A process for manufacturing jet fuel from biomass with optimized atom economy

Abstract

Process for manufacturing a jet fuel from biomass exhibiting optimized atom economy. The present invention relates to a process (10) for manufacturing a jet fuel comprising: - a process (20) for producing a jet fuel from a biomass stream, the production process (20) further producing a carbon dioxide stream, and - a subprocess (30) for converting at least a portion of the carbon dioxide stream (213) produced by the production process (20) into a secondary ethylene stream. Figure for the abstract: Figure 1

Description

Title of the invention: Process for manufacturing jet fuel from biomass with optimized atom economy Technical field

[0001] The present invention relates to a method for manufacturing jet fuel from biomass, this method having an optimized atom economy. The present invention also relates to an installation for the production of jet fuel from biomass allowing an optimized use of the biomass.

[0002] CONTEXT OF THE INVENTION

[0003] Environmental, economic and energy constraints have encouraged the diversification of energy resources and the development of new fuels, particularly in the field of aviation.

[0004] Renewable fuels derived from biological material are an alternative to conventional fossil fuels. Conventional jets can be blended with synthetic fuels derived from renewable feedstocks as provided for by standard D7566-21, thus enabling the production of synthetic aviation fuels. As a base for aviation fuel derived from renewable feedstocks, synthetic paraffinic kerosenes [SPK] are known in particular, notably produced by the Alcohol-to-jet route (transformation of alcohol into kerosene) [ATJ-SPK]. This synthesis route generally comprises a step of producing alcohol, for example ethanol, from biomass, followed by dehydration of these alcohols to produce olefins, these olefins then being oligomerized into a mixture of hydrocarbons which is hydrogenated and / or fractionated.

[0005] However, these different stages generate by-products, which are not necessarily recovered. In particular, the stage of producing alcohol from biomass generates large quantities of carbon dioxide, which results in a significant loss of renewable carbon atoms from the biomass used. STATE OF THE ART

[0006] Application US 2009 / 0299109 describes a process for preparing renewable hydrocarbons comprising (a) treating biomass to form a feedstock; (b) fermenting the feedstock with one or more species of microorganisms, thereby forming one or more C2-C6 alcohols; (c) dehydrating at least a portion of the C2-C6 alcohol(s) obtained in step (b), thereby forming a product comprising one or more C2-C6 olefins; (d) isolating the C2-C6 olefin(s); (e) oligomerizing at least a portion of the C2-C6 olefin(s) thereby forming a product comprising one or more unsaturated C6-C24 oligomers; and optionally (f) hydrogenating at least a portion of the product of step (e) in the presence of hydrogen, thereby forming a product comprising one or more saturated C6-C24 alkanes.

[0007] WO 2023287579 describes plants and processes for the integrated conversion and subsequent oligomerization of alcohols and / or ethers of biological origin using zeolite-based catalysts.

[0008] However, none of these documents mention that the biomass transformation step generates a significant production of carbon dioxide and a loss of carbon. Thus, none of the prior art processes include a route for recovering this carbon dioxide.

[0009] There is therefore a need for new processes and new installations for the preparation of jet fuel from biomass allowing an optimized use of the carbon atoms from the biomass, and preferably, allowing an optimized use of the atoms from the biomass. Put another way, there is a need for new processes and new installations for the preparation of jet fuel from biomass allowing a reduction in the quantity of biomass used and / or the quantity of energy required to obtain the same quantity of jet fuel. More generally, there is a need for new processes and new installations for the preparation of jet fuel from biomass having the highest possible atom economy, in particular having the highest possible renewable atom economy.

[0010] DESCRIPTION OF THE INVENTION

[0011] To this end, the invention relates to a method for manufacturing a jet fuel comprising:

[0012] - a process for producing jet fuel from a biomass stream, the production process further producing a carbon dioxide stream, and

[0013] - a sub-process for converting at least a portion of the carbon dioxide stream carbon produced by the production process into a secondary stream of ethylene.

[0014] Advantageously, recovering the carbon dioxide produced by the process for producing jet fuel from biomass and converting this carbon dioxide into ethylene makes it possible to significantly improve the quantity of carbon atoms from the biomass converted into jet fuel. The sub-process of converting at least a portion of the carbon dioxide stream produced by the process for producing jet fuel makes it possible to significantly improve the atom economy of the process for producing jet fuel from biomass.

[0015] Throughout the present application, the expression "a stream of X" must be understood as "a stream comprising X".

[0016] According to other advantageous aspects of the invention, the method according to the invention includes one or more of the following characteristics, taken individually or in all technically possible combinations:

[0017] - at least a portion, preferably all, of the ethylene secondary stream is recycled in the production process;

[0018] - the conversion sub-process further produces a secondary stream of ethanol, and at least a portion, preferably all, of said ethanol side stream is recycled into the production process;

[0019] - the conversion sub-process further produces a stream of dihydrogen, and at at least a portion of said dihydrogen stream is recycled into the production process;

[0020] - the production process further produces a stream of water, and at least a portion, preferably the entire water stream is recycled into the conversion sub-process;

[0021] - the production process further produces a lignin stream, said lignin stream lignin being burned during a combustion step to produce in particular a secondary stream of carbon dioxide and also energy in the form of steam and electricity, and at least a portion, preferably all, of the secondary stream of carbon dioxide is recycled in the conversion sub-process;

[0022] - the production process comprises the following steps:

[0023] - transformation of the biomass stream to produce an ethanol stream and the carbon dioxide stream,

[0024] - dehydration of the ethanol stream to produce an ethylene stream,

[0025] - oligomerization of the ethylene stream produced in the dehydration step for produce a stream of hydrocarbons,

[0026] - hydrogenation of the hydrocarbon stream to produce a stream of hydrogenated hydrocarbons, and

[0027] - fractionation of the hydrogenated hydrocarbon stream produced in step hydrogenation to produce jet fuel;

[0028] - the conversion sub-process comprises the following steps:

[0029] - capture of carbon dioxide produced during the transformation step of the production process, and optionally carbon dioxide produced during the lignin combustion step, to produce a captured carbon dioxide stream, and

[0030] - converting the captured carbon dioxide stream into at least one se stream secondary stream of ethylene, and possibly into a secondary stream of ethanol and / or into a stream of dihydrogen;

[0031] - at least a portion, preferably all, of the ethylene secondary stream produced by the conversion sub-process, preferably by the conversion step of the captured carbon dioxide stream, is recycled into the oligomerization step of the production process;

[0032] - at least a portion, preferably all, of the secondary ethanol stream produced by the conversion sub-process, preferably by the conversion step of the captured carbon dioxide stream, is recycled to the dehydration step of the production process;

[0033] - the conversion sub-process, preferably the step of converting the current of captured carbon dioxide, further produces a dihydrogen stream, and at least a portion of said dihydrogen stream is recycled to the hydrogenation step of the production process;

[0034] - the transformation step further produces a lignin stream, said lignin stream lignin being burned during a combustion step to produce in particular a secondary stream of carbon dioxide as well as energy, and at least a portion, preferably all, of the secondary stream of carbon dioxide is recycled in the conversion sub-process, preferably is captured during the capture step;

[0035] - the dehydration step further produces a stream of water, and at least a portion, preferably the entire water stream is recycled into the conversion sub-process, preferably into the step of converting the captured carbon dioxide stream;

[0036] - at least 20% by weight, preferably from 25 to 95% by weight, preferably from 45 to 90% by weight of the total weight in carbon atoms of the biomass introduced into the process is converted into the hydrogenated hydrocarbon stream (before the fractionation step);

[0037] - at least 15% by weight, preferably from 20% to 80% by weight, preferably from 40 at 80% by weight of the total weight in carbon atoms of the biomass introduced into the process is converted into jet fuel;

[0038] - all of the carbon atoms in jet fuel come from biomass.

[0039] The invention also relates to the use of jet fuel produced by implementing the method according to any one of the preceding claims,

[0040] (i) in admixture with a jet fuel resulting from a distillation of a petroleum, or

[0041] (ii) in admixture with a synthetic jet fuel,

[0042] to power at least one aircraft engine.

[0043] Mixing with a synthetic jet fuel makes it possible to make the mixture thus formed compatible with existing aircraft (drop-in).

[0044] The invention also relates to an installation for manufacturing jet fuel comprising:

[0045] - a production line for a biomass stream into jet fuel, the production line production also producing a stream of carbon dioxide, and

[0046] - a line for converting the carbon dioxide stream into at least one stream secondary ethylene,

[0047] characterized in that the conversion line comprises a conduit for supplying the carbon dioxide stream coming from the production line.

[0048] Preferably, the production line comprises a conduit for supplying the secondary stream of ethylene from the conversion line.

[0049] Preferably, the conversion line further produces a secondary stream of ethanol, and the production line further comprises a conduit for supplying the secondary stream of ethanol from the conversion line.

[0050] Preferably, the conversion line further produces a dihydrogen stream, and the production line further comprises a conduit for supplying the dihydrogen stream from the conversion line.

[0051] Preferably, the production line further produces a water stream, and the conversion line further comprises a conduit for supplying the water stream from the production line.

[0052] Preferably, the production line further produces a lignin stream, the production line comprises a combustion stage for said lignin to produce in particular a secondary stream of carbon dioxide, as well as energy in the form of steam and electricity, and the conversion line further comprises a conduit for supplying the secondary stream of carbon dioxide from the combustion stage.

[0053] The production line preferably comprises:

[0054] - a stage for transforming the biomass stream to produce a stream ethanol and carbon dioxide stream,

[0055] - a stage for dehydrating the ethanol stream to produce a stream of ethylene,

[0056] - an oligomerization stage of the ethylene stream produced by the dehydration stage processing to produce a hydrocarbon stream,

[0057] - a stage for hydrogenating the hydrocarbon stream to produce a stream of hydrogenated hydrocarbons, and

[0058] - a stage for fractionating the stream of hydrocarbons hydrogenated by the stage hydrogenation to produce jet fuel;

[0059] The conversion line preferably comprises:

[0060] - a stage for capturing carbon dioxide produced by the transformation stage, and possibly capturing carbon dioxide produced by the combustion stage, to produce a captured carbon dioxide stream, and

[0061] - a stage for converting the captured carbon dioxide stream into at least one secondary stream of ethylene, and possibly into a secondary stream of ethanol and / or into a stream of dihydrogen.

[0062] Preferably, the production line, preferably the oligomerization stage, comprises a conduit for supplying the secondary ethylene stream coming from the conversion line, preferably coming from the conversion stage of the captured carbon dioxide stream.

[0063] Preferably, the production line, preferably the dehydration stage, comprises a conduit for supplying the secondary ethanol stream from the conversion line, preferably from the conversion stage of the captured carbon dioxide stream.

[0064] Preferably, the production line, preferably the hydrogenation stage, comprises a conduit for supplying the dihydrogen stream coming from the conversion line, preferably coming from the conversion stage of the captured carbon dioxide stream.

[0065] Preferably, the production line, preferably the transformation stage, further produces a lignin stream, the production line further comprises a combustion stage for said lignin to produce in particular a secondary stream of carbon dioxide as well as energy in the form of steam and electricity, and the conversion line, preferably the capture stage, further comprises a conduit for supplying the secondary stream of carbon dioxide coming from the combustion stage.

[0066] Preferably, the production line, preferably the dehydration stage, further produces a water stream, and the conversion line, preferably the conversion stage, further comprises a conduit for supplying the water stream from the production line, preferably the dehydration stage.

[0067] Preferably, the carbon atoms of the jet fuel produced by the fractionation stage correspond to at least 15% by weight, preferably from 20 to 80% by weight, preferably from 40 to 80% by weight of the total weight in carbon atoms of the biomass stream introduced into the transformation stage.

[0068] Preferably, the carbon atoms of the hydrocarbon stream produced by the hydrogenation stage correspond to at least 20% by weight, preferably from 25 to 95% by weight, preferably from 45 to 90% by weight of the total weight in carbon atoms of the biomass stream introduced into the transformation stage. DETAILED DESCRIPTION

[0069] (a) Production of jet fuel from biomass

[0070] The production chain for jet fuel from biomass is known to those skilled in the art. Examples of processes for producing jet fuel from of biomass are in particular detailed in WO 2023 / 287579 and US 2009 / 0299109.

[0071] (al) Transformation of a biomass to produce ethanol and co-produce carbon dioxide

[0072] Any suitable type of lignocellulosic biomass may be used. Examples of biomass include, but are not limited to, sugarcane straw, corn cobs, corn stover, corn fiber, hard or soft wood, sugarcane bagasse.

[0073] Conventionally, the conversion of biomass into ethanol comprises the following steps:

[0074] (a) optionally, grinding of the lignocellulosic biomass;

[0075] (b) exposure of the biomass to steam or hot liquid water, possibly acid, for example in a digester, to release cellulose and hemicellulose from lignin and / or to increase the accessibility of cellulose and hemicellulose to enzymatic hydrolysis;

[0076] (c) enzymatic hydrolysis to depolymerize carbohydrate sugars of hemicellulose and cellulose and obtain sugars, for example in a hydrolysis reactor; and

[0077] (d) fermentation of sugars, for example in a fermenter, to obtain including ethanol and carbon dioxide.

[0078] The enzymes used during step c) may be cellulase enzymes (for example [3-glucosidases]) or hemicellulase enzymes (for example acetylesterase, xylanase, [3-xylosidase, galactomannase and glucomannase).

[0079] The sugars produced are in particular hexose sugars such as glucose and pentose sugars.

[0080] Examples of transformation of biomass into ethanol suitable for the process of the invention are detailed in WO 2011028554 or WO2016134195.

[0081] At the end of step (d), the stream obtained is rich in ethanol, but also contains solid residues, in particular lignin. These residues can be removed, for example in a recovery unit. This results in an ethanol stream free of solids but comprising water (from 60 to 80% by weight, for example). In some cases, the solids-free ethanol stream with a significant water content can be used as a feedstock for the conversion of ethanol to olefins. In other cases, at least part of the excess water is removed by a series of separators, such as distillation columns and / or molecular sieve separators. Concentrated ethanol (for example, between 40 and 96% by weight of ethanol, preferably from 80% by weight to 95% by weight, or from 85% by weight to 95% by weight,) is thus obtained.

[0082] (a2) Dehydration of the ethanol stream to produce an ethylene stream

[0083] Ethanol from biomass processing can be converted into ethylene by dehydration, by any process suitable for such a reaction.

[0084] The dehydration of ethanol to ethylene can be catalyzed by numerous catalysts, homogeneous or preferably heterogeneous, and the ethanol is generally activated by an acid catalyst to facilitate water loss. Water is generally removed from the reaction zone with the product. Since water is generated in large quantities during the dehydration step, the catalysts used are water tolerant and the dehydration stage is configured to remove the produced water.

[0085] The dehydration of ethanol can be carried out in a reactor in the presence of a zeolitic catalyst, such as for example in the presence of a catalyst comprising a phosphorus-modified zeolite as described in WO 2013 / 017496.

[0086] (a3) ​​Oligomerization of the ethylene stream produced in the dehydration step for produce a stream of hydrocarbons

[0087] The ethylene formed during the dehydration step can either be transferred directly to the oligomerization stage or can be isolated / purified before oligomerization, for example by distillation.

[0088] The oligomerization of ethylene is known to those skilled in the art, and can in particular be implemented according to the different conditions described in the following review: “Applications of light olefin oligomerization to the production of fuels and Chemicals” Christopher P. Nicholas Applied Catalysis A: General Volume 543, 5 August 2017, Pages 82-97.

[0089] Various heterogeneous and homogeneous catalysts may be used, including solid-phase acid catalysts such as solid phosphoric acid, acid resins, amorphous silica-alumina, and zeolites. Metallic or organometallic catalysts may also be used. The reaction is typically carried out in a reactor, for example, a catalytic bed reactor.

[0090] Ethylene is converted into unsaturated aliphatic compounds, mainly dimers, trimers, tetramers or pentamers. The hydrocarbon stream formed typically contains butenes, hexenes, heptenes, octenes, nonenes, decenes, undecenes and dodecenes.

[0091] In some cases, the catalyst and / or reactor of the ethylene dehydration stage and the oligomerization stage may be the same. Preferably, the dehydration and oligomerization / rearrangement steps may be carried out separately.

[0092] (a4) Hydrogenation of the hydrocarbon stream to produce a stream of hydrogenated hydrocarbons

[0093] The hydrocarbon stream undergoes hydrogenation to form a hydrogenated hydrocarbon stream. This saturates the olefinic compounds.

[0094] The hydrogenation of the hydrocarbons formed by the oligomerization step can be carried out by any technique known to those skilled in the art.

[0095] Hydrogenation is for example carried out in one or more fixed bed (descending or ascending) and mixed phase reactors, the fraction to be hydrogenated being mainly in the liquid phase.

[0096] The hydrogenation is for example carried out at a temperature between 50°C and 350°C, in particular between 100°C and 300°C. It is carried out under a pressure preferably greater than 10 bara and in particular between 20 bara and 80 bara.

[0097] A stream of hydrogen is fed into the or each reactor in a mixture with the stream of hydrocarbons to be treated. Excess hydrogen can be recycled into the reaction zone after separation and compression.

[0098] A hydrogen stream is fed into the or each reactor in a mixture with the hydrocarbon stream to be treated. The ratio of the volume flow rate of the hydrogen stream to the volume flow rate of the hydrocarbon stream (not including the recycled stream) to be hydrogenated is advantageously between 50 NL / L and 3000 NL / L, in particular between 100 NL / L and 500 NL / L. The hydrogen can be added to the hydrocarbon stream in several stages along the catalytic bed. The hourly space velocity is advantageously between 0.5 and 3 and in particular between 1 and 2 h1. The excess hydrogen can be recycled into the reaction zone after separation and compression.

[0099] The reaction is carried out in the presence of at least one catalyst comprising one or more metals from group VIII (typically Pt, Pd, Ni) supported on a support such as silica, alumina or any mixture of these two compounds or carbon. The reaction can also be carried out in the presence of a sulfide type catalyst containing an element from group VIB (Cr, Mo, W) and an element from group VIIIB (Fe, Ru, Co, Os, Co, Rh, Ir, Pd, Ni, Pt) or mixtures of these two groups of metals.

[0100] The hydrogenated hydrocarbon stream advantageously contains less than 10% by mass of olefins and preferably less than 3% of olefins.

[0101] It preferably contains more than 50% by mass of paraffins, in particular more than 50% by mass of C7 to C18 paraffins, in particular more than 60% by mass of C7 to C18 paraffins, in particular between 70% by mass and 95% by mass of C7 to C18 paraffins.

[0102] (a5) Fractionation of the hydrogenated hydrocarbon stream produced in step hydrogenation to produce jet fuel

[0103] To recover the jet fuel, the stream of hydrogenated hydrocarbons advantageously undergoes fractionation. This fractionation can be carried out by passing it through at least one separation column, for example a distillation column.

[0104] Preferably at least one first separation column is used to separate, at the top, a fraction of liquefied petroleum gas from the remainder of the stream of hydrogenated hydrocarbons which is obtained at the bottom.

[0105] The fractionation conditions in this column are as follows: pressure advantageously between 2 bara and 15 bara, head condensation temperature adjusted to be able to use an air or cooling water condenser, i.e. preferably between 20°C and 50°C.

[0106] The residual fraction of hydrogenated hydrocarbon stream is then introduced into a second separation column to produce a naphtha fraction at the top, a diesel fraction at the bottom and at least one intermediate stage the jet fuel fraction. This fractionation can be carried out in a single column including a side draw of the jet fuel fraction, or in two separate columns.

[0107] More than 80% by mass of the hydrogenated hydrocarbon stream introduced into the second column advantageously forms the jet fuel fraction.

[0108] The liquefied petroleum gas fraction preferably has a final boiling point of less than 50°C, and even more preferably a final boiling point of less than 30°C.

[0109] The naphtha fraction comprises more than 80% by mass of the C8- paraffins contained in the residual fraction.

[0110] The jet fuel fraction preferably has a final boiling point of less than 300°C. The initial boiling point may be from 120°C to 180°C.

[0111] The diesel fraction is the heaviest fraction, not all of whose molecules can be used to form jet fuel. This fraction typically has an initial boiling point above 200°C, and preferably 250°C.

[0112] (b) Conversion of carbon dioxide to ethylene

[0113] The process according to the invention is characterized in that the carbon dioxide produced by the process for producing jet fuel from biomass is recycled by its conversion into ethylene.

[0114] (bl) Capture of carbon dioxide produced during the transformation step of the production process, and possibly carbon dioxide produced during the lignin combustion step.

[0115] The most mature CO2 capture process is the one that uses an amine that countercurrently absorbs the CO2 from the stream to be treated. The captured CO2 is then regenerated in an amine regenerator to be recycled and perform a new absorption.

[0116] There are also adsorption processes that use solid adsorbents to retain CO2. The adsorbent is also regenerated to be able to adsorb CO2 again.

[0117] (b2) Conversion of the captured carbon dioxide stream into ethylene

[0118] Once captured, the carbon dioxide can be converted into ethylene.

[0119] Such a conversion is for example carried out by electrolysis, as detailed in WO 2012125053.

[0120] The reaction is typically carried out in an electrochemical cell where the cathode is an electrode modified with electrolytic catalyst deposits, in particular copper deposits. This makes it possible to optimize the production of ethylene. The CO2 electroconversion reactions are not 100% selective for ethylene, and ethanol and hydrogen are also produced at the cathode. The ethanol can be dehydrated to ethylene and the hydrogen used to carry out hydrotreatment reactions. Oxygen will be produced on the other electrode, the anode. The downstream separation contains a CO2 capture unit and a water / ethanol separation unit, the remainder (CO, CH3) is very comparable to the separations used in steam cracker units. The separation energy is low (15-20%) compared to the energy required for the electroconversion reactions.

[0121] (c) Combustion of lignin

[0122] The lignin combustion step is a step known industrially to those skilled in the art.

[0123] This combustion can be carried out in ambient air, or with oxygen-enriched air, or even with pure oxygen (oxycombustion). Oxycombustion or combustion in O2-enriched air makes it possible to produce CO2-enriched fumes and therefore facilitate CO2 recovery. DESCRIPTION OF FIGURES

[0124] The invention will be better understood on reading the following description, given solely by way of example, and made with reference to the appended drawings, in which:

[0125] - [Fig.l] [Fig.l] is a block diagram of a manufacturing process for a carburetor reactor according to the invention, and

[0126] - [Fig.2] [Fig.2] is a schematic view of an installation configured for the implementation of the method for manufacturing jet fuel according to the invention.

[0127] DESCRIPTION OF EMBODIMENTS OF THE INVENTION

[0128] A method 10 for manufacturing jet fuel is schematically represented in [Fig.l],

[0129] The process 10 comprises a process 20 for producing a jet fuel from a biomass stream and further producing a carbon dioxide stream, and a sub-process 30 for converting at least a portion of the carbon dioxide stream produced by the production process 20 into a secondary ethylene stream. The sub-process 30 is carried out in parallel with the process 20.

[0130] The production method 20 comprises a step 22 of transforming the biomass stream to produce an ethanol stream and the carbon dioxide stream.

[0131] The method 20 then comprises a step 24 of dehydration of the ethanol stream. to produce an ethylene stream.

[0132] The ethylene stream is then oligomerized during an oligomerization step 26, to produce a hydrocarbon stream.

[0133] During a hydrogenation step 28, the hydrocarbon stream is hydrogenated to produce a hydrogenated hydrocarbon stream.

[0134] The hydrogenated hydrocarbon stream is fractionated during a fractionation step 29, in particular to obtain jet fuel.

[0135] According to an alternative embodiment, fractionation step 29 is carried out before hydrogenation step 28. According to this embodiment, the hydrocarbon stream is fractionated using one or more fractionation columns to produce an LPG stream, a gasoline stream, a kerosene stream, and optionally a diesel cut stream. The kerosene stream is then hydrogenated to produce jet fuel.

[0136] In parallel, the carbon dioxide stream produced in transformation step 22 is captured during a capture step 32.

[0137] The captured carbon dioxide is then converted into ethanol during a conversion step 34.

[0138] The capture step 32 and the conversion step 34 of the sub-process 30 are therefore carried out in parallel with the dehydration step 24.

[0139] In a particular embodiment, step 22 of transforming the biomass into ethanol co-produces in particular lignin, which can be burned during a combustion step 40 to produce in particular energy. The combustion step 40 produces in particular a secondary stream of carbon dioxide, which is captured during the capture step 32.

[0140] A manufacturing installation 100 intended for implementing the method for manufacturing a jet fuel according to the invention is illustrated schematically in [Fig.2],

[0141] The installation 100 comprises a line 200 for producing a stream 203 of biomass into a jet fuel 255, the production line 200 further producing a stream 213 of carbon dioxide, and further comprises a line 300 for converting the stream 213 of carbon dioxide into at least the secondary stream 323 of ethylene.

[0142] The production line 200 comprises a stage 210 for transforming the biomass stream 203 to produce an ethanol stream 215 and the carbon dioxide stream 213. The transformation stage 210 is intended to implement the transformation step 22, making it possible to transform the biomass into ethanol. This transformation step 22 further produces the carbon dioxide stream 213, a lignin stream 217. The transformation stage 210 is as defined in part (al) above. above.

[0143] Advantageously, the production line 200 also comprises a combustion stage 410, intended to burn the lignin stream 217 and to produce steam and electricity necessary for the process. This combustion can be carried out in ambient air, or with oxygen-enriched air, or even with pure oxygen (oxycombustion). Oxycombustion or combustion with O2-enriched air makes it possible to produce CO2-enriched fumes and therefore to facilitate the recovery of CO2. This combustion produces in particular a secondary stream 413 of carbon dioxide, which is conveyed by a supply duct to the conversion line 300. The fact of being able to convert the lignin produced by the transformation stage 210 into CO2, and therefore into ethanol and ethylene, then into jet fuel, makes it possible to further improve the economy of atoms, in particular carbon atoms, of the installation.

[0144] The production line 200 further comprises a stage 220 for dehydrating the ethanol stream 215 to produce an ethylene stream 223. The dehydration stage 220 is intended to implement the dehydration step 24, and is configured to transform the ethanol into ethylene. This reaction produces water, which is separated by the stage 220 to produce a water stream 225. The dehydration stage 220 is as defined in part (a2) above.

[0145] The production line 200 further comprises a stage 230 for oligomerizing the ethylene stream 223 to produce a hydrocarbon stream 233. The oligomerization stage 230 is intended to implement the oligomerization step 26. The oligomerization stage 230 is as defined in part (a3) ​​above.

[0146] The hydrocarbon stream 233 is then conveyed to a hydrogenation stage 240 of the production line 200 to produce a stream 243 of hydrogenated hydrocarbons. The hydrogenation stage 240 is intended to implement the hydrogenation step 28 of the process according to the invention. The hydrogenation stage 240 is as defined in part (a4) above.

[0147] The production line 200 finally comprises a fractionation stage 250, making it possible to separate the stream 243 of hydrogenated hydrocarbons into different fractions. This fractionation stage 250 makes it possible, for example, to obtain a fraction 253 of liquefied propane gas (LPG), a fraction 254 of naphtha, a fraction 255 of jet fuel, and a fraction 257 of diesel. The fractionation stage 250 is as defined in part (a5) above.

[0148] In parallel, the installation 100 comprises a conversion line 300 making it possible to convert the stream 213 of carbon dioxide coming from the production line 200 in particular into a secondary stream 323 of ethylene, thanks to a conduit for supplying the stream 213 of carbon dioxide coming from the production line 200, and more precisely coming from the transformation stage 210. The stream The secondary ethylene stream 323 is then reintroduced into the production line 200, and more precisely into the oligomerization stage 230, to be oligomerized with the ethylene stream 223 coming from the production line 200 via a conduit for supplying the secondary ethylene stream 323 coming from the conversion line 300. The secondary ethylene stream 323 is in particular mixed with the ethylene stream 223 and the mixture of the ethylene stream 223 and the secondary ethylene stream 323 is oligomerized in the oligomerization stage 230.

[0149] This advantageously makes it possible to recycle the carbon dioxide produced during the transformation of biomass into jet fuel and transforming it into ethylene which is reintroduced into the main line for producing biomass into jet fuel, which therefore increases the carbon atom economy of the installation.

[0150] The conversion line 300 comprises a stage 310 for capturing the carbon dioxide produced by the transformation stage 210, and optionally for capturing the carbon dioxide produced by the combustion stage 410, to produce a captured carbon dioxide stream 313. This capture stage 310 is intended to implement the capture step 32 of the method according to the invention. The capture stage 310 is as defined in part (bl) above. The capture stage 310 may also make it possible to separate the CO2 from the other constituents of the carbon dioxide stream 213 coming from the production line 200, and optionally from the secondary carbon dioxide stream 413, and / or to concentrate the carbon dioxide in the captured carbon dioxide stream 313.

[0151] The conversion line 300 further comprises a stage 320 for converting the captured carbon dioxide stream 313 to produce the secondary ethylene stream 323, a secondary ethanol stream 325 and a dihydrogen stream 327. The conversion stage 320 is as defined in part (b2) above.

[0152] The supply conduit for the secondary stream 323 of ethylene comes from the conversion stage 320.

[0153] The secondary stream 325 of ethanol is conveyed to the dehydration stage 220 by a supply conduit for said secondary stream 325 of ethanol coming from the conversion stage 320. The secondary stream 325 of ethanol is in particular mixed with the stream 215 of ethanol, and the mixture of the stream 215 of ethanol and the secondary stream 325 of ethanol is dehydrated by the dehydration stage 220.

[0154] The dihydrogen stream 327 is conveyed to the hydrogenation stage 240 by a conduit for supplying said dihydrogen stream 327 from the conversion stage 320. In certain embodiments, the quantity of dihydrogen produced by the conversion stage 320 is greater than the quantity required by the hydrogenation stage 230. The dihydrogen stream 327 is therefore separated into a stream 328 of excess dihydrogen, and a stream 329 of dihydrogen recycled into the stage 240. of hydrogenation.

[0155] Finally, the water stream 225 co-produced during the dehydration stage 220 can be recycled by being conveyed to the conversion stage 320 by a conduit for supplying said water stream 225 coming from the dehydration stage 220. In certain embodiments, the quantity of water in the water stream 225 is not sufficient, and an additional water stream 316 must be added to the water stream 225 to form a water stream 318 introduced into the conversion stage 320.

[0156] Recovering and using the secondary ethanol stream 325, the dihydrogen stream 327 and the water stream 225 makes it possible to improve the efficiency of carbon atoms, and more broadly the efficiency of atoms in general.

[0157] This atom economy is illustrated by the values ​​in the following table, representing the quantities of materials expected from 500 kt of biomass according to three different processes and installations, described below:

[0158] Process / Installation 1 (comparative): No recycling (corresponds to jet fuel production line 200 without conversion line 300)

[0159] Process / Installation 2 (according to the invention): recycling of the secondary stream 323 of ethylene, of the stream 325 of ethanol and of the stream 327 of dihydrogen in the production line 200, but no recycling of the stream 225 of water or of the stream of lignin 217

[0160] Process / Installation 3 (according to the invention): recycling of the secondary stream 323 of ethylene, of the stream 325 of ethanol and of the stream 327 of dihydrogen in the production line 200, and recycling of the lignin stream 217 in the conversion line 300 (use of the secondary stream 413 of carbon dioxide).

[0161] [Tables 1] Current Quantity of material (kt) Process / Installation 1 (comparative) Process / Installation 2 (invention) Process / Installation 3 (invention) Biomass (203) 500 500 500 CO2 (213) 100 100 100 Lignin + residues (217) 300 300 300 CO2 (413) - - 270 Ethanol (215) 100 100 100 Ethylene (223) 61 69.5 69.5 Water (225) 39 44.5 Hydrocarbons (233) 62 92.5 178 Jet fuel (255) 52 78.6 151 Secondary ethylene (323) - 23 85 Secondary ethanol (325) - 14 52 Dihydrogen (327) - 1.4 5.2 Excess dihydrogen (328) - 0.5 1.8 Dihydrogen introduced (329) 0.7

[0162] These results illustrate the interest of the process and the installation according to the invention, since for the same initial quantity of biomass (500 kt), a much higher quantity of jet fuel can be obtained. In addition, this quantity is doubled when the stream 217 of lignin and residues is recovered.

Claims

Claims

1. A method (10) of manufacturing a jet fuel (255) comprising: - a method (20) of producing a jet fuel (255) from a biomass stream (203), the production method (20) further producing a carbon dioxide stream (213), and - a sub-process (30) of converting at least a portion of the carbon dioxide stream (213) produced by the production method (20) into a secondary ethylene stream (323).

2. The process (10) of claim 1, wherein at least a portion of the ethylene side stream (323) is recycled to the production process (20).

3. The process (10) of claim 1 or 2, wherein the conversion sub-process (30) further produces a secondary ethanol stream (325), and at least a portion of said secondary ethanol stream (325) is recycled to the production process (20).

4. A method (10) according to any preceding claim, wherein the production method (20) comprises the following steps: - transforming (22) the biomass stream (203) to produce an ethanol stream (215) and the carbon dioxide stream (213), - dehydrating (24) the ethanol stream (215) to produce an ethylene stream (223), - oligomerizing (26) the ethylene stream (223) produced in the dehydration step (24) to produce a hydrocarbon stream (233), - hydrogenating (28) the hydrocarbon stream (233) to produce a hydrogenated hydrocarbon stream (243), and - fractionating (29) the hydrogenated hydrocarbon stream (243) produced in the hydrogenation step (28) to produce jet fuel (255).

5. The process (10) of claim 4, wherein at least a portion of the ethylene side stream (323) produced by the conversion sub-process (30) is recycled to the oligomerization step (26) of the production process (20).

6. The process (10) of claim 4 or 5, wherein at least a portion of the secondary ethanol stream (325) produced by the conversion sub-process (30) is recycled to the dehydration step (24) of the production process (20).

7. A process (10) according to any one of claims 4 to 6, wherein the conversion sub-process (30) further produces a dihydrogen stream (327), and at least a portion of said dihydrogen stream (327) is recycled to the hydrogenation step (28) of the production process (20).

8. A method (10) according to any one of claims 4 to 7, wherein the transformation step (22) further produces a lignin stream (217), said lignin stream (217) being combusted during a combustion step (40) to produce in particular a secondary stream (413) of carbon dioxide as well as energy, and at least a portion of the secondary stream (413) of carbon dioxide is recycled to the conversion sub-process (30).

9. A method (10) according to any one of claims 4 to 8, wherein the dehydration step (24) further produces a water stream (225), and at least a portion of the water stream (225) is recycled to the conversion sub-process (30).

10. A method (10) according to any one of claims 4 to 9, wherein the conversion sub-process (30) comprises the following steps: - capturing (32) the carbon dioxide produced during the transformation step (22) of the production method (20), and optionally the carbon dioxide produced during the combustion step (40), to produce a captured carbon dioxide stream (313), and - converting (34) the captured carbon dioxide stream (313) into at least one secondary ethylene stream (323), and optionally into a secondary ethanol stream (325) and / or into a dihydrogen stream (327).

11. The process (10) of any one of claims 1 to 10, wherein at least 20% by weight of the total carbon atom weight of the biomass (203) introduced into the process (10) is converted into the hydrogenated hydrocarbon stream (243).

12. Use of the jet fuel (255) produced by implementing the method (10) according to any one of the preceding claims, (i) in a mixture with a jet fuel resulting from a distillation of a petroleum, or (ii) in a mixture with a synthetic jet fuel, to power at least one aircraft engine.

13. Installation (100) for manufacturing a jet fuel (255) comprising: - a line (200) for producing a stream (203) of biomass into a jet fuel (255), the transformation line (200) further producing a stream (213) of carbon dioxide, and - a line (300) for converting the carbon dioxide stream (213) into at least the secondary ethylene stream (323), characterized in that the conversion line (300) comprises a conduit for supplying the stream (213) of carbon dioxide coming from the transformation line (200).

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