Method for the organic preparation of a catalyst in the presence of a hydrogen halide additive

Abstract

The present invention relates to a method for preparing a catalyst, comprising: a) a step of preparing an organic solution comprising: a metal precursor of a metal element chosen from the elements of groups 3, 4 and 5 of the periodic table, an acid additive chosen from hydrogen halides, hydrogen halide precursors, and mixtures thereof, and an organic solvent, said at least one metal precursor and said at least one acid additive being present in the organic solution, at an acid / metal molar ratio between the number of moles of hydrogen halide equivalent and the number of moles of the metal element is greater than or equal to 1; b) a step of depositing said metal precursor on an oxide matrix, by bringing the organic solution into contact with said oxide matrix; then c) a heat treatment step.The present invention also relates to the catalyst obtained and its use for converting a feedstock comprising ethanol into butadiene.

Description

Title of the invention: Method for the organic preparation of a catalyst in the presence of a hydrogen halide additive Technical field

[0001] The present invention relates to a method for manufacturing a supported metal oxide catalyst of a group 3, 4 and / or 5 element having improved performance. More particularly, the present invention relates to a method for preparing a heterogeneous catalyst comprising at least one metallic element selected from the elements of groups 3, 4 and 5 of the periodic table, deposited on an oxide matrix by bringing said oxide matrix into contact with an organic solution of at least one precursor of said at least one metallic element, said organic solution also containing an acid additive of the hydrogen halide type, in particular a hydrogen halide or a hydrogen halide precursor. The present invention also relates to the catalyst obtained by said preparation method and the use of this catalyst for the conversion into butadiene of a feedstock comprising at least ethanol.The present invention also relates to a process for converting a feedstock comprising at least ethanol into butadiene, comprising in particular a step corresponding to the method for preparing a heterogeneous catalyst according to the invention. Prior art

[0002] Supported metal oxides are a class of heterogeneous catalysts that comprise one or more metal oxide species charged and deposited on the surface of a support material, such as silica (SiO2), alumina (Al2O3), titanium (TiO2), zirconia (ZrO2), magnesium oxide (MgO), and mixtures thereof. Examples of commonly used metal oxides include Group 3-10 metal oxides because they are capable of forming numerous catalysts that are used to synthesize a wide variety of chemicals.For example, supported tantalum oxide catalysts have active sites with diverse properties (acid-base and redox) and are therefore capable of catalyzing many chemical reactions relevant to industry, including the production of 1,3-butadiene (which may also be referred to in this description as butadiene) from ethanol, the decomposition of methyl-t-butyl ether into isobutene and methanol, the Beckmann rearrangement, the epoxidation of olefins. They also have utility in photocatalysis or electrocatalysis.

[0003] As with any catalyst composed of a metallic element deposited on a support, a particular dispersion and a specific distribution of the metallic element metal, for example tantalum, can be investigated to characterize the catalyst. The dispersion of the metallic element at the atomic level is known to affect the selectivity and activity of the catalyst, via modulation of the nature of the active site. Completely independently, the control of the distribution of the metallic element in a support particle is another parameter to explore to manage problems of intra-granular diffusional limitations when these exist. In the absence of intergranular diffusional limitations, it is generally known to use the entire available surface and volume, particularly for catalytic performance considerations.

[0004] There is still a need to improve the catalytic performance, for example the selectivity, of a heterogeneous catalyst comprising in particular a metallic element chosen from the elements of group 3, 4 and / or 5, and possibly to improve the distribution of the metallic element on the catalytic support.

[0005] In the case of the preparation of catalysts comprising the element tantalum, the use of commercial tantalum precursors, soluble in organic medium such as tantalum alcoholates or halides, is widely described, as in application WO2017 / 009107 or in the article by Corson from 1950 (BB Corson, at al. Butadiene form Ethyl Alcohol. Catalysis in the One- and Two-Step Processes. Industrial And Engineering Chemistry. 1950, 42 (2), 359-373). However, tantalum alcoholate precursors or halides may have the disadvantage of being extremely sensitive to hydrolysis. The formation of a tantalum hydroxide function results in the formation of tantalum clusters and can therefore lead to a modification or even a limitation of the catalytic performances (cf. Ambreen, S. et al., Characterization and photocatalytic study of tantalum oxide nanoparticles prepared by the hydrolysis of tantalum oxo-ethoxide Ta8(q3-O)2(qO)8(q-OEt)6(OEt)i4.Beilstein J. Nanotechnology. 2014, 5, 1082-1090). .

[0006] To limit the hydrolysis phenomenon, it therefore seems necessary to limit the quantity of water present within the support, for example by extensive drying of the support, in particular at temperatures above 100°C, preferably at 150°C for several hours. To further limit the hydrolysis phenomenon of tantalum or niobium precursors (which are group 5 elements), it is possible to modify said precursors via the addition of additives.

[0007] The literature is full of various complexing agents that have varying successes. For example, there are studies on the reaction of group 5 elements, particularly tantalum and niobium, with compounds such as:

[0008] - acetylacetone (see Kapoor PN, Mehrotra RC, Organic Compounds of Niobium and Tantalum. IV. Reactions of niobium and tantalum pentaethoxides with [3-diketones. J. Less-Common Metals, 8 (1965) 339-346),

[0009] - des cétoesters (cf. Mehrotra R.C., Kapoor P.N., Organic Compounds of Tantalum. Reactions of tantalum pentaethoxide with [3-ketoesters. J. Less-Common Metals, 7 (1964) 453-457),

[0010] - des hydroxyesters (cf. Narula A.K., et al., Some Aliphatic and Aromatic Hydroxy Ester Dérivatives of Niobium and Tantalum. Transition Met. Chem. 7 (1982) 325-330),

[0011] - des glycols (cf. Mehrotra R.C., Kapoor P.N., Organic Compounds of Tantalum. I. Reactions of tantalum pentaethoxide with glycols. J. Less-Common Metals, 10 (1965) 237-245),

[0012] - des halogénures d’acyle (cf. R Mehrotra R.C., Kapoor P.N., Organic Compounds of Niobium. I. Reactions of niobium penta-alkoxides with acyl halides. J. Less-Common Metals, 10 (1966) 348-353).

[0013] While these documents detail the reactions and properties of the complexes formed, they do not specify the effect and use of such Ta or Nb complexes in the preparation of heterogeneous catalysts. Application WO2022 / 165190 describes the use of acetylacetone in the preparation of a tantalum-based catalyst deposited on silica.

[0014] The objective of the present invention is to prepare a heterogeneous catalyst comprising at least one metallic element, in particular chosen from the elements of groups 3, 4 and 5, which exhibits good catalytic performances, or even a gain in performances compared to the catalysts of the state of the art, in particular in terms of selectivity and productivity, and in particular during the conversion into butadiene of a feed comprising ethanol, and which exhibits a better distribution (or distribution) of the metallic element over the entire support. Summary of the invention

[0015] The present invention thus relates to a method for preparing a catalyst, comprising:

[0016] a) a step of preparing at least one organic solution comprising:

[0017] at least one metallic precursor of at least one element chosen from the elements from groups 3, 4 and 5 of the periodic table,

[0018] at least one acid additive chosen from hydrogen halides, hydrogen halide precursors, and mixtures thereof, and

[0019] an organic solvent,

[0020] said at least one metal precursor and said at least one acid additive being present in the organic solution in quantities such that the acid / metal molar ratio between the number of moles of hydrogen halide equivalent and the number of moles of the metal element(s) provided by said at least one metal precursor is greater than or equal to 1;

[0021] b) a step of depositing said at least one metal precursor on an oxide matrix, by bringing the organic solution prepared in step a) into contact with said oxide matrix, to obtain a solid,

[0022] c) a step of heat treatment of the solid obtained at the end of step b).

[0023] Such a process makes it possible to obtain a catalyst whose catalytic performances, in particularly in terms of selectivity and productivity, during the reaction for converting a feedstock comprising ethanol into butadiene, are satisfactory or even improved compared to catalysts of the state of the art, in particular prepared organically. The present invention therefore has the advantage of allowing the simple preparation of catalysts with satisfactory or even improved performance, for reasonable production costs. A process according to the present invention can also allow a better distribution of the metallic elements in the particles of the support (i.e. of the oxide matrix).

[0024] The invention also relates to the catalyst obtained by the preparation process according to the invention, which comprises at least one metallic element chosen from the group of elements of groups 3, 4 and 5 of the periodic table, preferably chosen from yttrium, zirconium, hafnium, niobium, tantalum and their mixtures, preferentially from the element tantalum, the element niobium and / or the element zirconium, very preferably the element tantalum, and an oxide matrix preferably based on silica.

[0025] The present invention also relates to the use of said catalyst for converting a feedstock comprising ethanol into butadiene, at a temperature of between 250 and 450°C, at a pressure of between 0.05 and 2.00 MPa.

[0026] Finally, the present invention relates, according to another aspect, to a process for converting a feedstock comprising at least ethanol into butadiene, which comprises:

[0027] A) the preparation of a catalyst according to the preparation method according to the invention;

[0028] B) a step of converting the feedstock comprising ethanol into butadiene, carried out in the presence of the catalyst prepared in step A), at a temperature between 250 and 450°C, at a pressure between 0.05 and 2.00 MPa. Description of the embodiments

[0029] According to the invention, the expressions "between ... and ..." and "between .... and ..." are equivalent and mean that the limit values ​​of the interval are included in the range of values ​​described. If this is not the case and the limit values ​​are not included in the range described, such clarification will be provided by the present description.

[0030] In the present description, the different parameter ranges for a step given, such as pressure ranges and temperature ranges, may be used alone or in combination. For example, in the present disclosure, a range of preferred pressure values ​​may be combined with a range of more preferred temperature values.

[0031] In the following, particular embodiments of the invention are described. They can be implemented separately or combined with each other, without limitation of combinations when this is technically feasible.

[0032] According to the present invention, the pressures are absolute pressures and are given in absolute MPa (or MPa abs.).

[0033] According to the invention, the times and durations are expressed in hours (h), in minutes (min) and / or in seconds (sec).

[0034] In the present description, the term "ambient temperature (Tamb)" corresponds to a temperature typically of 20°C ± 5°C (the acronym "±" meaning "more or less", "20°C ± 5°C" means between 15 and 25°C), and the term "atmospheric pressure" means a pressure of approximately 0.1 MPa, i.e. between 0.05 MPa and 0.15 MPa, preferably between 0.08 MPa and 0.12 MPa, and generally a pressure of 0.101325 MPa.

[0035] The terms “upstream” and “downstream” are to be understood in relation to the general flow of the fluid(s) or flow(s) in question in the process.

[0036] The present invention relates to a method for preparing a catalyst, also called a heterogeneous catalyst, which comprises at least one metallic element chosen from the elements of groups 3, 4 and 5 of the periodic table, preferably from yttrium, zirconium, hafnium, niobium, tantalum, and mixtures thereof, preferentially niobium, tantalum, zirconium, and mixtures thereof, very preferentially tantalum, and an oxide matrix, preferably based on silica.

[0037] The preparation method according to the invention comprises, very particularly consists of, the following steps:

[0038] a) a step of preparing at least one organic solution which comprises at least one metal precursor of at least one metal element chosen from the elements of groups 3, 4 and 5 of the periodic table, at least one acid additive, advantageously at least one hydrogen halide and / or one hydrogen halide precursor, and an organic solvent, said at least one metal precursor and said at least one acid additive being present in the organic solution in amounts such that the molar ratio (acid / metal) between the number of moles of hydrogen halide equivalent, in particular the number of moles of said at least one acid additive, and the number of moles of the metal element(s) provided by said at least one metal precursor is greater than or equal to 1, preferably greater than or equal to 2, preferably between 2 and 20, more preferably between 5 and 15;

[0039] b) a step of depositing said at least one metal precursor on an oxide matrix, by bringing the organic solution prepared in step a) into contact with said oxide matrix, to obtain a solid,

[0040] b') optionally a step of maturation of the solid obtained at the end of step b),

[0041] c) a step of heat treatment of the solid resulting from step b) of deposition or even (b) maturation, preferably comprising drying or drying followed by calcination,

[0042] the drying being advantageously carried out at a temperature between 50 and 200°C and preferably between 80 and 150°C, for a duration between 1 and 24 hours, advantageously under a gas flow, preferably under an air flow;

[0043] the calcination, when integrated into step c), being advantageously carried out under a gas flow, preferably under a gas flow comprising oxygen, at a temperature of between 350 and 700°C, preferably between 450 and 600°C, for a duration of between 1 and 6 h, preferably between 2 and 4 h; and

[0044] d) optionally the repetition of the succession of steps b) of deposition and c) of heat treatment, or optionally of the succession of step b) of deposition, followed by step b') of maturation then by step c) of heat treatment.

[0045] Advantageously, step a) of the preparation method makes it possible to prepare at least one organic solution which comprises at least one metal precursor, preferably which comprises one or two metal precursor(s), and very particularly a metal precursor, comprising at least one metal element chosen from the elements of groups 3, 4 and 5 of the periodic table, that is to say at least one metal precursor of at least one metal element chosen from the elements of groups 3, 4 and 5 of the periodic table, preferably one or two, and very particularly one, metal precursor(s) of at least one element of group 3, group 4 and / or group 5. Preferably, the or each metal precursor comprises a metal element chosen from the elements of groups 3, 4 and 5 of the periodic table.The or each metallic precursor may optionally comprise another element chosen from the elements of a group of the periodic table other than those of groups 3, 4 and 5.

[0046] Said at least one metallic precursor of at least one metallic element chosen from the elements of group 3, group 4 and / or group 5 of the periodic table is advantageously a metallic precursor of at least one metallic element chosen in particular from yttrium (Y), zirconium (Zr), hafnium (Hf), niobium (Nb), tantalum (Ta), and mixtures thereof, preferably from zirconium (Zr), niobium (Nb), tantalum (Ta) and mixtures thereof, very preferably tantalum. According to a very preferred embodiment of the invention, said at least one metallic precursor is a metallic precursor of the element tantalum, optionally combined with a metallic precursor of the element niobium and / or a metallic precursor of the element zirconium.

[0047] Advantageously, a metal precursor of at least one metal element chosen from the elements of group 3, 4 and / or 5, for example a metal precursor of the element tantalum, is any compound comprising said at least one element respectively of group 3, 4 and / or 5, for example tantalum, and capable of releasing this element in solution in reactive form. The metal precursors used are thus organic or inorganic compounds comprising said metal element of group 3, 4 and / or 5, and which are advantageously soluble at least partially, preferably entirely, in the organic solvent, under the temperature and pressure conditions implemented during step a) and step b) of the preparation method.The organic or inorganic compounds are in particular chosen from the group consisting of halides, nitrates, sulfates, phosphates, hydroxides, carbonates, carboxylates, alcoholates, diketonates, amines, cyclopentadienyl, of said metal element from group 3, 4 and / or 5, and combinations of two or more thereof, more preferably chosen from the group consisting of chlorides, nitrates, carboxylates, alcoholates, diketonates, of said metal element from group 3, 4 and / or 5, and combinations of two or more thereof. The alcoholate type precursors have, for example, the formula M(0R)n where M is a metallic element from group n of the periodic table, n being an integer equal to 3, 4 or 5, preferably M is Ta or Nb or Zr, very preferably Ta, and R is a group chosen from alkyls such as ethyl, isopropyl, n-butyl, s-butyl, t-butyl groups.For example, preferred metal precursors of tantalum are tantalum pentachloride (TaCl5) and tantalum pentaethanoate (Ta(OEt)5 or Ta(OC2H5)5) which can be used with most organic solvents. The metal precursor of niobium can be selected from niobium pentachloride (NbCl5) and niobium pentaethanoate (Nb(OC2H5)5 or Nb(OEt)5). The metal precursor of zirconium can be selected from zirconium tetrachloride (ZrCl4) and zirconium tetraethanoate (Zr(OC2H5)4 or Zr(OEt)4). According to a very preferred embodiment of the invention, said at least one metallic precursor is tantalum pentachloride (TaCl5) or tantalum pentaethanoate (Ta(OC2H5)5 or Ta(OEt)5), optionally combined with a metallic precursor of the element niobium and / or with a metallic precursor of the element zirconium.

[0048] The organic solution prepared in step a) of the method according to the invention comprises, in addition to said at least one metallic precursor of at least one element from group 3, 4 and / or 5 of the periodic table, at least one acid additive and an organic solvent.

[0049] Said at least one acid additive may also optionally be called an acid compound. Said acid additive is advantageously a hydrogen halide, a hydrogen halide precursor or mixtures thereof.

[0050] As is well known, a hydrogen halide may be hydrogen fluoride, hydrogen chloride, hydrogen bromide or hydrogen iodide. Preferably, the hydrogen halide is chosen from hydrogen chloride, hydrogen bromide, hydrogen iodide and mixtures thereof. Preferably, the hydrogen halide is hydrogen chloride. It may, for example, be introduced into the organic solution by bubbling gaseous hydrogen halide into the organic solution, or into the organic solvent prior to step a); at least a portion of the gaseous hydrogen halide is then advantageously dissolved in the organic solvent.

[0051] According to the invention, a hydrogen halide precursor is advantageously a compound comprising at least one halide and in which said at least one halide is labile. The hydrogen halide precursor is therefore advantageously capable of releasing at least one halide ion which can react with the organic solvent to form a hydrogen halide. According to a particular embodiment, the hydrogen halide precursor is chosen from acyl halides (R-COHa, with Ha a halide, i.e., fluoride, chloride, bromide or iodide), alcohol hydrohalides (ROH-HHa, with Ha a halide, i.e., fluoride, chloride, bromide or iodide, and ROH said alcohol preferably chosen from methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tert-butanol and mixtures thereof), and mixtures thereof, very preferably acyl halides.Preferably, the hydrogen halide precursor is selected from formyl (or methanoyl) halides, acetyl (or ethanoyl) halides, propionyl (or propanoyl) halides, butyryl (or butanoyl) halides, methanol hydrohalides, ethanol hydrohalides, and mixtures thereof. Preferably, the hydrogen halide precursor is selected from formyl chloride, acetyl chloride, propionyl chloride, butyryl chloride, methanol hydrochloride, ethanol hydrochloride, propanol hydrochloride, isopropanol hydrochloride, and mixtures thereof. According to a preferred embodiment, the hydrogen halide precursor is acetyl chloride.

[0052] Preferably, the organic solution prepared in step a) comprises one or two acid additive(s) and preferably one acid additive, advantageously as defined in the present description above. Said organic solution may optionally comprise, in addition to said at least one acid additive, another additive, advantageously soluble in the organic solvent, chosen for example from hydroxyacids, ketoacids, their anhydrides, hydroxyesters, ketoesters (in par particularly beta-ketoesters), hydroxyketones, diketones (such as acetylacetone).

[0053] The organic solution comprises an organic solvent, preferably at least 5% by weight of organic solvent, or even at least 20% by weight of organic solvent, the percentages being given by weight of organic solvent relative to the total weight of the organic solution. Advantageously, the organic solvent of the organic solution prepared in step a) according to the invention comprises, preferably consists of, at least one organic compound and preferably an oxygenated organic compound (called oxygenated organic solvent). More particularly, the organic solvent is chosen from alcohols, carboxylic acids, ethers, esters, ketones and mixtures thereof.Preferably, the organic solvent comprises at least one alcohol, preferably at least 10% by weight (and up to 100% by weight), in particular at least 50% by weight (and up to 100% by weight), or even at least 90% by weight (and up to 100% by weight), of alcohol(s), the percentages being given relative to the total weight of organic solvent in the organic solution. The organic solvent may optionally comprise water. The alcohols which may be used as organic solvent are preferably monoalcohols having between 1 and 6 carbon atoms (i.e. C1-C6), preferably between 1 and 4 carbon atoms (i.e. C1-C4) and in particular having 1, 2, 3 or 4 carbon atoms, in particular linear, branched or cyclic, advantageously non-aromatic. The alcohols which can be used as organic solvent are for example chosen from methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tert-butanol and their mixtures.Preferably, the carboxylic acids which can be used as organic solvent are preferably carboxylic acids having between 2 and 4 carbon atoms (i.e. C2-C4), in particular linear, branched or cyclic, advantageously non-aromatic. The carboxylic acids which can be used as organic solvent are for example chosen from acetic acid, propionic acid, butyric acid. The ethers optionally used as organic solvent are preferably ethers of C4-C8 alcohols, in particular linear, branched or cyclic, advantageously non-aromatic, for example tetrahydrofuran (THF), diethyl ether, diisopropyl ether.The esters which can be used as organic solvent are preferably esters of C2-C6, preferably C2-C4, carboxylic acid and C1-C6, preferably C1-C4 alcohol, in particular linear, branched or cyclic, advantageously non-aromatic, such as methyl acetate, ethyl acetate, propyl acetate, isopropyl acetate, ethyl propanoate, ethyl acetoacetate. Preferably, the ketones optionally used as organic solvent are chosen from diketones, for example acetylacetone. For example, the organic solvent of the organic solution of . step a) comprises, preferably consists of, at least one organic compound chosen from methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tert-butanol, acetic acid, propionic acid, butyric acid, tetrahydrofuran (THF), diethyl ether, diisopropyl ether, methyl acetate, ethyl acetate, isopropyl acetate, ethyl propanoate, acetylacetone and mixtures thereof, in particular from methanol, ethanol, propanol, isopropanol, isobutanol, tert-butanol, acetic acid, propionic acid, diethyl ether, isopropyl acetate and mixtures thereof. According to a highly preferred embodiment, the organic solvent of the organic solution of step a) comprises, preferably consists of, methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tert-butanol or mixtures thereof, optionally mixed with acetic acid and / or propionic acid.In particular, the organic solvent comprises, preferably consists of, ethanol, isopropanol, and / or tert-butanol, optionally in admixture with acetic acid.

[0054] The metal precursor(s) of at least one element from group 3, 4 and / or 5 and the acid additive(s) are present in the organic solution in amounts such that the molar ratio (acid / metal) of the number of moles of acid equivalent (or hydrogen halide equivalent) provided by the acid additive(s) relative to the number of moles of the metal element(s), i.e. the total number of moles of elements from groups 3, 4 and 5 (for example the element tantalum), provided by the metal precursor(s) is greater than or equal to 1, preferably greater than or equal to 2, preferentially between 2 and 20, more preferably between 5 and 15. The number of moles of acid equivalent provided by the acid additive(s) is advantageously equal to the number of moles of halide provided by the acid additive(s) of the organic solution.According to particular embodiments, the number of moles of acid equivalent (or halide equivalent) is equal to the number of moles of acid additive(s) introduced into the organic solution, i.e. the number of moles of hydrogen halide and / or hydrogen halide precursor introduced into the organic solution, in which case the hydrogen halide precursor contains a single halide, per molecule; the molar ratio can then also be called additive / metal.

[0055] The metal precursor(s) and the acid additive(s) may be dissolved, diluted and / or in advantageously colloidal suspension, in the organic solvent of the organic solution prepared in step a). Whatever their form, the metal precursor(s) and the acid additive(s) are distributed uniformly in the organic solution at the end of step a). The organic solution may then be said to be homogeneous.

[0056] During step a), several organic solutions, for example two or three organic solutions, can be prepared. The organic solutions then prepared may each advantageously contain a metal precursor identical or different between said organic solutions, of an element from group 3, group 4 and / or group 5 identical or different between the organic solutions prepared, and at least one acid additive identical or different between them. In the case where several organic solutions are prepared, the method for preparing a catalyst advantageously comprises a step d) of repeating at least steps b) of deposition and c) of heat treatment, so as to bring each of the organic solutions prepared into contact at least once with the oxide matrix (or support).

[0057] Preferably, step a) of preparing the organic solution is carried out at a temperature between room temperature and 80°C, and at a pressure between atmospheric pressure and 3.0 MPa. Step a) of preparing the organic solution very advantageously comprises mixing said at least one metal precursor and said at least one acid additive with the organic solvent.

[0058] Step a) thus makes it possible to prepare at least one organic solution comprising at least one metallic precursor of at least one element from group 3, group 4 and / or group 5 of the periodic table, and at least one acid additive advantageously chosen from hydrogen halides, hydrogen halide precursors, and mixtures thereof, in an organic solvent which is preferably oxygenated and in particular comprising at least one alcohol.

[0059] Said organic solution obtained at the end of step a) can then be brought into contact with an oxide matrix to obtain a solid. This contacting step corresponds to step b) of the preparation method according to the invention which is a step of depositing said metal precursor(s) on said oxide matrix.

[0060] Said oxide matrix may also be called a support and is typically in the form of particles. Preferably, the oxide matrix comprises silica; said oxide matrix may then be called a silica-based oxide matrix. It preferably comprises at least 90% by weight (i.e. between 90% and 100% by weight), preferably at least 95% by weight (i.e. from 95% up to 100%), more preferably at least 98% by weight (i.e. from 98% up to 100%) and even more preferably at least 99.5% by weight (i.e. from 99.5% up to 100%) of silica relative to the total mass of oxide matrix. Said oxide matrix very advantageously comprises pores, in particular mesopores.The average pore diameter (or pore size) of the oxide matrix, in particular based on silica, is preferably at least 4 nm, preferably between 4.5 and 50 nm and even more preferably between 4.5 and 20 nm. Preferably, the pore volume of the oxide matrix, in particular based on silica, is in particular between 0.4 and 1.8 ml / g, and in particular between 0.5 and 1.5 ml / g. preferably, the oxide matrix has a specific surface area SBet of at least 250 m2 / g, preferably between 250 m2 / g and 700 m2 / g and even more preferably between 400 m2 / g and 600 m2 / g.

[0061] The above-mentioned textural parameters are determined by the analysis technique known as “Nitrogen Volumetry” which corresponds to the physical adsorption of nitrogen molecules in the porosity of the material via a progressive increase in pressure at constant temperature. According to the invention, the specific surface area in particular of the oxide matrix corresponds to the BET specific surface area (SBet in m2 / g) determined by nitrogen adsorption in accordance with the ASTM D 3663-78 standard established from the BRUNAUER-EMMETT-TELLER method described in the periodical “The Journal of American Society”, 1938, 60, 309. The representative pore distribution of a mesopore population is determined by the Barrett-Joyner-Halenda (BJH) model. The obtained nitrogen adsorption-desorption isotherm according to the BJH model is described in the periodical "The Journal of American Society", 1951, 73, 373, written by EP Barrett, LG Joyner and PP Halenda.The pore volume V is defined as the value corresponding to the volume observed for the partial pressure P / P°max of the nitrogen adsorption-desorption isotherm. The nitrogen adsorption volume is the volume measured for P / P°max = 0.99, the pressure for which it is assumed that nitrogen has filled all the pores. The diameter of the mesopores ¢) of the material tested, in particular of the oxide matrix, is determined by the formula 4000.V / SBEt- .

[0062] Optionally, the oxide matrix may be dried, prior to step b), for example in a fixed or circulating oven, at a temperature typically less than or equal to 500°C, more particularly between 100 and 300°C, or even between 100 and 250°C, for example for 1 to 24 hours, in particular for 2 to 16 hours. Advantageously, the oxide matrix which is brought into contact with the organic solution in step b) has a water content preferably less than or equal to 5% by weight, preferably less than or equal to 2.5% by weight, relative to the total weight of the oxide matrix. However, the oxide matrix may optionally comprise traces of water, for example at a content greater than or equal to 0.5% by weight, or even between 0.5 and 2.5% by weight, relative to the total weight of the oxide matrix.The presence of traces of water in the support does not seem to affect the quality of the heterogeneous catalyst obtained, in particular its catalytic performances, such as selectivity and productivity, especially during the reaction of converting a feedstock comprising ethanol into butadiene. Thus, as the requirement to work with dry materials is relaxed, handling constraints can be mitigated, for example: prior drying of the oxide matrix can be avoided or be lightened (for example, drying of the oxide matrix at 100°C for 2 hours may be sufficient; storage of the oxide matrix can be considered in particular without particular humidity conditions; . handling of the oxide matrix under dry atmosphere can be avoided; drying of the organic solvent is not necessary. Thus, the process according to the invention makes it possible to reduce energy consumption and the cost of the preparation process.

[0063] The oxide matrix, in particular based on silica, can be commercially available or synthesized to order using methods known to those skilled in the art. The oxide matrix, in particular based on silica, can be used directly in powder form or already shaped, in particular in the form of pelletized, crushed and sieved powder, beads, pellets, granules, or extrudates (hollow or non-hollow cylinders, multi-lobed cylinders with 2, 3, 4 or 5 lobes for example, twisted cylinders), or rings, etc., these shaping operations being carried out using conventional techniques known to those skilled in the art. For example, said oxide matrix, in particular based on silica, is in the form of balls or extrudates, optionally spheronized, preferably of a size between 0.5 and 10 mm, preferably between 1.0 and 5 mm.

[0064] The contacting in step b), i.e. the deposition of said at least one metal precursor on said oxide matrix, can be carried out by any methods known to those skilled in the art. For example, and in a non-exhaustive manner, the methods known as dry impregnation, excess impregnation, CVD (Chemical Vapor Deposition), CLD (Chemical Liquid Deposition), etc. can be used.For example, step b) of the method for preparing the catalyst according to the invention comprises, preferably consists of: bringing a volume of organic solution prepared in step a) into contact with the oxide matrix such that said volume of organic solution can correspond to the total or partial pore volume of said oxide matrix, and impregnating the organic solution on the surface of said oxide matrix, so as to ensure the dispersion of said at least one metal precursor over the entire surface of the oxide matrix. Very advantageously, the contacting and the impregnation are carried out at a temperature between room temperature and 80°C and at a pressure between atmospheric pressure and 3.0 MPa.

[0065] The deposition step b) may optionally be followed by a step b') of maturation of the solid obtained, so as to further promote the dispersion and distribution of said at least one metal precursor over the entire surface of the oxide matrix. For example, the maturation step may be carried out between room temperature and 80°C and at a pressure between atmospheric pressure and 3.0 MPa, for a duration of between 1 and 5 h, in particular for 2 hours.

[0066] The method for preparing the catalyst according to the invention also comprises a step c) of heat treatment of the solid obtained at the end of step b) of deposition or possibly from stage b') of maturation.

[0067] Preferably, step c) of heat treatment comprises, preferably consists of, drying or drying followed by calcination, preferably drying followed by calcination. The drying is very advantageously carried out at a temperature of between 50 and 200°C and preferably between 80 and 150°C, for a duration of between 1 and 24 hours, advantageously under a gas flow, preferably under an air flow, for example in an oven. The calcination, when carried out in step c) of the method for preparing the catalyst, is advantageously carried out under a gas flow, preferably under a gas flow comprising oxygen, for example under an air flow, at a temperature of between 350 and 700°C, preferably between 450 and 600°C, for a duration of between 1 and 6 h and preferably between 2 and 4 h.

[0068] Optionally, steps b) of deposition and c) of heat treatment, or optionally steps b), b') then c), may be repeated n times, n being an integer between 1 and 10, preferably between 1 and 5. Thus, the method of preparing the catalyst may comprise a step d) of repetition, for example in the case where the targeted catalyst comprises several metallic elements from group 3, group 4 and / or group 5, for example the element Nb and the element Ta or the element Ta and the element Zr; or so as to achieve the targeted content of the metallic element (or metallic elements) in the prepared catalyst; or in the case where several organic solutions are prepared in step a) as explained above in this description, etc.When the preparation method comprises a repetition step d), the organic solution is then brought into contact with the solid heat-treated in step c) during the first repetition, or with the solid heat-treated in the (il)th heat treatment step during the ith repetition, i being an integer between 2 and n. When it comprises a repetition step d), i.e. the repetition n times of steps b) and c), or possibly b), b') and c), the method for preparing the catalyst therefore comprises: .

[0069] - at least one step a) of preparing an organic solution (step a) can itself also be repeated if necessary);

[0070] - a deposition step b), possibly followed by a maturation step b'), then

[0071] - a step c) of heat treatment advantageously comprising drying or drying then calcination;

[0072] then n times the succession of: a step b) of deposition, optionally followed by a step b') of maturation, followed by a step c) of heat treatment advantageously comprising drying or drying then calcination, the last heat treatment (i.e. the nth heat treatment) preferably comprising drying followed by calcination.

[0073] The catalyst obtained at the end of step c) or optionally of step d), is a heterogeneous catalyst, comprising at least one metallic element from group 3, group 4 and / or group 5, deposited on a support (or oxide matrix) in particular based on silica.

[0074] The preparation method may optionally further comprise a step of shaping the catalyst obtained, optionally followed by a heat post-treatment, in particular in the case where the oxide matrix used in step b) is in the form of an unshaped powder. Thus, during this optional shaping step, at the end of step c) or optionally of step d), the catalyst may be shaped in the form of pelletized, crushed, sieved powder, beads, pellets, granules, or extrudates (hollow or non-hollow cylinders, multi-lobed cylinders with 2, 3, 4 or 5 lobes for example, twisted cylinders), or rings, etc., these shaping operations being carried out by conventional techniques known to those skilled in the art. Preferably, said catalyst is shaped in the form of extrudates of a size between 1 and 10 mm, optionally spheronized.During this optional shaping step, the catalyst may optionally be mixed with at least one porous oxide material acting as a binder so as to generate the appropriate physical properties of the catalyst (mechanical strength, attrition resistance, etc.). The porous oxide material, which acts as a binder, is preferably chosen from the group formed by silica, magnesia, clays (such as kaolinite, antigorite, chrysotile, montmorillonnite, beidellite, vermiculite, talc, hectorite, saponite, laponite), titanium oxide, titanates (for example zinc, nickel, cobalt titanates), lanthanum oxide, cerium oxide, boron phosphates and mixtures thereof.Very preferably, the binder used is of silicic nature and preferably at a content of between 5 and 60% by weight, and preferably between 10 and 30% by weight of binder relative to the total mass of the final shaped and optionally heat-post-treated catalyst. The heat post-treatment when carried out is of the same nature and follows the operating conditions of the heat treatment of step c).

[0075] The catalyst obtained at the end of step c) or optionally at the end of step d), or even at the end of the optional shaping step, comprises at least one metallic element chosen from the elements of group 3, group 4 and / or group 5, preferably from yttrium, zirconium, hafnium, niobium, tantalum, and mixtures thereof, preferentially from the element tantalum, the element niobium, the element zirconium and mixtures thereof, very preferentially the element tantalum, and preferably at a content of between 0.1 and 30% by weight, preferably between 0.3 and 10% by weight, preferably between 0.5 and 5% by weight of metallic element(s) relative to the weight of the oxide matrix.

[0076] Very advantageously, the catalyst obtained can be loaded into any type of catalytic reactor known to those skilled in the art, in particular a reactor in axial, radial mode or a tubular reactor, with or without heat exchange, with or without multiple injection.

[0077] The present invention thus also relates to the catalyst obtained by the preparation method according to the invention, which comprises at least one metallic element chosen from the group of elements of group 3, group 4 and group 5 of the periodic table, preferably chosen from yttrium, zirconium, hafnium, niobium, tantalum, and mixtures thereof, preferentially from the element tantalum, the element niobium, the element zirconium and mixtures thereof, very preferentially the element tantalum, and an oxide matrix, preferably based on silica. Preferably, said metallic element(s) is (are) present at a content of between 0.1 and 30% by weight, preferably between 0.3 and 10% by weight, preferably between 0.5 and 5% by weight of metallic element(s) relative to the weight of the oxide matrix.According to a highly preferred embodiment, the catalyst comprises a silica-based oxide matrix and between 0.5 and 5% by weight of tantalum relative to the weight of the oxide matrix. According to another embodiment, the catalyst comprises a silica-based oxide matrix and between 0.3 and 10% by weight, in particular between 0.5 and 5% by weight, of zirconium relative to the weight of the oxide matrix. According to another embodiment, the catalyst comprises a silica-based oxide matrix and between 0.3 and 10% by weight, in particular between 0.5 and 5% by weight, of niobium relative to the weight of the oxide matrix.

[0078] The method for preparing a catalyst, according to the invention, advantageously makes it possible to obtain, in a simple and inexpensive manner, a heterogeneous catalyst comprising at least one metallic element from group 3, group 4 and / or group 5, in particular the element Nb and / or Ta and / or Zr, very preferably the element Ta, having catalytic performances, in particular selectivity and productivity during the reaction for converting a feedstock comprising ethanol into butadiene, which are very satisfactory or even improved compared to the catalysts of the state of the art prepared by organic means. Such a preparation method can also possibly make it possible to ensure good dispersion of the metallic elements from group 3, group 4 and / or group 5 over the entire surface of the oxide matrix (i.e. good distribution of the metallic elements in the support particles).

[0079] The present invention also relates to the use for the conversion of a feedstock comprising at least ethanol into butadiene, of a catalyst obtained by the preparation method according to the invention, and which comprises at least one metallic element chosen from the group of elements of groups 3, 4 and / or 5 of the periodic table, of preferably among yttrium, zirconium, hafnium, niobium, tantalum, and mixtures thereof, preferably among the element tantalum, the element niobium, the element zirconium, and mixtures thereof, preferably the element tantalum, and an oxide matrix preferably based on silica, preferably at a content between 0.1 and 30% by weight, preferably between 0.3 and 10% by weight, preferably between 0.5 and 5% by weight of metallic element(s) relative to the weight of the oxide matrix. According to a preferred embodiment, the catalyst used comprises an oxide matrix based on silica and between 0.5 and 5% by weight of tantalum relative to the weight of the oxide matrix. The use of the catalyst obtained, for the conversion of a feedstock comprising at least ethanol into butadiene, then results in improvements in catalytic performance, particularly in terms of selectivity and productivity.The operating conditions for the conversion reaction are preferably a temperature between 250 and 450°C, preferably between 270°C and 380°C, preferentially between 300 and 360°C, a pressure between 0.05 and 2.00 MPa, preferably between 0.05 and 1.50 MPa, preferentially between 0.08 and 1.00 MPa, and preferably a space velocity between 0.2 and 10 h1, preferentially 0.5 and 5 h 1 and more preferably between 1 and 4 h *. The space velocity is defined as the ratio between the mass flow rate of feedstock and the mass of catalyst. When the treated feedstock also comprises acetaldehyde, the ethanol / acetaldehyde molar ratio is between 1 and 5, preferably between 2 and 4.

[0080] The present invention also relates, according to another aspect, to a process for converting into butadiene a feedstock comprising ethanol and optionally acetaldehyde, which comprises at least:

[0081] A) the preparation of a catalyst according to the preparation method according to the invention;

[0082] B) a step of converting the feedstock comprising ethanol, preferably ethanol and acetaldehyde, into butadiene, preferably in a molar ratio of ethanol to acetaldehyde of between 1 and 5, preferably between 2 and 4, the conversion step being carried out in the presence of the catalyst prepared in step A), and at a temperature of between 250 and 450°C, preferably between 270 and 380°C, preferably between 300 and 360°C, at a pressure of between 0.05 and 2.00 MPa, preferably between 0.05 and 1.50 MPa, preferably between 0.08 and 1.00 MPa, and preferably at a space velocity of between 0.2 and 10 h1, preferably between 0.5 and 5 h1, preferably between 1 and 4 h1.

[0083] When the feedstock comprises ethanol and acetaldehyde, the catalyst prepared in step A) very preferably comprises the element tantalum and a silica-based oxide matrix, the tantalum element content of the catalyst prepared in A) preferably being between 0.3 and 10%, and in particular between 0.5 and 5% by weight relative to the weight of the silica-based oxide matrix.

[0084] The following examples illustrate the invention, in particular particular embodiments of the invention, without limiting its scope. Examples

[0085] Catalysts are prepared as described in Examples 1 and 2. The catalysts are then tested: they are used to convert a feedstock comprising ethanol and acetaldehyde as described in Examples 3 and 4.

[0086] Example 1: Preparation of 3% Ta catalysts on silica dried at 100°C for 2 hours

[0087] Catalysts are prepared at 3% by weight of tantalum on silica beads (also called silicic support), the percentage of tantalum being given in weight of tantalum element relative to the weight of the silica beads. For each of the catalysts, the preparation method is as follows:

[0088] The silica support used for the impregnation step has the following characteristics:

[0089] [Tables 1] Characteristic Unit Value BET surface area m2 / g 450 Pore volume ml / g 1.0 Pore diameter nm 10.4 Average bead size* mm 2

[0090] (*: the average size of the balls corresponds to an average diameter in number of the silica beads.)

[0091] Before impregnation, the support is dried in an oven at 100°C for 2 hours.

[0092] In some cases, an acid additive, acetyl chloride (AcCl), is introduced into a volume Vsoivant of organic solvent (ethanol), to form an organic solution. In other cases (references), no additive is introduced into said volume of ethanol Vsoivant. The volume of organic solvent Vsoivant is proportional to the pore volume of the silicic support and equal to the total pore volume of the silicic support used.

[0093] A tantalum precursor, tantalum pentachloride (TaCl5) or tantalum pentaethanoate (Ta(OEt)5), is then introduced and diluted in a volume Vsovant of organic solvent (references) or in the organic solution containing the acid additive (acetyl chloride AcCl) at a concentration corresponding to a precise additive / Ta molar ratio (varying between 2.5 and 20). The organic solution is then homogenized with stirring.

[0094] The organic solution obtained is quickly added dropwise and mixed with the silica support until wettability of the surface of the latter is observed. (dry impregnation). The solid is then placed in an ethanol-saturated atmosphere for 3 hours. The solid is then dried at 100°C for 24 hours in an oven, then calcined in air at 550°C for 4 hours, to obtain a catalyst.

[0095] The prepared catalysts and the preparation parameters are presented in Table 2 in the case of the precursor Ta(OEt)5 and Table 3 in the case of the precursor TaCl5. The distribution coefficient of tantalum (also called distribution) in the silica beads is also presented in Tables 2 and 3.

[0096] The distribution coefficient of an element (in this case, the tantalum element) in a support particle (in this case, the silica bead) is calculated from a profile measured by Castaing microprobe and represents the ratio of the concentrations of the element (i.e. tantalum) at the heart of the support particle (in particular the silica bead) compared to the edge of this same support particle (cf. L. Sorbier, De-termining the Distribution of Metal by Electron Probe Micro Analysis, in: H. Toulhoat, P. Raybaud (Eds.), Catalysis by Transition Metal Sulphides, Ed. Technip, Paris, 2013, pp. 407-411 and references cited). A value of this coefficient close to 1 indicates a homogeneous distribution of the element in the support particle (i.e. of Ta in the silica bead); a value approaching 0 is significant of a distribution of the element on the surface of the support particle and called crust.

[0097] [Tables2] Catalyst According to the invention Metallic precursor Additive Additive / Ta (mol / mol) Solvent Distribution coefficient A no Ta(OEt)5 - 0 ethanol 0.45 + / - 0.02 B yes Ta(OEt)5 Acetyl chloride 2.5 ethanol 0.62 + / - 0.13 C yes Ta(OEt)5 Acetyl chloride 5 ethanol 0.59 + / - 0.11 D yes Ta(OEt)5 Acetyl chloride 10 ethanol 0.85 + / - 0.23 E yes Ta(OEt)5 Acetyl chloride 20 ethanol 0.73 + / - 0.19

[0098] [Tables3] Catalyst According to the invention Metallic precursor Additive Additive / Ta (mol / mol) Solvent Distribution coefficient F no TaCl5 - 0 ethanol 0.65+ / - 0.14 G yes TaCl5 Acetyl chloride 10 ethanol 0.81 + / - 0.21

[0099] It appears that the distribution of tantalum in the silica beads is more uniform when the catalyst is in accordance with the invention (catalysts B to E and catalyst G), that is to say prepared in the presence of an acid additive, acetyl chloride, whatever the metal precursor used (Ta(OEt)5 or TaCl5), compared to the corresponding reference catalyst (catalyst A or catalyst F), non-compliant prepared from the same metal precursor (Ta(OEt)5 or TaCl5) but without introducing an additive into the organic solution. Indeed, in the case of the metal precursor Ta(OEt)5, the distribution coefficients measured for the compliant catalysts B, C, D, E, vary between 0.59 + / - 0.11 and 0.85 + / - 0.23 whereas the distribution coefficient of the reference catalyst A (non-compliant) is measured equal to 0.45 + / - 0.02.In the case of the metallic precursor TaCl5, the distribution coefficient measured for the compliant catalyst G is 0.81 + / - 0.21 while the distribution coefficient of the reference catalyst F (non-compliant) is measured equal to 0.65 + / - 0.14.

[0100] Example 2: Preparation of 3% Ta catalysts on dried silica at different temperatures for durations between 2 and 16 hours

[0101] Catalysts are prepared at 3% by weight of tantalum on silica beads (also called silicic support), the percentage of tantalum being given in weight of tantalum element relative to the weight of the silica beads. The silica beads used are the same, i.e. having the same characteristics, as those used for the catalysts prepared according to Example 1 (see Table 1).

[0102] However, before impregnation, the silica beads are dried in an oven at different temperatures between 100°C and 500°C and for durations ranging from 2 hours to 16 hours. The residual water content of the silica beads is determined after drying on a 50 g sample (see Table 4 - content given as a percentage by weight of water relative to the total weight of the silica beads). They are then stored overnight in a dry atmosphere before being used for impregnation.

[0103] The same impregnation and heat treatment protocol as described in Example 1 is followed. The tantalum precursor used to prepare the catalysts according to Example 2 is tantalum pentaethanoate (Ta(OEt)5). The organic solvent is ethanol and the acid additive used is acetyl chloride (AcCl) at a molar ratio to tantalum, in the organic solution, of 10.

[0104] The prepared catalysts and the preparation parameters are presented in Table 4. The distribution coefficient of tantalum (also called distribution) in the silica beads is also presented in Table 4 for the prepared catalysts. The distribution coefficient is measured as explained in Example 1.

[0105] [Tables4] Catalyst According to the invention Drying protocol Residual water content of silica beads (% weight) Additive Additive / T a (mol / mol) Distribution coefficient A no 2h at 100°C 1.6% - 0 0.45 + / - 0.02 D yes 2h at 100°C 1.6% AcCl 10 0.85 + / - 0.23 H yes 16h at 100°C 0.5% AcCl 10 0.96 + / - 0.03 I no 16h at 150°C 0.2% - 0 0.41 + / - 0.01 J yes 16h at 150°C 0.2% AcCl 10 0.94 + / - 0.01 K no 4h at 250°C 0.1% - 0 0.56 + / - 0.09 L yes 4h at 250°C 0.1% AcCl 10 0.96 + / - 0.05 M yes 4h at 350°C <0.1% AcCl 10 nd* N yes 4h at 450°C <0.1% AcCl 10 nd* O yes 4h at 500°C <0.1% AcCl 10 0.93+ / - 0.15

[0106] * nd = not determined

[0107] The distribution of tantalum in the silica beads is more uniform in the case of catalysts D, H, J, L, M, N, O, in accordance with the invention, prepared in the presence of acetyl chloride AcCl in the organic solution, compared to catalysts A, I, K, not in accordance with the invention, prepared without additive. Indeed, the distribution coefficient of tantalum in the dried silica beads is at least 0.85 when the organic solution comprises the acid additive acetyl chloride AcCl. On the contrary, the distribution coefficient does not exceed 0.56 when the catalyst is not in accordance, prepared without additive, even if the silica is dried extensively, i.e. for 16 hours at 150°C or for 4 hours at 250°C.

[0108] Furthermore, the distribution coefficient seems to have a tendency to increase and approach more closely 1, when the support undergoes increasingly intensive drying prior to impregnation.

[0109] Example 3: Use of the catalysts prepared according to Example 1 to convert an ethanol-acetaldehyde feedstock into butadiene

[0110] Description of the catalytic test unit

[0111] The reactor used consists of a 20 cm long, 10 mm diameter stainless steel tube. The reactor is first charged with carborundum, then with the catalyst diluted in carborundum and finally with carborundum. Carborundum is inert to the charge and does not affect the catalytic results; it allows the catalyst to be positioned in the isothermal zone of the reactor and to limit the risks of heat and material transfer problems; the temperature of the reactor is controlled with a tube furnace with three heating zones.

[0112] The liquid feed (mixture of ethanol and acetaldehyde) is injected via a double piston HPLC pump. The liquid stream is vaporized in the lines heated by a tracer before entering the reactor and is homogenized by passing through a static mixer.

[0113] At the reactor outlet, the products formed during the reaction are kept in the vapor phase to be analyzed online by gas chromatography (PONA capillary column) to allow the most precise identification of the hundreds of products formed. The catalyst is activated in situ under nitrogen at the test temperature.

[0114] For each test, the Ethanol / Acetaldehyde ratio of the feed is set at 2.6 (mol / mol), the temperature at 350°C and the pressure at 0.15 MPa.

[0115] For each catalyst tested, the carbon productivity value is measured at iso-feed rate (constant pph of 250g / gTa / h, i.e. a space velocity of 7.5 h1) while the butadiene selectivity measurement is determined at iso-conversion (feed conversion at 40%). The carbon productivity (which is generally expressed in % weight / weight per hour) corresponds to the mass flow rate of butadiene (in g / h), measured at the reactor outlet, per unit mass of element Ta, for a pph of the feed of 250 g / gTa / h. The butadiene selectivity (which is expressed in % weight / weight) measured is a carbon selectivity and corresponds to the butadiene flow rate measured at the reactor outlet relative to the sum of the flow rates of the carbonaceous products formed (unconverted ethanol and acetaldehyde are not taken into account in the calculation of the selectivity).

[0116] The results obtained in terms of butadiene selectivity and carbon productivity, with catalysts A to E and F to G prepared as described in Example 1 are presented in Tables 5 and 6, in the form of gain in butadiene selectivity compared to the reference catalyst A or F (i.e. gain in selectivity = [selectivity obtained with the catalyst] - [selectivity obtained with the corresponding reference catalyst], expressed in points or % weight / weight) and in the form of a gain in carbon productivity expressed relative to the productivity measured for the corresponding reference catalyst A or F (i.e. gain in productivity = ([productivity obtained with the catalyst] - [productivity obtained with the corresponding reference catalyst]) / [productivity obtained with the corresponding reference catalyst], expressed in % weight / weight).

[0117] [Tables5] Catalyst tested according to the invention additive additive / Ta solvent Selectivity gain (% w / w) Productivity gain (%) A no ___ 0 ethanol - - B yes Acetyl chloride 2.5 ethanol + 2.8 + 25% C yes Acetyl chloride 5 ethanol + 3.5 + 32% D yes Acetyl chloride 10 ethanol + 4.2 + 29% E yes Acetyl chloride 20 ethanol + 4.2 + 36%

[0118] [Tableauxô] Catalyst tested according to the invention additive additive / Ta solvent Selectivity gain (% weight / weight) Productivity gain (%) F no ___ 0 ethanol - - G yes Acetyl chloride 10 ethanol + 3.7 + 42%

[0119] It appears that whatever the metal precursor (TaCl5 and Ta(OEt)5) used to prepare the catalyst, the presence of an additive of the hydrogen chloride type (HCl or acetyl chloride) in the organic impregnation solution, even in small quantities (for example even for an additive / Ta molar ratio of 2.5) makes it possible to improve the catalytic performances of the compliant catalysts, compared to the reference catalysts (A and F), prepared without additive in the organic solution.

[0120] Example 4: Use of the catalysts prepared according to Example 2 to convert an ethanol-acetaldehyde feedstock into butadiene

[0121] Catalysts A, D and H to O prepared as described in Example 2 are tested on the catalytic test unit described above in Example 3, under the same conditions, to convert a feedstock comprising ethanol and acetaldehyde (Ethanol / Acetaldehyde molar ratio of 2.6).

[0122] The results obtained in terms of butadiene selectivity and carbon productivity, with catalysts A, D and H to O prepared as described in Example 2, are presented in Table 7. The results are given in the form of gain in butadiene selectivity compared to the reference catalyst A (i.e. gain in selectivity = [selectivity obtained with the catalyst] - [selectivity obtained with the reference catalyst A], expressed in points or % weight / weight) and in the form of gain in carbon productivity expressed relative to the productivity measured for the reference catalyst A (i.e. gain in productivity = ([productivity obtained with the catalyst] - [productivity obtained with the reference catalyst A]) / [productivity obtained with the reference catalyst A], expressed in % weight / weight).

[0123] [Tables?] Catalyst according to the invention Drying protocol Additive Additive / Ta (mol / mol) Selectivity gain (% w / w) Productivity gain (%) A no 2h at 100°C - 0 - - D yes 2h at 100°C AcCl 10 + 4.2 + 29% H yes 16h at 100°C AcCl 10 + 4.2 + 32% I no 16h at 150°C - 0 + 3.2 + 25% J yes 16h at 150°C AcCl 10 + 4.2 + 29% K no 4h at 250°C - 0 + 4.2 + 29% L yes 4h at 250°C AcCl 10 + 4.4 + 36% M yes 4h at 350°C AcCl 10 + 3.8 + 36% N yes 4h at 450°C AcCl 10 + 3.7 + 32% O yes 4h at 500°C AcCl 10 + 3.3 + 39%

[0124] Table 7 shows that butadiene selectivity and carbon productivity measured during the conversion of an ethanol-acetaldehyde feedstock into butadiene are improved in the case of catalysts in accordance with the invention, prepared in the presence of the acetyl chloride additive and regardless of the silica drying protocol, compared to the reference catalyst A, non-compliant, prepared without additive and with a silica support dried for 2 hours at 100°C. Indeed, the selectivity gains of the compliant catalysts D, J, L, M, N, O vary between +3.3 points (catalyst O, prepared with silica dried for 4 hours at 500°C) and +4.2 points (catalysts D, H, J, prepared with silica beads dried for 2 or 16 hours at 100°C or 16 hours at 150°C), or even +4.4 points (catalyst L, prepared with silica dried for 4 hours at 250°C), compared to the selectivity achieved with the non-compliant catalyst A and prepared without additive with silica dried for 2 hours at 100°C.At the same time, the productivity gains obtained with compliant catalysts vary between +29% (catalysts D and J) and +39% (catalyst O), relative to the productivity measured for non-compliant catalyst A.

[0125] It also appears that, for the same silica drying protocol, catalysts D, J and L, compliant, prepared with an acid additive and with silicas dried respectively for 2 hours at 100°C, 16 hours at 150°C and 4 hours at 250°C, make it possible to achieve butadiene selectivities and carbon productivity, improved compared respectively to catalysts A, I and K, non-compliant, prepared without additive and with silicas dried respectively for 2 hours at 100°C, 16 hours at 150°C and 4 hours at 250°C.

[0126] Table 7 also shows that the silica drying protocol, up to a drying temperature of 250°C, does not appear to have any effect on selectivity; indeed, the selectivity gains of catalysts D, H, J, L, compliant (drying temperature varying between 100 and 250°C) are + 4.2 points for catalysts D, H, J, and + 4.4 points for catalyst L. Beyond a silica drying temperature of 250°C, i.e. at 350°C, 450°C and 500°C, the selectivity gains tend to decrease slightly and are only +3.8 points, +3.7 points and +3.3 points respectively. Thus, gentle drying, 2 hours at 100°C, of ​​the silica prior to impregnation with an organic solution in accordance with the invention seems sufficient to achieve optimized selectivity, thus limiting handling constraints and inducing limited energy consumption and production costs for the catalysts.

Claims

Claims

1. A method for preparing a catalyst, comprising: a) a step of preparing at least one organic solution comprising: at least one metal precursor of at least one element selected from the elements of groups 3, 4 and 5 of the periodic table, at least one acid additive selected from hydrogen halides, hydrogen halide precursors, and mixtures thereof, and an organic solvent, said at least one metal precursor and said at least one acid additive being present in the organic solution in amounts such that the acid / metal molar ratio between the number of moles of hydrogen halide equivalent and the number of moles of the metal element(s) provided by said at least one metal precursor is greater than or equal to 1;b) a step of depositing said at least one metallic precursor on an oxide matrix, by bringing the organic solution prepared in step a) into contact with said oxide matrix, to obtain a solid; c) a step of heat treatment of the solid obtained at the end of step b).;

2. Method according to claim 1, wherein the metallic element is chosen from yttrium, zirconium, hafnium, niobium, tantalum and mixtures thereof, preferably from tantalum, niobium, zirconium and mixtures thereof, preferentially the element tantalum.

3. Method according to claim 1 or 2, wherein the hydrogen halide is selected from hydrogen chloride, hydrogen bromide, hydrogen iodide and mixtures thereof, preferably hydrogen chloride.

4. Method according to one of claims 1 to 3, in which the hydrogen halide precursor is chosen from acyl halides, alcohol hydrohalides, and mixtures thereof, preferentially from formyl chloride, acetyl chloride, propionyl chloride, butyryl chloride, methanol hydrochloride, ethanol hydrochloride, propanol hydrochloride, isopropanol hydrochloride, and mixtures thereof, the hydrogen halide precursor being very preferably acetyl chloride.

5. Method according to one of claims 1 to 4, in which the ratio molar acid / metal in step a) is greater than or equal to 2, preferably between 2 and 20, more preferably between 5 and 15.

6. Method according to one of claims 1 to 5, in which the organic solvent comprises at least one organic compound chosen from alcohols, carboxylic acids, ethers, esters, ketones and mixtures thereof, preferably chosen from methanol, ethanol, propanol, isopropanol, butanol, isobutanol, tert-butanol, acetic acid, propionic acid, butyric acid, tetrahydrofuran (THF), diethyl ether, diisopropyl ether, methyl acetate, ethyl acetate, isopropyl acetate, ethyl propanoate, acetylacetone and mixtures thereof, in particular from methanol, ethanol, propanol, isopropanol, isobutanol, tert-butanol, acetic acid, propionic acid, diethyl ether, isopropyl acetate and mixtures thereof.

7. Method according to one of claims 1 to 6, in which the oxide matrix comprises silica, preferably at least 90% by weight of silica relative to the total mass of the oxide matrix.

8. Method according to one of claims 1 to 7, in which step c) of heat treatment comprises drying, the drying preferably being carried out at a temperature between 50 and 200°C for a duration between 1 and 24 hours, preferably under a gas flow.

9. Method according to claim 8, in which step c) of heat treatment comprises calcination following said drying, the calcination being carried out under gas flow, at a temperature between 350 and 700°C, for a duration between 1 and 6 h.

10. Catalyst obtained by the preparation method according to one of claims 1 to 9, which comprises at least one metallic element chosen from the group of elements of groups 3, 4 and 5 of the periodic table, preferably chosen from yttrium, zirconium, hafnium, niobium, tantalum and their mixtures, preferentially from the element tantalum, the element niobium and / or the element zirconium, very preferably the element tantalum, and an oxide matrix preferably based on silica.

11. Catalyst according to claim 10, wherein said at least one metallic element is present at a content of between 0.1 and 30% by weight, preferably between 0.3 and 10% by weight, more preferably between 0.5 and 5% by weight of metallic element(s) relative to the weight of the oxide matrix.

12. Use of the catalyst according to claim 10 or 11 for converting a feedstock comprising ethanol into butadiene, at a temperature between 250 and 450°C, at a pressure between 0.05 and 2.00 MPa.

13. Process for converting a feedstock comprising ethanol into butadiene, which comprises: A) the preparation of a catalyst according to the preparation method according to one of claims 1 to 9; B) a step of converting the feedstock comprising ethanol into butadiene, carried out in the presence of the catalyst prepared in step A), at a temperature of between 250 and 450°C, at a pressure of between 0.05 and 2.00 MPa.

14. Conversion process according to claim 13, wherein the feed comprises ethanol and acetaldehyde, preferably in a molar ratio of ethanol to acetaldehyde of between 1 and 5.