 280°C and 450°C, and even more preferably between 320°C and 420°C; - pressure between 0.2 MPa and 15 MPa, preferably between 0.5 MPa and 12 MPa, more preferably between 1 MPa and 10 MPa; - space velocity defined as being the ratio of the volume flow rate of the feed at ambient temperature and pressure to the volume of the catalyst, between 0.1 h 1 and 10 h 1, preferably between 0.2 h 1 and 7 h 1, more preferably between 0.5 h 1 and 5 h 1; - hydrogen flow rate between 100 and 2000 normal liters of hydrogen per liter of charge per hour and preferably between 150 and 1500 normal liters of hydrogen per liter of charge and more preferably between 300 and 1500 normal liters of hydrogen per liter of charge.

[0041] According to a second aspect, the aforementioned objects, as well as other advantages, are obtained by a device for converting a hydrocarbon feedstock, comprising: - a CO and CO2 production unit adapted to treat the hydrocarbon feedstock and produce at least one synthesis gas comprising at least CO and CO2; - a first separation unit adapted to treat the synthesis gas and separate CO and CO2; - a methanol synthesis reaction unit adapted to treat CO2 to produce methanol; - a methanol aromatization unit suitable for treating methanol and producing aromatic compounds; - an alkylation reaction unit adapted to treat at least in part the aromatic compounds with ethanol and produce an alkylation effluent, preferably to the specifications for transport applications (e.g. air); - a Fischer-Tropsch reaction unit adapted to convert CO and produce an FT effluent; - a second separation unit adapted to treat at least in part the FT effluent and produce: a hydrocarbon effluent, water optionally recycled at least in part to the inlet of the water electrolysis unit, and a gaseous effluent optionally recycled at least in part to the inlet of the Fischer-Tropsch reaction unit; - a hydrogen reaction unit (hydrotreatment and / or hydrocracking and / or hydroisomerization unit) suitable for treating the hydrocarbon effluent and producing at least one hydrocarbon cut, preferably to specifications for transport applications (e.g. air); and - a mixing unit for mixing at least in part the hydrocarbon cut and the alkylation effluent, and for producing a formulation for synthetic fuel (preferably a synthetic fuel), preferably comprising proportions adapted to the specifications for transport applications (e.g. air).

[0042] According to a third aspect, the aforementioned objects, as well as other advantages, are obtained by a formulation for synthetic fuel, preferably for air transport, produced mainly (> 50% vol.) or essentially (> 90% vol., preferably > 95% vol., very preferably > 99% vol.) from a bio-sourced hydrocarbon source, preferably from biomass, the formulation comprising: between 3% and 70% volume, preferably between 10% and 50% volume, preferably between 15% and 30% volume of alkylbenzenes and between 30% and 97% volume, preferably between 50% and 90% volume, preferably between 70% and 85% volume of paraffins. According to one or more embodiments, the formulation for synthetic fuel is produced by the method according to the first aspect and / or in a unit according to the second aspect.

[0043] According to a fourth aspect, the aforementioned objects, as well as other advantages, are obtained by a synthetic fuel comprising the formulation for synthetic fuel according to the third aspect, and / or being produced in a device according to the second aspect, and / or being produced by the method according to the first aspect, the synthetic fuel preferably comprising proportions (for example in formulation for synthetic fuel) adapted to the specifications for transport applications, preferably for air transport. Preferably, the synthetic fuel comprises mainly (> 50% vol.) or even essentially (> 90% vol., preferably > 95% vol., very preferably > 99% vol.) of the formulation for synthetic fuel. Advantageously, the synthetic fuel is produced mainly or essentially from a bio-sourced hydrocarbon source.

[0044] Embodiments as well as other characteristics and advantages of the inventions according to the aforementioned aspects will appear on reading the description which follows, given solely for illustrative and non-limiting purposes, and with reference to the following drawing. List of figures

[0045] [Fig.l] represents a schematic view of a method and device according to the present invention for producing a mixture of paraffins and aromatic compounds suitable for use as aviation fuel. Description of the embodiments

[0046] Embodiments of the device will now be described in detail. In the following detailed description, numerous specific details are set forth in order to provide a more thorough understanding of the device. However, it will be apparent to those skilled in the art that the device may be implemented without these specific details. In other instances, well-known features have not been described in detail to avoid unnecessarily complicating the description.

[0047] In the present application, the term "comprise" is synonymous with (means the same as) "include" and "contain", and is inclusive or open and does not exclude other elements not recited. It is understood that the term "comprise" includes the exclusive and closed term "consist". Furthermore, in the present description, an effluent comprising essentially, approximately, or only compounds A corresponds to an effluent comprising at least 80% or 90% by weight, preferably at least 95% by weight, very preferably at least 99% by weight, of compounds A. By default, the pressure values ​​are absolute pressures.

[0048] The present invention can be defined as a device and a method comprising a sequence of unit operations making it possible to produce a mixture of paraffins and aromatic compounds suitable for use as fuel and in particular as aviation fuel.

[0049] One of the features of the present invention can be summarized in the use of carbon monoxide (CO) and carbon dioxide (CO2), products of a unit for producing CO and CO2 from hydrocarbon feedstock, to produce a synthetic fuel comprising paraffins and aromatic compounds, preferably suitable for use as aviation fuel.

[0050] Specifically, the combination of a CO2 to methanol conversion unit, a methanol aromatization unit, a CO to paraffin conversion unit by Fischer-Tropsh synthesis and an aromatics alkylation unit with ethanol, makes it possible to produce a mixture which can be advantageously used as a synthetic fuel, in particular for aviation and which can be entirely bio-sourced. For example, the present invention makes it possible to potentially recover all of the CO and CO2 produced from a bio-sourced hydrocarbon feedstock, for example by the pyrolysis of biomass.

[0051] Unlike eFuels for aviation produced solely by Fischer-Tropsh synthesis, the present invention makes it possible to produce a mixture of paraffins and aromatic compounds that is much better suited for use as aviation fuel, in particular due to the presence of alkylated aromatics.

[0052] With reference to [Fig. 1], according to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises: - a CO and CO2 production unit 1, such as for example a pyrolysis unit, adapted to treat a hydrocarbon feedstock 12 and produce at least one synthesis gas 14, i.e. a gas comprising at least CO and CO2 and preferably comprising H2; - a first separation unit 2, downstream of the CO and CO2 production unit 1, adapted to separate the CO and the CO2 and obtain a CO stream 16 and a CO2 stream 17; - a methanol synthesis reaction unit 3 adapted to convert CO2 17, optionally mixed with a hydrogen supplement 18, and produce methanol 19; - a methanol aromatization reaction unit 5 to produce an effluent enriched in aromatic compounds 23; - a Fischer-Tropsch 7 reaction unit adapted to convert CO 16, optionally mixed with a hydrogen supplement 28, and produce an FT effluent 29; - a second separation unit 8 adapted to treat at least in part the FT effluent 29 and produce: a hydrocarbon effluent 32, water 33 and a gaseous effluent 30 optionally recycled at least in part to the inlet of the Fischer-Tropsch reaction unit 7; - a hydrogen reaction unit 9 (hydrotreatment and / or hydrocracking and / or hydroisomerization unit) adapted to treat the hydrocarbon effluent 32 with hydrogen 35 and produce at least one hydrocarbon cut 34, for example to the specifications for transport applications; - an alkylation reaction unit 10 to treat at least in part the aromatic compounds 23 with a source of ethanol 36 and produce an alkylation effluent 38 and water 37; and - a mixing unit 41 adapted to mix at least in part the hydrocarbon cut 34 and the alkylation effluent 38 to produce a formulation for synthetic fuel 42 (or even directly a synthetic fuel) preferably comprising proportions adapted to the specifications for transport applications (e.g. air).

[0053] According to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises a purification unit 4 adapted to treat the methanol 19 to separate from the water 21 and preferably recycle to the inlet of the methanol synthesis reaction unit 3 a recycle gas 20 comprising unconverted CO2. The purification unit 4 makes it possible to obtain purified methanol 22.

[0054] According to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises a third separation unit 6 adapted to treat the effluent enriched in aromatic compounds 23 to separate water 26 and a light gas purge 27 comprising hydrogen and C1-C2 hydrocarbon compounds, and produce an effluent enriched in aromatic compounds 25 sent to the alkylation reaction unit 10. According to one or more embodiments, the third separation unit 6 is adapted to separate and recycle at least in part a recycle effluent 24 at the inlet of the aromatization reaction unit 5, the recycle effluent 24 comprising at least one of the following compounds: C3-C4 hydrocarbon compounds, non-aromatic C5-C10 hydrocarbon compounds, benzene, toluene.

[0055] According to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises a fourth separation unit 11 adapted to treat the alkylation effluent 38 to separate a cut enriched in alkylated aromatic compounds 40 and a cut containing C6-C8 paraffinic compounds 39, and to preferably recycle the cut containing C6-C8 paraffinic compounds 39 to the inlet of the methanol aromatization reaction unit 5.

[0056] According to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises a water electrolysis unit (not shown in the figure) adapted to convert water to produce hydrogen (18, 28, 35) and preferably send a hydrogen supplement to the methanol synthesis reaction unit 3 and / or the Fischer-Tropsch reaction unit 7 and / or the hydrogen reaction unit 9.

[0057] According to one or more embodiments, the method and device for converting aromatic compounds according to the invention uses / comprises a water-gas conversion unit ("Water-Gas Shift" or "WGS" according to English terminology). and / or a reverse water-gas shift (RWGS) unit, which can be arranged (directly) upstream or downstream of the first separation unit 2. Preferably, the WGS or RWGS unit is arranged directly upstream of the first separation unit 2. Advantageously, the WGS or RWGS unit makes it possible to modify the CO and CO2 contents in the synthesis gas 14, the CO 16 or the CO2 17, so that the CO and CO2 molecules can be (fully) recovered as synthetic fuel. The WGS and RWGS reactions are known and make it possible to modify the CO and CO2 contents of a synthesis gas according to the reaction between CO and H2O producing CO2 and H2. CO and CO2 production unit 1

[0058] According to one or more embodiments, the hydrocarbon feedstock 12 comprises at least one compound chosen from a saturated or unsaturated hydrocarbon (e.g. light C1-C4 gases, light C5-C9 liquids, heavy C10+ liquids or solids, asphalts, petroleum coke), coal, an oxygenated compound.

[0059] According to one or more embodiments, the hydrocarbon feedstock 12 is a mixture of hydrocarbon compounds having an elemental oxygen content at least greater than 1% by weight, preferably 3% by weight, very preferably 5% by weight relative to the total weight of said hydrocarbon feedstock 12. According to one or more embodiments, the hydrocarbon feedstock 12 comprises or consists of lignocellulosic biomass or one or more constituents of lignocellulosic biomass chosen from the group formed by cellulose, hemicellulose and lignin.

[0060] Lignocellulosic biomass may consist of wood, agricultural waste or plant waste. Other non-limiting examples of lignocellulosic biomass material are agricultural residues (straw, corn stalk, etc.), forestry residues (first thinning products), forestry products, dedicated crops (short rotation coppices), residues from the agri-food industry, household organic waste, waste from wood processing facilities, used construction wood, paper, recycled or not.

[0061] Lignocellulosic biomass can also come from by-products of the paper industry such as Kraft lignin, or black liquor from the manufacture of paper pulp.

[0062] The lignocellulosic biomass may advantageously undergo at least one pretreatment step before its introduction into the process according to the invention. Preferably, the biomass is ground and dried, until the desired particle size is obtained. A feedstock having a particle diameter of between 0.3 and 0.5 mm can advantageously be obtained. Typically, the particle size of lignocellulosic biomass is a particle size sufficient to pass through a 1 mm sieve up to a particle size sufficient to pass through a 30 mm sieve.

[0063] According to one or more embodiments, when the hydrocarbon feedstock 12 is solid (e.g. biomass type feedstock), the hydrocarbon feedstock 12 is advantageously loaded into a drive compartment or pneumatic transport so as to be driven into a CO and CO2 production reactor by a drive fluid. Preferably, the drive fluid used is nitrogen gas. However, it is also envisaged that other non-oxidizing drive fluids may be used. Preferably, synthesis gas 14 produced during the process may be recycled and used as a drive fluid. Said synthesis gas 14 is mainly composed of a non-condensable gaseous effluent comprising at least carbon monoxide (CO) and carbon dioxide (CO2) and optionally comprising hydrogen and / or light olefins comprising from 2 to 4 carbon atoms.In this way, the costs of carrying out the CO and CO2 production reaction can be considerably reduced. The hydrocarbon feedstock 12 can be loaded into a feed hopper or other device which allows said feedstock to be brought into the drive compartment in an appropriate quantity. In this way, a constant quantity of feedstock is delivered into the drive compartment.

[0064] The drive fluid advantageously transports the hydrocarbon feedstock 12 from the drive compartment into the CO and CO2 production reactor through a feed tube.

[0065] Typically, the feed tube is cooled to maintain the temperature of the hydrocarbon feedstock 12 at a required level prior to its entry into the CO and CO2 production reactor. The feed tube may be cooled by lining the tube, typically with an air-cooled or liquid-cooled jacket. However, it is also contemplated that the feed tube is not cooled.

[0066] According to one or more embodiments, the CO and CO2 production unit 1 comprises at least one unit chosen from a pyrolysis unit, an oxycombustion unit, a gasification unit, a steam reforming unit, a partial oxidation unit, an autothermal reforming unit, a combined reforming unit and a dry reforming unit, an ethanol production unit. According to one or more embodiments, the CO and CO2 production unit 1 is chosen from a pyrolysis unit, an oxycombustion unit and a gasification unit. According to one or more embodiments, the CO and CO2 production unit 1 is a pyrolysis unit.

[0067] The CO and CO2 production unit 1 produces a synthesis gas 14 comprising CO, CO2 and optionally hydrogen, and possibly by-products 15.

[0068] The synthesis gas 14 comprises a mixture containing mainly (eg comprising at least 50% by weight) CO and CO2. According to one or more embodiments, the synthesis gas 14 comprises at least 20% by weight of CO, preferably at least 30% by weight of CO, very preferably at least 40% by weight of CO (eg at least 50% by weight of CO), relative to the total weight of the synthesis gas 14. According to one or more embodiments, the synthesis gas 14 comprises at least 20% by weight of CO2, preferably at least 30% by weight of CO2, very preferably at least 40% by weight of CO2 (eg at least 50% by weight of CO2), relative to the total weight of the synthesis gas 14. According to one or more embodiments, the synthesis gas 14 comprises at least 0.2% by weight of hydrogen, preferably at least 0.5% by weight of hydrogen, very preferably at least 0.8% by weight of hydrogen, relative to the total weight of the synthesis gas 14.According to one or more embodiments, the synthesis gas 14 contains methane and / or ethylene and / or propylene (eg less than 10% by weight) and optionally ethane and / or propane and / or water (eg less than 3% by weight).

[0069] It is understood that the synthesis gas 14 entering the first separation unit 2 may be a mixture of synthesis gases originating from different CO and CO2 production units 1. Thus, the synthesis gas may comprise very varied CO and CO2 contents. Pyrolysis unit

[0070] According to one or more embodiments, the pyrolysis unit comprises at least one pyrolysis reactor (e.g. fluidized bed) adapted to be used in at least one of the operating conditions listed below.

[0071] According to one or more embodiments, the pyrolysis step is catalytic and carried out in the presence of a catalyst. Preferably, said step operates in the presence of a zeolite catalyst comprising and preferably consisting of at least one zeolite chosen from ZSM-5, ferrierite, Beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-11 and preferably the catalyst is a catalyst comprising only ZSM-5. The zeolite used in the catalyst used in the catalytic pyrolysis step can advantageously be doped preferably with a metal chosen from Iron, Gallium, Zinc and Lanthanum.

[0072] According to one or more embodiments, the pyrolysis step is carried out at a temperature between 400°C and 1000°C, preferably between 400°C and 650°C, preferably between 450°C and 600°C and preferably between 450°C and 590°C. When the pyrolysis step is carried out in the presence of catalyst, the use of hot regenerated catalyst from a catalyst regeneration step can ensure reactor temperature ranges.

[0073] The pyrolysis step is also advantageously carried out at an absolute pressure of between 0.1 MPa and 0.5 MPa and optionally at a WH of between 0.01 h 1 and 10 h 1, preferably between 0.01 h 1 and 5 h 1, and very preferably between 0.1 h 1 and 3 h 1. The WH is the ratio of the volume flow rate of feedstock to the volume of catalyst used.

[0074] Under these conditions, the hydrocarbon feedstock 12 undergoes rapid pyrolysis in the reactor by contacting the hot catalyst from the regenerator which in this step plays the role of thermal vector. The gases resulting from this pyrolysis will then react on the catalyst which this time plays its role as a catalyst making it possible to catalyze the reactions producing the desired chemical intermediates.

[0075] In the pyrolysis unit, the hydrocarbon feedstock 12 is in particular converted at least partially into a pyrolysis effluent 13 comprising hydrocarbon compounds whose carbon number ranges from 6 to 10 carbon atoms. The pyrolysis effluent 13 preferably feeds the alkylation reaction unit 10. The pyrolysis unit also produces synthesis gas 14 comprising CO, CO2 and optionally hydrogen, and possibly by-products 15.

[0076] The products obtained at the end of the pyrolysis step are advantageously recovered in the form of an effluent comprising aromatic compounds BTX (i.e., Benzene, Toluene and Xylenes), effluent comprising hydrocarbon compounds whose carbon number ranges from 6 to 10 carbon atoms. According to one or more embodiments, benzene and / or toluene and / or xylenes present in the pyrolysis effluent 13 is separated for petrochemical use.

[0077] The coked catalyst as well as the unconverted hydrocarbon feedstock usually called "char" according to English terminology are advantageously withdrawn from the reactor and preferably sent to a stripper so as to eliminate the potentially adsorbed hydrocarbons and thus avoid their combustion in the regenerator and this by contacting with at least one gas chosen from water vapor, an inert gas such as for example nitrogen, and a part of the gaseous fraction of incondensables resulting from the fractionation of the gaseous effluent resulting from the pyrolysis step.

[0078] Said coked catalyst and the second unconverted hydrocarbon feedstock, optionally stripped, are advantageously sent to a regenerator where coke and char are burned by adding air or oxygen, thus producing regenerated catalyst and a combustion gas rich in CO2.

[0079] According to one or more embodiments, the regenerated catalyst is advantageously recycled into the reactor of the pyrolysis stage in order to undergo another cycle.

[0080] Advantageously, the pyrolysis step of the process according to the invention allows the production of at least 10% by weight and preferably at least 15% by weight of aromatic relative to the total mass of the reaction products obtained, with a selectivity of at least 65% and preferably at least 70% in BTX.

[0081] The pyrolysis step thus produces at least one BTX cut (pyrolysis effluent 13) and a gaseous fraction of incondensables (synthesis gas 14) comprising at least carbon monoxide CO and carbon dioxide CO2.

[0082] According to one or more embodiments, the pyrolysis effluent 13 is a hydrocarbon fraction containing predominantly (i.e., > 50% by weight) molecules whose carbon number ranges from 6 to 10 carbon atoms. The pyrolysis effluent 13 may also contain molecules having more than 10 carbon atoms and / or molecules with 5 carbon atoms. The pyrolysis effluent 13 is rich in aromatics (eg > 50% by weight) and preferably contains at least 20% by weight of benzene, preferably at least 30% by weight, very preferably at least 40% by weight of benzene, relative to the total weight of the pyrolysis effluent 13. According to one or more embodiments, the pyrolysis effluent 13 is treated to meet the required specifications of the alkylation reaction unit 10, for example in order to have contents of sulfur, nitrogen and oxygenated elements compatible with an ethanol alkylation unit.

[0083] The process also makes it possible to obtain a heavier liquid fraction, mainly comprising aromatics with at least 9 carbon atoms, called by-products 15 or “C9+ cut” which can advantageously be used in a process external to the process according to the invention.

[0084] According to one or more embodiments, the by-products 15 comprise a cut containing more or less alkylated di- and tri-aromatics. This cut can be upgraded directly into bunker fuel for example or undergo hydrotreatment and / or hydrocracking to improve its properties and upgrade it into Jet Fuel or diesel. According to one or more embodiments, the by-products 15 comprise a cut of alkylaromatics sent at least in part to the mixing unit 41 to be mixed with the hydrocarbon cut 34 and the alkylation effluent 38 to produce the formulation for synthetic fuel 42. According to one or more embodiments embodiment, the alkylaromatic fraction comprises or consists of alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms), and optionally paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms.

[0085] Preferably, a portion of the gaseous fraction of incondensables is recycled, preferably via a compressor, into the reactor of the pyrolysis step. This gaseous flow then serves as a fluid for driving the charge in said reactor. In this case, a purge of said recycled gaseous effluent is preferably carried out, preferably either upstream or downstream of said compressor. Oxycombustion unit

[0086] According to one or more embodiments, the oxycombustion unit, for example of biomass, comprises at least one reactor used in at least one of the following operating conditions: - a reactor operating in a fluidized bed; - temperature between 500°C and 1000°C; - pressure between 0.1 MPa and 3 MPa, preferably between 0.1 MPa and 1 MPa.

[0087] According to one or more embodiments, the oxycombustion step is carried out in the presence / by injection of a gas source comprising at least 80% by weight of oxygen, preferably at least 90% by weight of oxygen, very preferably at least 95% by weight of oxygen, relative to the total weight of the gas source. According to one or more embodiments, the gas source is a source of pure oxygen, such as a gas comprising at least 99% by weight of oxygen, preferably at least 99.5% by weight of oxygen relative to the total weight of the gas source. The control of the temperature of the hearth can be carried out by adjusting the O2 concentration at the reactor inlet. This adjustment of the O2 concentration can be done via the recycling of combustion fumes. Gasification unit

[0088] According to one or more embodiments, the gasification unit, for example of biomass, comprises at least one gasification furnace used in at least one of the following operating conditions: - temperature between 700°C and 1400°C. Steam reforming unit

[0089] According to one or more embodiments, the steam reforming unit comprises at least one steam reforming reactor used under at least one of the following operating conditions: - temperature between 600°C and 1500°C, preferably between 700°C and 900°C; - absolute pressure between 0.1 MPa and 4 MPa, and preferably between 1 MPa and 3 MPa; - presence of water vapor, for example in excess; - nickel catalyst, for example comprising from 5% to 30% by weight of nickel deposited on a support mainly comprising alumina, or a mixture of alumina and one or more other refractory compounds.

[0090] Steam reforming consists of reacting a hydrocarbon feedstock (e.g. natural gas, naphtha) on a catalyst in the presence of excess water vapor to obtain a synthesis gas rich in CO and H2. The steam reforming reaction is favored by high temperatures and is generally carried out in a furnace. The heat required for the reaction is produced by the combustion with air of a fuel (e.g. natural gas or the hydrocarbon feedstock) in the steam reforming furnace. The synthesis gas obtained by the steam reforming reaction mainly contains hydrogen, carbon monoxide, carbon dioxide, as well as water vapor and unconverted hydrocarbon feedstock. Partial oxidation unit

[0091] According to one or more embodiments, the partial oxidation unit comprises at least one partial oxidation reactor used under at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 9 MPa, and preferably between 1 MPa and 4 MPa; - temperature between 600°C and 2000°C, preferably between 800°C and 1700°C, preferably between 1100°C and 1500°C; and - presence of oxygen used for combustion, with an oxygenation rate between 0.2 and 0.6, preferably between 0.25 and 0.5, in order to promote the formation of carbon monoxide (the oxygenation rate is defined as the ratio of the flow of oxygen consumed to the theoretical flow of oxygen for complete oxidation of all hydrocarbons into CO2 and water); - presence of a catalyst containing nickel.

[0092] Partial oxidation (POX), sometimes called partial oxidation gasification, is a combustion process that promotes the production of CO by controlling oxygen quantities below stoichiometric quantities to form carbon dioxide and steam. Partial oxidation POX can process light and heavy hydrocarbon feedstocks, asphalts, petroleum coke, but also coal and biomass (e.g. wood, green waste, etc.). Partial oxidation POX is preferably carried out in the presence of almost pure oxygen (purity greater than 98% by volume). Autothermal reforming unit

[0093] According to one or more embodiments, the autothermal reforming unit comprises at least one autothermal reforming reactor used under at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 10 MPa, and preferably between 1 MPa and 4 MPa; - temperature between 800°C and 1100°C, preferably between 900°C and 1000°C; and - presence of a nickel catalyst.

[0094] Autothermal reforming (ATR), also called catalytic partial oxidation, consists of partial oxidation immediately followed by catalytic steam reforming in adiabatic regime at high temperature, for example in the outlet temperature range 900°C -1000°C. It consumes less oxygen than POX partial oxidation, but requires a catalytic bed. As with steam reforming, ATR autothermal reforming can only process light feedstocks (gas, naphtha). In the ATR autothermal reforming process, the hydrocarbon feedstock is mixed with steam and then optionally heated in a furnace before being introduced into the autothermal reactor. Oxygen is also introduced into the autothermal reactor. The reactor comprises two successive zones: a first zone corresponding to a combustion chamber and a second zone with a catalytic bed.In the combustion chamber, partial oxidation of the hydrocarbon feedstock takes place with oxygen burners. In the second zone, the synthesis gas produced in the combustion chamber passes through a catalytic bed in which the steam reforming reaction takes place. Combined reforming unit

[0095] According to one or more embodiments, the combined reforming unit comprises at least one combined reforming reactor used under at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 10 MPa, and preferably between 1 MPa and 4 MPa; - temperature between 800°C and 1100°C, preferably between 900°C and 1000°C; and - presence of a nickel catalyst.

[0096] Combined reforming (CR), or two-stage reforming, comprises a first tubular steam reformer (steam reforming furnace) combined in series with a second autothermal reformer (reforming reactor) in which oxygen is added. Dry reforming unit

[0097] According to one or more embodiments, the dry reforming unit comprises at least one dry reforming reactor used under at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 10 MPa, and preferably between 1 MPa and 4 MPa; - temperature between 800°C and 1100°C, preferably between 900°C and 1000°C; and - presence of a nickel catalyst.

[0098] Dry reforming, also called carbon dioxide reforming, corresponds to the reaction between CH4 and CO2 to form 2 CO and 2 H2 (in the case of methane for example). The name carbon dioxide reforming comes from the fact that carbon dioxide replaces the steam in conventional steam reforming. Dry reforming is particularly interesting if you are looking for a synthesis gas with a low H2 to CO molar ratio, around 1. Ethanol production unit.

[0099] According to one or more embodiments, the ethanol production unit comprises at least one fermentation reactor comprising sugars, for example of lignocellulosic origin, in the presence of a yeast for fermenting sugars into ethanol.

[0100] The fermentation ethanol production units produce substantially as much CO2 as ethanol. Thus, the CO2 by-products of the ethanol production units can be recovered into aromatic compounds in a process according to the present invention by feeding either the first separation unit 2 or directly the methanol synthesis reaction unit 3. Gas to water conversion unit

[0101] The WGS reaction unit (not shown in [Fig. 1]) makes it possible to increase the CO2 content, for example of the synthesis gas 14 or of the CO2 17 if the latter contains CO. The water required for the WGS reaction can come from a make-up line and / or from the water (21, 26, 33, 37) recycled from the purification unit 4 and / or from the second separation unit 8, and / or from the third separation unit 6 and / or from the alkylation reaction unit 10.

[0102] According to one or more embodiments, the WGS reaction unit comprises at least one reactor used under at least one of the following operating conditions: - temperature between 250°C and 500°C, preferably between 300°C and 450°C, and even more preferably between 310°C and 450°C; - pressure between 0.1 MPa and 5 MPa, preferably between 0.2 MPa and 4 MPa, and more preferably between 0.5 MPa and 3 MPa; - a molar ratio H2O / CO between 1 and 4, preferably between 1.5 and 2.5, very preferably between 1.8 and 2.2, such as 2 (± 0.1); - the space velocity of the gas at the reactor inlet between 1000 mL / gcata / h and 30000 mL / gcata / h; Inverted gas to water conversion unit

[0103] The RWGS reaction unit (not shown in [Fig.l]) makes it possible to increase the CO content, for example of the synthesis gas 14 or of the CO 16 if the latter contains CO2. The hydrogen required for the RWGS reaction can come from the water electrolysis unit.

[0104] According to one or more embodiments, the RWGS reaction unit comprises at least one reactor used under at least one of the following operating conditions: - temperature between 700°C and 1200°C, preferably between 800°C and 1100°C, and more preferably still between 850°C and 1050°C; - pressure between 0.1 MPa and 10 MPa, preferably between 0.1 MPa and 5 MPa, and more preferably between 0.1 MPa and 3.5 MPa; - space velocity of the gas at the reactor inlet between 5000 NL / kgcata / h and 40000 NL / kgcata / h; - catalysts based on the elements Ni, Cu, Fe, Co or precious metals such as Pt, Pd, Ru, Ag and Au. According to one or more embodiments, the catalyst for the RWGS reaction comprises a support, for example based on alumina, silica, silica-alumina, alumina-silica. First Separation Unit 2

[0105] The synthesis gas 14 consists of a mixture containing mainly CO and CO2. From this mixture, the CO2 17 is selectively extracted to obtain a synthesis gas containing mainly CO 16.

[0106] The separation of CO2 can be achieved by an acid gas removal step, carried out for example using solvent absorption systems, or by means of membranes. Current processes for removing these gases from raw synthesis gas generally involve countercurrent absorption with a regenerative solvent, in an absorbent column.

[0107] Preferably, the CO2 concentration of the CO2 stream 17 at the outlet of the first separation unit 2 is greater than 90% by volume, preferably greater than 97% by volume and even more preferably 98% by volume.

[0108] The CO 16 from the first separation unit 2, which may contain hydrogen and traces of CO2, is sent to the Fischer-Tropsch synthesis reaction unit 7. This CO 16 stream can be purified before being converted into a mixture of hydrocarbons in the Fischer Tropsch synthesis reaction unit 7. different purification methods are well known to those skilled in the art; reference may be made, for example, to: Oil & Gas Science and Technology - Rev. IFP Energies nouvelles, Vol. 68 (2013), No. 4. or to Applied Energy 237 (2019) 227-240. Methanol Synthesis Unit 3

[0109] According to one or more embodiments, a hydrogen supply 18 supplied by a make-up line is added to the CO2 flow 17 so that the H2 / (CO2) molar ratio of the CO2 flow 17 at the inlet of the methanol synthesis reaction unit 3 is between 3 and 10, preferably between 3 and 8, preferably between 3 and 7, preferably between 3 and 6, very preferably between 3 and 5. The make-up hydrogen can advantageously come from any process allowing the production of hydrogen, such as for example a steam reforming process or a catalytic reforming process, the electrolysis of water, the dehydrogenation of alkanes, and its hydrogen purity is most often between 75 and 99.9% volume. It is understood that the hydrogen supply 18 can be provided directly in the methanol synthesis reaction unit 3 and then mixed with the CO2 stream 17.

[0110] In the methanol synthesis reaction unit 3, the CO2 stream 17, if necessary enriched with a hydrogen supply 18, is converted at least partially into methanol and water. The methanol synthesis reaction from CO2 is well known to those skilled in the art (see for example: US5631302, US4238403, EP 3 402 773, and Renewable Energy, 146 (2020), 1192-1203).

[0111] According to one or more embodiments, the methanol synthesis reaction unit 3 comprises at least one reactor used under at least one of the following operating conditions: - temperature between 200°C and 450°C, preferably between 220°C and 400°C, and even more preferably between 250°C and 350°C; - pressure between 1 MPa and 12 MPa, preferably between 2 MPa and 10 MPa, and more preferably between 5 MPa and 10 MPa; - H2 / CO2 molar ratio between 3 and 10, preferably between 3 and 7, very preferably between 3 and 5; - gas space velocity at the reactor inlet between 0.2 g / gcata / h and 1 g / gcata / h.

[0112] According to one or more embodiments, the reactor of the methanol synthesis reaction unit 3 is adapted to operate in a fluid bed or fixed bed, preferably in a fixed bed.

[0113] According to one or more embodiments, the methanol synthesis reaction is carried out in the presence of a hydrogenation catalyst. According to one or more embodiments, said catalyst is a catalyst for the hydrogenation of CO2. According to one or more embodiments, the catalyst for the hydrogenation of CO2 comprises copper (eg in oxide form) and optionally at least one promoter chosen from the following elements: Zn, Zr, Si, Al, Ti, Cr, Ga, Ce (eg in oxide form), and optionally a support (eg a refractory oxide such as alumina). According to one or more embodiments, the catalyst for the hydrogenation of CO2 is of the CuO / ZnO / Al2O3 type. According to one or more embodiments, the catalyst for the hydrogenation of CO2 comprises 50-75% by weight of CuO, 15-35% by weight of ZnO and 5-20% of Al2O3, relative to the total weight of the catalyst.

[0114] According to one or more embodiments, the CO2 17 can be purified before being introduced into the methanol synthesis reaction unit 3. The purification of the CO2 aims to remove sulfur compounds, nitrogen compounds, halogens, heavy metals and transition metals. The main technologies for purifying synthesis gases are: adsorption, absorption, catalytic reactions. The different purification methods are well known to those skilled in the art; reference may be made, for example, to: Oil & Gas Science and Technology - Rev. IFP Energies nouvelles, 68 (2013), No. 4; and to Applied Energy, 237 (2019), 227-240. Purification Unit 4

[0115] In the optional purification unit 4, the methanol 19 is treated to separate water 21 and a recycle gas 20 comprising unconverted CO2, and to produce a so-called purified methanol stream 22 (relative to the methanol stream 19). The recycle gas 20 is preferably recycled to the inlet of the methanol synthesis reaction unit 3. The water-methanol separation can be carried out by distillation. According to one or more embodiments, the purified methanol 22 comprises at least 99.1% by weight of methanol. According to one or more embodiments, the water 21 comprises at least 99.99% by weight of water. The water 21, a co-product of the methanol synthesis reaction, is purged and removed from the process or sent to an electrolyzer to produce hydrogen or used upstream of the CO and CO2 production unit 1 for biomass pretreatment operations. Methanol Aromatization Unit 5

[0116] According to the invention, the methanol 19 or the purified methanol 22 is sent to the aromatization reaction unit 5 to treat the methanol and produce aromatic compounds 23. According to one or more embodiments, the aromatization reaction unit 5 comprises at least one reactor used in at least one of the following operating conditions - temperature between 250°C and 500°C, preferably between 300°C and 450°C, and even more preferably between 350°C and 420°C; - pressure between 0.1 MPa and 1 MPa, preferably between 0.2 MPa and 0.8 MPa, and more preferably between 0.4 MPa and 0.5 MPa; - space velocity of the gas at the reactor inlet between 0.2 and 1 g / gcata / h.

[0117] According to one or more embodiments, the reactor of the aromatization reaction unit 5 is adapted to operate in a fluid bed.

[0118] According to one or more embodiments, the aromatization reaction is carried out in the presence of an aromatization catalyst. According to one or more embodiments, said catalyst is a catalyst for the aromatization of methanol. According to one or more embodiments, the catalyst for the aromatization of methanol comprises zinc optionally impregnated on a zeolite (eg ZSM-5), the zeolite being optionally arranged on a support (eg a refractory oxide such as alumina). According to one or more embodiments, the catalyst for the aromatization of methanol is of the Zn-ZSM-5 / Al2O3 type, and preferably comprises between 0.1% by weight and 10% by weight, such as between 1% by weight and 5% by weight of Zn, relative to the total weight of the catalyst. Examples of such catalysts are described in Journal of Catalysis, 394 (2021), 416-428, and in Catalysis Today, 233 (2014), 8-13. Third separation unit 6

[0119] At the outlet of the aromatization reaction unit 5, the aromatic compounds 23 can be sent directly to the alkylation unit 10 or preferably at least one of the following four streams can be separated by means of the third separation unit 6: - an effluent enriched in aromatic compounds 25 (relative to the stream of aromatic compounds 23) which is sent to the alkylation unit 10 with the feedstock 13; - a recycle effluent 24 comprising C3-C4 hydrocarbon compounds and / or non-aromatic C5-C10 hydrocarbon compounds, which can be recycled to the inlet of the aromatization reaction unit 5; - water 26 purged at the outlet of the aromatization reaction unit 5, potentially sent to an electrolyzer to produce hydrogen or used upstream of the CO and CO2 production unit 1 for biomass pretreatment operations; and - an optional purge of light gas 27 including hydrogen and C1-C2.

[0120] According to one or more embodiments, the recycle effluent 24 comprises benzene and / or toluene.

[0121] Advantageously, the combination of a methanol synthesis reaction unit 3, followed by a methanol aromatization unit 5 makes it possible to produce additional aromatics from CO2, products of the CO and CO2 production unit 1. Fischer-Tropsch Reaction Unit 7

[0122] According to the invention, in the reaction unit FT 7, the CO 16 and the hydrogen (either present in the CO 16 flow or added by a make-up line) react to produce an FT 29 effluent comprising unconverted synthesis gas, CO2, gaseous and liquid hydrocarbon products and water.

[0123] According to one or more embodiments, the gas sent into the reaction unit FT 7 comprises carbon monoxide and hydrogen with a molar ratio H2 / CO of between 0.5 and 4, preferably between 1 and 3, more preferably between 1.5 and 2.5. According to one or more embodiments, the quantity of hydrogen upstream (eg at the inlet) of the reaction unit FT 7 is adjusted, by means of a hydrogen supply 28, so that the molar ratio H2 / CO is as defined above.

[0124] The FT 7 reaction unit is implemented in a reaction unit comprising one or more suitable reactors, the technology of which is known to those skilled in the art. This may be, for example, one or more multitubular fixed bed reactors, or one or more slurry bubble column reactors, or one or more microchannel reactors.

[0125] According to one or more embodiments, the FT 7 reaction unit uses one or more bubble column type reactors. Since the synthesis is highly exothermic, this embodiment makes it possible, among other things, to improve the thermal control of the reactor and to create little pressure loss.

[0126] The catalyst used in this Fischer-Tropsch synthesis is generally any catalytic solid known to those skilled in the art for carrying out the Fischer-Tropsch synthesis. According to one or more embodiments, the catalyst used in the Fischer-Tropsch synthesis comprises cobalt or iron, preferably cobalt. The catalyst used is generally a supported catalyst. The support may be, for example, based on alumina, silica, silica-alumina, alumina-silica or titanium.

[0127] According to one or more embodiments, the reaction unit FT 7 comprises at least one reactor used in at least one of the following operating conditions: - temperature between 170°C and 280°C, preferably between 190°C and 260°C and preferentially between 210°C and 240°C, - absolute pressure between 1.0 MPa and 6.0 MPa, preferably between 1.5 MPa and 3.5 MPa and preferably between 2.0 MPa and 3.0 MPa.

[0128] The effluent FT 29 is sent to the second separation unit 8. Second separation unit 8

[0129] In the second separation unit 8, at least a (first) part of the effluent FT 29 is treated to produce: - hydrocarbon effluent 32 (depleted in water compared to effluent FT 29), - the gaseous effluent 30, and - water 33.

[0130] At the outlet of the second separation unit 8, the hydrocarbon effluent 32 is sent to the hydrogen reaction unit 9, and the water 33 is optionally sent to the water electrolysis unit (not shown in [Fig.l]).

[0131] According to one or more embodiments, the hydrocarbon effluent 32 comprises: n-paraffins, olefins and oxygenated compounds resulting from the condensation of gaseous hydrocarbons under the operating conditions of the Fischer-Tropsch reaction.

[0132] According to one or more embodiments, the gaseous effluent 30 comprises unconverted synthesis gas, carbon dioxide and gaseous hydrocarbons such as paraffins from C1 to C4 (predominantly), olefins from C2 to C4, and oxygenated compounds from C1 to C3.

[0133] According to one or more embodiments, the hydrocarbon effluent 32 comprises less than 5% by weight of water, preferably less than 2% by weight of water, very preferably less than 1% by weight of water.

[0134] According to one or more embodiments, at least a portion 31 of the gaseous effluent 30 is sent into the reaction unit FT 7. Hydrogen reaction unit 9

[0135] The hydrocarbon effluent 32 is sent to the hydrogen reaction unit 9 to undergo a hydrotreatment and / or hydrocracking and / or hydroisomerization reaction, in which one or more hydrocarbon cuts 34 (eg obtained by distillation) can be recovered, in particular into synthetic fuel, namely gasoline, kerosene, diesel, in particular kerosene.

[0136] According to one or more embodiments, the hydrocarbon fraction 34 comprises or consists substantially of a fraction having an initial distillation point (IP) of between 150°C and 180°C, and a final distillation point (FP) of between 220°C and 250°C. According to one or more embodiments, the hydrocarbon fraction 34 comprises or consists substantially of paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms. According to one or more embodiments, the hydrocarbon fraction 34 comprises at least 80% by weight, preferably 90% by weight, preferably at least 95% by weight of paraffins comprising between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms (eg between 95% and 99.9% by weight).According to one or more embodiments, the hydrocarbon fraction 34 comprises at least 70% by weight, preferably at least 80% by weight, preferably at least 90% by weight of iso-paraffins comprising between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms (eg between 90% and 99% by weight). According to . one or more embodiments, the hydrocarbon fraction 34 comprises between 0% (or 1%) and 20% by weight, preferably between 2% and 10% by weight of cyclic paraffins comprising between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms.

[0137] According to one or more embodiments, the hydrogen reaction unit 9 comprises at least one reactor used under at least one of the following operating conditions: - temperature between 250°C and 450°C, more preferably between 280°C and 450°C, and even more preferably between 320°C and 420°C; - pressure between 0.2 MPa and 15 MPa, preferably between 0.5 MPa and 12 MPa, more preferably between 1 MPa and 10 MPa; - space velocity defined as being the ratio of the volume flow rate of the feed at ambient temperature and pressure to the volume of the catalyst, between 0.1 h 1 and 10 h 1, preferably between 0.2 h 1 and 7 h 1, more preferably between 0.5 h 1 and 5 h 1; - hydrogen flow rate between 100 and 2000 normal liters of hydrogen per liter of charge per hour and preferably between 150 and 1500 normal liters of hydrogen per liter of charge and more preferably between 300 and 1500 normal liters of hydrogen per liter of charge.

[0138] According to one or more embodiments, the hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises at least one hydrogenating-dehydrogenating metal chosen from the group comprising the metals of group VIB and group VIIIB of the periodic table and at least one solid which is a Bronsted acid, i.e. a solid capable of releasing one or more protons, and optionally a binder.

[0139] According to one or more embodiments, the hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises at least one noble metal from group VIIIB chosen from ruthenium, rhodium, palladium, osmium, iridium and platinum, taken alone or as a mixture, and preferably from platinum and palladium taken alone or as a mixture, and preferably used in their reduced form.

[0140] According to one or more embodiments, the hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises: at least one metal chosen from nickel, molybdenum, tungsten, cobalt, ruthenium, indium, palladium, platinum; at least one support chosen from aluminas, boron oxides, magnesias, zirconias, titanium oxides, clays. According to one or more embodiments, the support is an alumina, silica-alumina, alumina-silica, silica.

[0141] According to one or more embodiments, the hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises at least one base metal from group VIIIB chosen from nickel and cobalt in combination with at least one metal from group VIB chosen from molybdenum and tungsten, used alone or as a mixture, and preferably used in their sulfurized form.

[0142] According to one or more embodiments, in the case where said hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises at least one noble metal from group VIIIB, the noble metal content of said catalyst is between 0.01% and 5% by weight, preferably between 0.05% and 4% by weight and very preferably between 0.10% and 2% by weight, relative to the total weight of the catalyst.

[0143] According to one or more embodiments, in the case where said hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises at least one metal from group VIB in combination with at least one non-noble metal from group VIII chosen from nickel and cobalt, the content of metal from group VIB in said catalyst is comprised in oxide equivalent between 5% and 40% by weight, preferably between 10% and 35% by weight, and the content of metal from group VIIIB in said catalyst is comprised in oxide equivalent between 0.5% and 15% by weight, preferably between 1% and 10% by weight, preferably between 1% and 8% by weight, and very preferably between 1.5% and 6% by weight, relative to the total weight of the catalyst.

[0144] According to one or more embodiments, the hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst comprises or consists of at least one noble metal and a support comprising or consisting of at least one zeolite and at least one binder.

[0145] According to one or more embodiments, the zeolite-based hydrotreatment and / or hydrocracking and / or hydroisomerization catalyst is advantageously of the bifunctional type, that is to say that it has a hydro-dehydrogenating function and a hydro-isomerizing function. Ethanol alkylation reaction unit 10

[0146] The effluents rich in aromatic compounds (23 or 25 and optionally 13) are at least partly introduced into the alkylation reaction unit 10 for reaction with an ethanol source 36 to produce: an alkylation effluent 38 comprising aromatic compounds including ethylbenzenes and polyethylbenzenes; and an aqueous effluent 37 comprising water and optionally unconverted ethanol and / or oligomers formed from ethanol. Advantageously, the aromatic compounds and in particular benzene, toluene and xylenes are at least partly alkylated in the alkylation reaction unit 10 to produce ethylbenzenes and polyethylbenzenes of interest for transport applications, and in particular air transport, such as for example ethylbenzene, methyl- ethylbenzenes, dimethylethylbenzenes, diethylbenzenes, methyldiethylbenzenes, or even trimethylethylbenzenes and / or dimethyldiethylbenzenes and / or triethylbenzenes. The alkylation effluent 8 may also comprise unconverted aromatic compounds such as xylenes, trimethylbenzenes and tetramethylbenzenes.

[0147] According to one or more embodiments, the alkylation effluent 38 comprises or consists of alkylbenzenes comprising between 7 and 14 carbon atoms, preferably between 8 and 12 carbon atoms, preferably between 9 and 11 carbon atoms, such as alkylbenzenes comprising between 9 and 10 carbon atoms.

[0148] According to one or more embodiments, the alkylation effluent 38 comprises at least 15% by weight, preferably at least 20% by weight, preferably at least 25% by weight, preferably at least 30% by weight, of compounds with 9 carbon atoms, e.g. methylethylbenzenes and / or trimethylbenzenes. The proportion of methylethylbenzenes can be defined by determining (e.g. by distillation) the toluene content in the effluents rich in aromatic compounds. The proportion of trimethylbenzenes can be defined by determining (e.g. by distillation) the content of aromatic compounds with 9 carbon atoms in the effluents rich in aromatic compounds.

[0149] According to one or more embodiments, the alkylation effluent 38 comprises at least 30% by weight, preferably at least 40% by weight, preferably at least 50% by weight, preferably at least 60% by weight of compounds with 10 carbon atoms, e.g., diethylbenzenes or dimethylethylbenzene. The proportion of diethylbenzenes can be defined by determining (e.g. by distillation) the benzene content in the effluents rich in aromatic compounds. The proportion of diethylbenzenes can be defined by separating benzene from the effluents rich in aromatic compounds (e.g. by distillation) for petrochemical use. Similarly, the proportion of dimethylethylbenzenes can be defined by determining (e.g. by distillation) the xylenes content in the effluents rich in aromatic compounds.

[0150] According to one or more embodiments, the alkylation effluent 38 comprises at least 10% by weight, preferably at least 15% by weight, preferably at least 20% by weight, preferably at least 25% by weight, of compounds with 11 carbon atoms, e.g. methyl-diethylbenzenes and / or trimethyl-ethylbenzenes.

[0151] According to one or more embodiments, the alkylation effluent 38 comprises less than 10% by weight, preferably at least 5% by weight, preferably at least 2% by weight, preferably at least 1% by weight of naphthalenes. The proportion of naphthalenes can be defined by determining (eg by distillation) the naphthalene content in the effluents rich in aromatic compounds.

[0152] According to one or more embodiments, the alkylation effluent 38 comprises: at least 15% by weight, preferably at least 20% by weight, of compounds with 9 carbon atoms; at least 30% by weight, preferably at least 45% by weight of compounds with 10 carbon atoms; preferably at least 10% by weight, preferably at least 15% by weight of compounds with 11 carbon atoms; and less than 10% by weight, preferably less than 5% by weight of naphthalenes. According to one or more embodiments, the alkylation effluent 8 comprises: at least 25% by weight, preferably at least 30% by weight, of compounds with 9 carbon atoms; at least 50% by weight, preferably at least 60% by weight of compounds with 10 carbon atoms; preferably at least 10% by weight, preferably at least 15% by weight of compounds with 11 carbon atoms; and less than 2% by weight, preferably less than 1% by weight of naphthalenes.

[0153] According to one or more embodiments, the alkylation reaction unit 10 comprises at least one second alkylation reactor adapted to be used under at least one of the following operating conditions: - temperature between 20°C and 400°C, preferably between 150°C and 400°C, and even more preferably between 250°C and 310°C; - pressure between 1 and 10 MPa, preferably between 2 and 7 MPa, and more preferably between 3 and 5 MPa; - benzene / ethanol molar ratio between 5 and 15, and preferably between 5 and 12; - PPH between 0.5 and 50 h1, preferably between 1 and 10 h1, and more preferably between 1 and 3 h*.

[0154] The term PPH corresponds to the weight of hourly hydrocarbon charge injected relative to the weight of catalyst charged.

[0155] According to one or more embodiments, the alkylation reactor is operated in the presence of a catalyst comprising a zeolite. According to one or more embodiments, the zeolite-based catalyst, preferably based on zeolite Y, very preferably based on dealuminated zeolite Y, comprises from 1% to 100% by weight, preferably 20% to 98% by weight, for example 40% to 98% by weight of said zeolite and 0% to 99% by weight, preferably 2% to 80% by weight, and, for example, 2% to 60% by weight of a matrix. According to one or more embodiments, the catalyst comprises a dealuminated zeolite Y with an overall Si / Al atomic ratio greater than 4, preferably between 8 and 70 and preferably not containing extra-network aluminum species.Said dealuminated Y zeolite can be used alone or in a mixture with a binder or a matrix generally chosen from the group formed by clays, aluminas, silica, magnesia, zirconia, titanium oxide, boron oxide and. any combination of at least two of these oxides such as silica-alumina, silica-magnesia. All known methods of agglomeration and shaping are applicable, such as, for example, extrusion, pelletizing or drop coagulation. Zeolites such as dealuminated Y zeolites and their preparation are well known. Reference may be made, for example, to patent US4738940.

[0156] According to one or more embodiments, the alkylation reactor is of the fixed bed type.

[0157] According to one or more embodiments, the ethanol 36 is biosourced. According to one or more embodiments, the ethanol 36 comes from an ethanol production unit. According to one or more embodiments, the ethanol 36 comes from a sugar fermentation process whose water content is between 0.5% by weight and 40% by weight. Fourth Separation Unit 11

[0158] The alkylation effluent 38 leaving the alkylation unit 10 is sent to the fourth optional separation unit 11 to produce a cut enriched in alkylated aromatic compounds 40 and a cut containing C6-C8 paraffinic compounds 39 which can be recycled to the inlet of the methanol aromatization reaction unit 5. Mixing unit 41

[0159] In the mixing unit 41, the alkylation effluent 38 or the cut enriched in alkylated aromatic compounds 40 is mixed with the hydrocarbon cut 34 to produce a formulation for synthetic fuel 42.

[0160] According to one or more embodiments, the formulation for synthetic fuel 42 comprises between 3% and 70% by volume, preferably between 10% and 50% by volume, preferably between 15% and 30% by volume of alkylation effluent 38 (e.g., alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms), and between 30% and 97% by volume, preferably between 50% and 90% by volume, preferably between 70% and 85% by volume of hydrocarbon cut 34 (i.e., paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms).

[0161] According to one or more embodiments, the formulation for synthetic fuel 42 comprises between 3% and 25% volume, preferably between 3% and 20% volume, preferably between 3% and 15% volume of alkylation effluent 38 (eg alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms), and between 75% and 97% volume, preferably between 80% and 97% volume, preferably between 85% and 97% volume of hydrocarbon cut 34 (i.e., paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms). Advantageously, the CO and CO2 production unit (1) may be chosen to produce a majority (at least 50% by weight) of CO, for example at least 70% by weight, preferably at least 80% by weight, very preferably at least 90% by weight. This is also the case when a RWGS reaction unit (not shown in [Fig.l]) is added to treat the synthesis gas stream 14.

[0162] According to one or more embodiments, the formulation for synthetic fuel 42 comprises between 20% and 80% volume, preferably between 30% and 70% volume (eg between 40% and 60% volume) of alkylation effluent 38 (eg alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms), and between 20% and 80% volume, preferably between 30% and 70% volume, preferably between 40% and 60% volume of hydrocarbon cut 34 (ie, paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms). Advantageously, the CO and CO2 production unit (1) can be chosen to produce mainly (at least 50% by weight) CO2 and / or aromatic compounds, for example at least 70% by weight, preferably at least 80% by weight, very preferably at least 90% by weight.This is also the case when a WGS reaction unit (not shown in [Fig.l]) is added to treat the synthesis gas stream 14. .

[0163] According to one or more embodiments, the alkylation effluent 38 of the synthetic fuel formulation 42 comprises or consists of alkylbenzenes comprising between 7 and 14 carbon atoms, preferably between 8 and 12 carbon atoms, preferably between 9 and 11 carbon atoms, such as alkylbenzenes comprising between 9 and 10 carbon atoms.

[0164] Advantageously, the formulation for synthetic fuel 42 can be used for the preparation of a synthetic fuel preferably comprising proportions adapted to the specifications for transport applications (e.g. air). According to one or more embodiments, the synthetic fuel comprises mainly, i.e., more than 50% volume, or even essentially, i.e., more than 90% volume, preferably more than 95% volume, very preferably more than 99% volume, of the formulation for synthetic fuel 42. Advantageously, the synthetic fuel is produced mainly or essentially from a bio-sourced hydrocarbon source.

[0165] According to one or more embodiments, the synthetic fuel is produced at more than 50% volume, preferably at more than 90% volume, very preferably more than 95% volume, very preferably more than 99% volume from a bio-sourced hydrocarbon source. Preferably, the synthetic fuel comprises: between 3% and 70% volume, preferably between 10% and 50% volume, preferably between 15% and 30% volume of alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms; and between 30% and 97% volume, preferably between 50% and 90% volume, preferably between 70% and 85% volume of paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms.Most preferably, the synthetic fuel comprises between 3% and 25% volume, preferably between 3% and 20% volume, preferably between 3% and 15% volume of alkylbenzenes comprising between 7 and 12 carbon atoms, preferably between 8 and 11 carbon atoms, preferably between 9 and 10 carbon atoms, and between 75% and 97% volume, preferably between 80% and 97% volume, preferably between 85% and 97% volume of hydrocarbon fraction 34 of paraffins comprising between 9 and 14 carbon atoms, preferably between 10 and 13 carbon atoms, preferably between 10 and 12 carbon atoms. Water electrolysis unit

[0166] The water electrolysis unit (not shown in [Fig. 1]) treats water from a make-up line and / or water (21, 26, 33, 37) recycled from the purification unit 4 and / or the second separation unit 8, and / or the third separation unit 6 and / or the alkylation reaction unit 10.

[0167] According to one or more embodiments, the water electrolysis unit comprises at least one alkaline type electrolyzer. Other electrolyzer technologies may be used for the water electrolysis unit, such as proton exchange membrane (PEM) electrolysis, solid oxide electrolysis (SOE), or anion exchange membrane (AEM) electrolysis. The operating conditions (temperature, pressure, nature of the electrolyte, electrodes and diaphragm / membrane) are then specific to each technology.

[0168] According to one or more embodiments, the water electrolysis unit comprises at least one reactor used in at least one of the following operating conditions: Alkaline type electrolyzer: - temperature between 60°C and 90°C, - pressure between 0.1 MPa and 20 MPa, preferably between 0.1 MPa and 4 MPa, - electrolyte comprising KOH, - electrodes comprising a metal alloy, - diaphragm comprising asbestos, polytetrafluoroethylene and / or nickel oxide; Proton exchange membrane (PEM) electrolyzer: - temperature between 50°C and 80°C, - pressure between 0.1 MPa and 20 MPa, preferably between 1.8 MPa and 5.5 MPa, - electrolyte comprising a polymer membrane, - electrodes comprising a metal alloy; Solid Oxide Electrolyzer (SOE): - temperature between 800°C and 900°C, - pressure between 0.1 MPa and 2 MPa, preferably between 0.1 MPa and 0.5 MPa, - electrolyte comprising a ceramic membrane (eg perovskite type), - electrodes comprising a metal alloy; Anion exchange membrane (AEM) type electrolyzer: - temperature between 50°C and 70°C, - pressure between 0.1 MPa and 20 MPa, preferably between 0.1 MPa and 3.5 MPa, - electrolyte comprising a polymer membrane, - electrodes comprising a metal alloy.

[0169] According to one or more embodiments, the hydrogen produced by the water electrolysis unit comprises between 99.5% by weight and 99.999% by weight of H2 (after drying).

[0170] The device and the method according to the invention thus make it possible to produce a 100% bio-sourced aviation fuel based on paraffinic and aromatic compounds.

[0171] In the present application, the groups of chemical elements are given by default according to the CAS classification (CRC Handbook of Chemistry and Physics, publisher CRC press, editor-in-chief DR Lide, 81st edition, 2000-2001). For example, group VIIIB according to the CAS classification corresponds to the metals of columns 8, 9 and 10 according to the new IUP AC classification; group VIB according to the CAS classification corresponds to the metals of column 6 according to the new IUPAC classification. Examples

[0172] Example 1

[0173] Table 1 shows the conversion of biomass into bases to make efuels containing both paraffins and aromatic compounds. For this, a process as described in [Fig.l] is used. In this example, the CO and CO2 production unit 1 is a pyrolysis unit.

[0174] [Table 1] Compounds Input of 1 (t / h) Output of 1 (t / h) Biomass 90 t / h 0 Benzene - 2.63 Toluene - 5.64 Xylenes+ethylbenzene - 3.71 CO - 22.25 co2 - 82.99 h2 - 0.338 Compounds Input of 3 (t / h) Output of 5 (t / h) co2 82.99 - h2 9.427 - Xylenes+ethylbenzene - 19.99 A9 aromatics - 4.527 h2o - 67.9 Compounds Input of 10 (t / h) Output of 10 (t / h) Benzene 2.63 0 Toluene 5.64 0 Xylenes+ethylbenzenes 23.7 3.57 A9 aromatics 4.527 11.88 A10 aromatics 0 29.96 Ethanol 14.656 0 h2o - 5.743 Compounds Input of 7 (t / h) Output of 9 (t / h) CO 22.25 - h2 3.337 - C4- Compounds - 5.12 Naphtha - 2.45 Kerosene (paraffinic) - 5.17 h2o - 12.847

[0175] We then obtain a formulation for synthetic fuel 42 which contains: - paraffinic kerosene: 5.17 t / h, - aromatic compounds: a part, for example 5.17 t / h, of the 41.84 t / h of aromatics A9 and A10.

[0176] The CO and CO2 production unit 1 in this example 1 being a pyrolysis unit, a significant production of aromatic compounds is obtained, in particular by the production of 2.63 t / h of benzene, 5.64 t / h of toluene and 3.71 t / h of xylenes and ethylbenzene. It is understood that the production of aromatic compounds can vary, and in particular decrease in favor of the production of paraffinic kerosene, by choosing another type of CO and CO2 production unit 1 producing little or no aromatics.

[0177] Example 2

[0178] Another way of improving the formulation with a view to producing aviation fuel is the possibility of adding a RWGS reaction unit (not shown in [Fig.l]) to the synthesis gas stream 14 which leaves the pyrolysis unit, while keeping all the other units identical, so as to modify the ratios of the CO and CO2 streams to obtain at the outlet of the first separation unit 2: - CO: 65.7 t / h (instead of 22.25 t / h) - CO2: 14.7 t / h (instead of 82.99 t / h)

[0179] We then obtain a formulation for synthetic fuel 42 which contains: - paraffinic kerosene: 15.26 t / h, - aromatic compounds: 16.43 t / h (having separated the benzene from the pyrolysis unit for petrochemical use).

[0180] Advantageously, the proportion between paraffinic kerosene and aromatic compounds can be modified by means of the RWGS reaction unit or a WGS unit, for example to approach or even reach the specifications and other constraints of use of fuels for air transport.

[0181] The examples according to the invention show that it is possible to produce from biomass a fuel formulated with paraffins (kerosene) and aromatic compounds whose aromatic compound composition is characterized by the majority presence of compounds with 9 and 10 carbon atoms per molecule, compounds particularly suitable for aviation fuels.

Claims

Claims

1. A method for converting a hydrocarbon feedstock, comprising the following steps: - treating the hydrocarbon feedstock (12) in a CO and CO2 production unit (1) adapted to produce at least one synthesis gas (14) comprising at least CO and CO2; - treating the synthesis gas (14) a first separation unit (2) adapted to separate CO (16) and CO2 (17); - treating the CO2 (17) in a methanol synthesis reaction unit (3) to produce methanol (19); - treating the methanol (19) in a methanol aromatization unit (5) to produce aromatic compounds (23); - treating at least in part the aromatic compounds (23) with ethanol (36) in an alkylation reaction unit (10) to produce an alkylation effluent (38), preferably to specifications for transport applications;- converting the CO (16) in a Fischer-Tropsch reaction unit (7) to produce an FT effluent (29) comprising paraffins; - treating at least in part the FT effluent (29) in a second separation unit (8) to produce: a hydrocarbon effluent (32), water (33) optionally recycled at least in part to the inlet of a water electrolysis unit, and a gaseous effluent (31) optionally recycled at least in part to the inlet of the Fischer-Tropsch reaction unit (7); - treating the hydrocarbon effluent (32) in a hydrogen reaction unit (9) (hydrotreatment and / or hydrocracking and / or hydroisomerization unit) to produce at least one hydrocarbon cut (34), preferably to specifications for transport applications;and - mixing at least in part the hydrocarbon fraction (34) and the alkylation effluent (38) in a mixing unit (41) to produce a synthetic fuel formulation (42) preferably comprising proportions adapted to the specifications for transport applications.;

2. A method according to claim 1, wherein the hydrocarbon feedstock (12) is a mixture of hydrocarbon compounds having an elemental oxygen content at least greater than at 1% by weight, preferably 3% by weight, very preferably 5% by weight relative to the total weight of said hydrocarbon feedstock 12, preferably the hydrocarbon feedstock 12 comprises or consists of lignocellulosic biomass or one or more constituents of lignocellulosic biomass chosen from the group formed by cellulose, hemicellulose and lignin.

3. Method according to claim 1 or claim 2, comprising: - providing a supply of hydrogen (18, 28) in the CO (16) and / or the CO2 (17), downstream of the first separation unit (2), by means of make-up lines, preferably arranged upstream of the methanol synthesis reaction unit (3) and upstream of the Fischer-Tropsch reaction unit (7).

4. A method according to any one of the preceding claims, comprising: - treating methanol (19) in a purification unit (4) to separate water (21) and produce purified methanol (22).

5. A method according to claim 4, wherein the purification unit (4) is adapted to: - separate a recycle gas (20) comprising unconverted CO2 in; and - recycle the recycle gas (20) to the inlet of the methanol synthesis reaction unit (3).

6. A method according to any one of the preceding claims, comprising: - treating aromatic compounds (23) in a third separation unit (6) to separate water (26) and a light gas purge (27) comprising hydrogen and C1-C2 hydrocarbon compounds, and producing an effluent enriched in aromatic compounds (25) sent to the alkylation reaction unit (10).

7. Method according to claim 6, in which the third separation unit (6) is adapted to: - separate a recycle effluent (24) comprising at least one of the following compounds: C3-C4 hydrocarbon compounds, C5-C10 non-aromatic hydrocarbon compounds, benzene, toluene; and - recycle the recycle effluent (24) to the inlet of the aromatization reaction unit (5).

8. Method according to any one of the preceding claims, comprising: - treating the alkylation effluent (38) in a fourth separation unit (11) to separate a cut enriched in alkylated aromatic compounds (40) and optionally recycling a cut containing C6-C8 paraffinic compounds (39) to the inlet of the methanol aromatization reaction unit (5), the cut enriched in alkylated aromatic compounds (40) being mixed at least in part with the hydrocarbon cut (34).

9. A method according to any one of the preceding claims, wherein the CO and CO2 production unit (1) comprises at least one unit selected from a pyrolysis unit, an oxycombustion unit, a gasification unit, a steam reforming unit, a partial oxidation unit, an autothermal reforming unit, a combined reforming unit and a dry reforming unit, an ethanol production unit, preferably the CO and CO2 production unit (1) comprises at least one unit selected from a pyrolysis unit, an oxycombustion unit and a gasification unit.

10. A method according to any one of the preceding claims, wherein the CO and CO2 production unit (1) comprises or consists of a pyrolysis unit adapted to produce at least one pyrolysis effluent (13) comprising hydrocarbon compounds of 6 to 10 carbon atoms and to send the pyrolysis effluent (13) to the alkylation reaction unit (10).

11. Process according to any one of the preceding claims, wherein: the CO and CO2 production unit (1) comprises a pyrolysis unit comprising at least one reactor used under at least one of the following operating conditions: - absolute pressure between 0.1 MPa and 0.5 MPa and WH between 0.01 h 1 and 10 h ', preferably between 0.01 h 1 and 5 h ', and very preferably between 0.1 h 1 and 3 h ', the WH is the ratio of the volume flow rate of feedstock to the volume of catalyst used; - temperature between 400°C and 1000°C, preferably between 400°C and 650°C, preferably between 450°C and 600°C and preferably between 450°C and 590°C; - zeolite catalyst comprising and preferably consisting of at least one zeolite chosen from ZSM-5, ferrierite, Beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-11 and preferably the catalyst is a catalyst comprising only ZSM-5; and / or the CO and CO2 production unit (1) comprises an oxycombustion unit comprising at least one reactor used under at least one of the following operating conditions: - a reactor operating in a fluidized bed; - temperature between 500°C and 1000°C; - pressure between 0.1 MPa and 3 MPa, preferably between 0.1 MPa and 1 MPa, and / or the methanol synthesis reaction unit (3) comprises at least one reactor used under at least one of the following operating conditions: - temperature between 200°C and 450°C, preferably between 220°C and 400°C, and even more preferably between 250°C and 350°C; - pressure between 1 MPa and 12 MPa, preferably between 2 MPa and 10 MPa, and more preferably between 5 MPa and 10 MPa; - hydrogen to COX molar ratio in which COX represents CO and CO2, between 3 and 10, preferably between 3 and 7, very preferably between 3 and 5; - gas space velocity at the reactor inlet between 0.2 g / gcata / h and 1 g / gcata / h, and / or the aromatization reaction unit (5) comprises at least one reactor used under at least one of the following operating conditions: - temperature between 250°C and 500°C, preferably between 300°C and 450°C, and even more preferably between 350°C and 420°C; - pressure between 0.1 MPa and 1 MPa, preferably between 0.2 MPa and 0.8 MPa, and more preferably between 0.4 MPa and 0.5 MPa; - space velocity of the gas at the reactor inlet between 0.2 g / gcata / h and 1 g / gcata / h, and / or the alkylation reaction unit (10) comprises at least one alkylation reactor used under the following operating conditions: - temperature between 20°C and 400°C; - pressure between 1 and 10 MPa; - benzene / ethanol molar ratio between 3 and 15; - PPH between 0.5 and 50 h1.

12. A method according to any one of the preceding claims, wherein: the Fischer-Tropsh reaction unit (7) comprises at least one reactor used under at least one of the following operating conditions: - temperature between 170°C and 280°C, preferably between 190°C and 260°C and preferentially between 210°C and 240°C; - absolute pressure between 1.0 MPa and 6.0 MPa, preferably between 1.5 MPa and 3.5 MPa and preferentially between 2.0 MPa and 3.0 MPa; - catalyst comprising cobalt or iron, preferably cobalt, the catalyst optionally comprising a support, and / or the hydrogen reaction unit (9) comprises at least one reactor used under at least one of the following operating conditions: - temperature between 250°C and 450°C, more preferably between 280°C and 450°C, and even more preferably between 320°C and 420°C;- pressure between 0.2 MPa and 15 MPa, preferably between 0.5 MPa and 12 MPa, more preferably between 1 MPa and 10 MPa; - space velocity defined as the ratio of the volume flow rate of the feed at ambient temperature and pressure to the volume of the catalyst, between 0.1 h 1 and 10 h 1, preferably between 0.2 h 1 and 7 h 1, more preferably between 0.5 h 1 and 5 h 1; - hydrogen flow rate between 100 and 2000 normal liters of hydrogen per liter of charge per hour and preferably between 150 and 1500 normal liters of hydrogen per liter of charge and more preferably between 300 and 1500 normal liters of hydrogen per liter of charge.

13. Device for converting a hydrocarbon feedstock, comprising: - a CO and CO2 production unit (1) adapted to treat the hydrocarbon feedstock (12) and produce at least one synthesis gas (14) comprising at least CO and CO2; - a first separation unit (2) adapted to treat the synthesis gas (14) and separate CO (16) and CO2 (17); - a methanol synthesis reaction unit (3) adapted to treat the CO2 (17) to produce methanol (19); - a methanol aromatization unit (5) adapted to treat the methanol (19) and produce aromatic compounds (23); - an alkylation reaction unit (10) adapted to treat at least in part the aromatic compounds (23) with ethanol (36) and produce an alkylation effluent (38), preferably to the specifications for transport applications; - a Fischer-Tropsch reaction unit (7) adapted to convert CO (16) and produce an FT effluent (29);- a second separation unit adapted to treat at least in part the FT effluent (29) and produce: a hydrocarbon effluent (32), water (33) optionally recycled at least in part to the inlet of the water electrolysis unit, and a gaseous effluent (31, 31) optionally recycled at least in part to the inlet of the Fischer-Tropsch reaction unit (7); - a hydrogen reaction unit (9) (hydrotreatment and / or hydrocracking and / or hydroisomerization unit) adapted to treat the hydrocarbon effluent (32) and produce at least one hydrocarbon cut (34), preferably to the specifications for transport applications; and - a mixing unit (41) for mixing at least in part the hydrocarbon fraction (34) and the alkylation effluent (38), and for producing a formulation for synthetic fuel (42), preferably comprising proportions adapted to the specifications for transport applications.;

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