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    • 专利摘要:
    The present invention relates to a hydrotreating catalyst comprising a support based on alumina, at least one group VIB metal, at least one group VIII metal and phosphorus in which: the specific surface area of the catalyst is between 20 and 150 m2 / g; The group VIB metal density, expressed as the number of Group VIB metal atoms per unit area of the catalyst, is between 7 and 30 Group VIB metal atoms per nm 2 of catalyst; the catalyst being prepared by impregnating the Group VIB, Group VIII and phosphorus metals on the support so as to obtain an impregnated catalytic precursor and then drying said impregnated catalytic precursor at a temperature below 200 ° C and without subsequent calcination.
    公开号:FR3023184A1
    申请号:FR1456464
    申请日:2014-07-04
    公开日:2016-01-08
    发明作者:Antoine Daudin
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a hydrotreating catalyst and a process for preparing said catalyst useful for the hydrodesulfurization of a petroleum fraction, in particular a petrol fraction. The invention also relates to a hydrodesulphurization process of a petrol fraction using a catalyst according to the invention. State of the art Oil refining and petrochemicals are now subject to new constraints. Indeed, all countries are gradually adopting severe sulfur specifications, the objective being to achieve, for example, 10 ppm (wt) of sulfur in commercial species in Europe and Japan. The problem of reduction of sulfur contents is essentially concentrated on the species obtained by cracking, whether catalytic (FCC Fluid Catalytic Cracking according to the English terminology) or non-catalytic (coking, visbreaking, steam cracking), main sulfur precursors. in the gasoline pools. One solution, well known to those skilled in the art, for reducing the sulfur content is to hydrotreat (or hydrodesulphurize) the hydrocarbon cuts (including catalytic cracking gasolines) in the presence of hydrogen and a heterogeneous catalyst . However, this process has the major disadvantage of causing a very significant drop in the octane number if the catalyst used is not selective enough. This reduction in the octane number is notably related to the hydrogenation of the olefins present in this type of gasoline concomitantly with hydrodesulfurization. Unlike other hydrotreatment processes, the hydrodesulfurization of gasolines must therefore make it possible to respond to a double antagonistic constraint: to ensure a deep hydrodesulfurization of the species and to limit the hydrogenation of the unsaturated compounds present. Thus, US Pat. No. 5,318,690 proposes a process consisting in fractionating gasoline, softening the light fraction and hydrotraying the heavy fraction on a conventional catalyst and then treating it on a ZSM5 zeolite to approximately recover the initial octane number. .
    [0002] The patent application WO 01/40409 claims the treatment of an FCC gasoline under conditions of high temperature, low pressure and high hydrogen / charge ratio. Under these particular conditions, the recombination reactions leading to mercaptan formation, involving the H2S formed by the desulfurization reaction and the olefins are minimized.
    [0003] Finally, US Pat. No. 5,968,346 proposes a scheme making it possible to achieve very low residual sulfur contents by a multi-step process: hydrodesulphurization on a first catalyst, separation of the liquid and gaseous fractions, and second hydrotreatment on a second catalyst. The liquid / gas separation makes it possible to eliminate the H2S formed in the first reactor, in order to achieve a better compromise between hydrodesulfurization and octane loss. Another way to address the dual problem mentioned above is to employ hydrodesulfurization catalysts both active in hydrodesulphurization but also very selective in hydrodesulphurization with respect to the hydrogenation reaction of olefins. Thus known in the state of the art the document US 2009/321320 which discloses hydrodesulphurization catalysts which comprise a cobalt / molybdenum active metal phase and a high-temperature alumina-based support, that is to say calcined at a temperature above 800 ° C, and with a specific surface area of 40 to 200 m 2 / g. The catalysts are obtained by dry impregnation of an aqueous solution containing cobalt, molybdenum and at least one additive in the form of an organic compound. EP 1892039 discloses selective hydrodesulphurization catalysts comprising at least one carrier, at least one group VIII element, at least one group VIB element and phosphorus in which the group VIB element density per unit area of the support is between 2.10-4 and 18.10-4g of Group VIB element oxides per m 2 of support, in which the group VI phosphorus molar ratio is between 0.27 and 2, in which the Group VIB elements are between 1 and 20% by weight of Group VIB element oxides and in which the carrier has a specific surface area of less than 135 m 2 / g. Diesel hydrotreating catalysts comprising a support, at least one Group VIB metal associated with at least one Group VIII metal, having a specific surface area of between 200 and 300 m 2 / g and thus a metal density of group VIB per unit area, expressed as the number of Group VIB metal atoms per 30 nm 2 of catalyst, less than 7. Thus, there is still a great deal of interest in refiners for hydrodesulphurisation catalysts, especially for slices which have improved catalytic performance, especially in terms of catalytic activity in hydrodesulfurization and / or selectivity and which, once used, make it possible to produce a gasoline with a low sulfur content without a severe reduction in the octane number. . SUMMARY OF THE INVENTION The invention therefore relates to a hydrotreatment catalyst comprising a support based on alumina, at least one group VIB metal, at least one group VIII metal and phosphorus in which: the specific surface of the catalyst is between 20 and 150 m 2 / g; the group VIB metal density, expressed as the number of Group VIB metal atoms per unit area of the catalyst, is between 7 and 30 Group VIB metal atoms per nm 2 of catalyst; the catalyst being prepared by impregnating the Group VIB, Group VIII and phosphorus metals on the support so as to obtain an impregnated catalytic precursor and then drying said impregnated catalytic precursor at a temperature below 200 ° C and without subsequent calcination. The group VIB metal content is generally between 3 and 35% by weight of oxide of said group VIB metal relative to the total weight of the catalyst; The metal content of group VIII is generally between 0.1 and 10% by weight of oxide of said group VIII metal relative to the total weight of the catalyst; The phosphorus content is generally between 0.3 and 10% by weight of P2O5 relative to the total weight of the catalyst. Preferably, the molar ratio (Group VIII metal) / (Group VIB metal) is between 0.1 and 0.8 and the phosphorus / (Group VIB metal) molar ratio is between 0.1 and 0.7. The catalyst according to the invention preferably has a specific surface area of between 30 and 120 m 2 / g, preferably between 40 and 95 m 2 / g and very preferably between 50 and 90 m 2 / g. Preferably, the group VIB metal density is between 7 and 25 Group VIB metal atoms per nm 2 of catalyst, preferably between 7 and 20 Group VIB metal atoms per nm 2 of catalyst, preferably between 7 and 15 Group VIB metal atoms per nm 2 of catalyst.
    [0004] The Group VIB metal is selected from tungsten and molybdenum and the Group VIII metal is selected from nickel and cobalt.
    [0005] In a preferred embodiment, the Group VIB metal is molybdenum and the Group VIII metal is cobalt. In the context of the invention, the support based on alumina of the catalyst is obtained from alumina gel kneaded, shaped and calcined.
    [0006] According to the invention, the catalyst may further comprise at least one organic compound containing oxygen and / or nitrogen. The organic compound may be selected from carboxylic acid, alcohol, aldehyde, ester, amine, amino carboxylic acid, amino alcohol, nitrile and amide.
    [0007] For example the organic compound is chosen from ethylene glycol, triethylene glycol, glycerol, polyethylene glycol having a molecular weight of 150 to 1500, acetophenone, 2,4-pentanedione, pentanole, acetic acid , maleic acid, oxalic acid, tartaric acid, formic acid, citric acid, C1-04 dialkyl succinate, a cyclic oligosaccharide composed of at least 6 α-linked glucopyranose units -4), ethylene diamine, tetramethylurea, aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, monoethanolamine, acetonitrile, N-methylpyrrolidone, dimethylformamide and ethylene diamine tetraacetic acid. The invention also relates to a process for preparing the catalyst according to the invention, which comprises the following steps: a) one deposits on alumina support by one or more impregnations the metals of group VIII, group VIB and phosphorus so as to obtain an impregnated catalytic precursor; b) the impregnated precursor is dried at a temperature below 200 ° C without subsequent calcination so as to provide a dried catalyst. The catalyst according to the invention when it further comprises an organic additive, is prepared according to a process which comprises the following steps: i) is deposited on a support based on alumina by one or more impregnations group VIII metals, group VIB, phosphorus and at least one organic compound containing oxygen and / or nitrogen so as to obtain an impregnated catalytic precursor; ii) the impregnated precursor is dried at a temperature below 200 ° C without subsequent calcination so as to provide a dried catalyst. According to the invention, step i) may comprise the following successive steps: i1) an alumina support is impregnated with at least one solution containing at least one Group VIB metal, at least one Group VIII metal and phosphorus to obtain an impregnated support, i2) the impregnated support obtained in step II) is dried at a temperature below 200 ° C without subsequent calcination to obtain a dried catalyst, i3) the dried catalyst obtained in the stage is impregnated i2) by an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an additivated catalyst precursor, i4) optionally allowing the additive-treated catalyst precursor obtained to step i3). Finally, the subject of the invention is also a process for the hydrodesulfurization of a petrol cut in which said petrol cut, hydrogen and a catalyst according to the invention or prepared according to one of the processes been sulphured. The placing in contact is carried out at: a temperature of between 200 and 400 ° C .; a total pressure of between 1 and 3 MPa; a Hourly Volumetric Velocity, defined as the volume flow rate of charge relative to the catalyst volume, of between 1 and 10 h -1; a hydrogen volume / gasoline charge ratio of between 100 and 600 Nl / l. The gasoline that is treated by the hydrodesulfurization process is preferably a gasoline from a catalytic cracking unit. DETAILED DESCRIPTION OF THE INVENTION The Applicant has thus discovered a hydrotreatment catalyst comprising a support based on alumina and metals of groups VIB and VIII of the periodic table of elements and phosphorus which, after sulphurization, not only has an activity improved hydrodesulphurization but also a high selectivity in hydrodesulfurization relative to the hydrogenation reaction of olefins. According to a first aspect, the invention relates to a hydrotreatment catalyst comprising a support based on alumina, at least one Group VIB metal, at least one Group VIII metal and phosphorus, in which: specific surface of the catalyst is between 20 and 150 m 2 / g; the group VIB metal density, expressed as the number of Group VIB metal atoms per unit area of the catalyst, is between 7 and 30 Group VIB metal atoms per nm 2 of catalyst; the catalyst being prepared by impregnating the Group VIB, Group VIII and phosphorus metals on the support so as to obtain an impregnated catalytic precursor and then drying said impregnated catalytic precursor at a temperature below 200 ° C and without subsequent calcination. According to the invention, the group VIB metal density, expressed as the number of Group VIB metal atoms per unit area of the catalyst (number of Group VIB metal atoms per nm 2 of catalyst) is calculated, for example from the following relationship: d (Group VIB metal) = (X x NA) (100 x 1018 x S x MM) with: - X = wt% of Group VIB metal; - NA = Avogadro number equal to 6,022,1023; S = Specific surface area of the catalyst (m 2 / g), measured according to ASTM D3663; MM = Molar mass of the Group VIB metal (for example 95.94 g / mol for molybdenum). Surprisingly, the inventors have established that a catalyst having the characteristics mentioned above and prepared by impregnation of Group VIB and VIII metals and phosphorus and then only dried at a temperature below 200 ° C. without subsequently undergoing a step The calcination has a high activity in hydrodesulfurization while being more selective with respect to the hydrogenation reaction of the olefins. The gain in activity makes it possible to reduce the temperature of the reactor to reach the same desulphurization rate with the advantage of limiting the deactivation phenomena due for example to the coking of the catalyst and thus to keeping the unit in service for an additional duration, compared to the performances obtained in the presence of hydrodesulfurization catalysts (HDS) of the state of the art. Furthermore, the catalyst according to the invention demonstrates a selectivity in hydrodesulphurization with respect to the hydrogenation of olefins which is improved thereby conferring on it an advantageous property in the context of the hydrotreatment of gasoline-type hydrocarbon cuts (c '). that is, having a boiling temperature generally between 30 ° C and 250 ° C) containing olefins where it is desired to minimize the hydrogenation reaction of the olefins in order to limit the loss of octane of the treated gasoline. The catalyst according to the invention thus comprises a support on which is deposited an active metal phase. The support is a porous solid based on alumina, that is to say it contains alumina and optionally metals and / or dopants which have been introduced outside the impregnation stage. metals of the active phase. For example metals and / or dopants were introduced during the preparation (kneading, peptization) of the support or during its shaping. Preferably, the support is made of alumina. Preferably, the alumina is a delta, gamma or theta alumina, alone or as a mixture. The pore volume of the alumina support is generally between 0.4 cm3 / g and 1.3 cm3 / g, preferably between 0.6 cm3 / g and 1.1 cm3 / g. The total pore volume is measured by mercury porosimetry according to ASTM D4284 with a wetting angle of 140 °, as described in Rouquerol F .; Rouquerol J .; Singh K. "Adsorption by Powders & Porous Solids: Principle, methodology and applications", Academic Press, 1999, for example by means of an Autopore IIITM model apparatus of the Microméritics ™ brand. The specific surface of the alumina support is generally between 20 m 2 / g and 200 m 2 / g, preferably between 20 m 2 / g and 180 m 2 / g, more preferably between 30 m 2 / g and 170 m 2 / g. The specific surface is determined in the present invention by the B.E.T. method according to ASTM D3663, a method described in the same work cited above. The alumina support is advantageously in the form of powder or in the form of balls, extrudates, pellets, or irregular and non-spherical agglomerates, the specific shape of which may result from a crushing step.
    [0008] According to a preferred embodiment, the catalyst according to the invention comprises an alumina support which is obtained from an alumina gel (or alumina gel) which essentially comprises a precursor of the oxy (hydroxide) aluminum type (A10 (OH)) - also referred to as boehmite. The alumina gel (or otherwise known as boehmite gel) can be synthesized by precipitation of basic solutions and / or acid salts of aluminum induced by pH change or any other method known to those skilled in the art (P. Euzen , P. Raybaud, X. Krokidis, H. Touihoat, JL Le Loarer, JP Jolivet, C. Froidefond, Alumina, Handbook of Porous Solids, Eds F. Schüth, Sing KSW, J. Weitkamp, Wiley-VCH, Weinheim, Germany, 2002, pp. 1591-1677).
    [0009] Generally the precipitation reaction is carried out at a temperature between 5 ° C and 80 ° C and at a pH between 6 and 10. Preferably the temperature is between 35 ° C and 70 ° C and the pH is between 6 and 10. According to one embodiment, the gel alumina is obtained by contacting an aqueous solution of an acidic aluminum salt with a basic solution. For example, the acid salt of aluminum is selected from the group consisting of aluminum sulphate, aluminum nitrate or aluminum chloride. Preferably, said acid salt is aluminum sulphate. The basic solution is preferably chosen from sodium hydroxide or potassium hydroxide. Alternatively, an alkaline solution of aluminum salts may be contacted which may be selected from the group consisting of sodium aluminate and potassium aluminate with an acidic solution. In a very preferred variant, the gel is obtained by contacting a solution of sodium aluminate with nitric acid. The sodium aluminate solution advantageously has a concentration of between 10-5 and 10-1 mol.L-1 and preferably this concentration is between 10-4 and 10-2 mol.L-1. According to another embodiment, the gel alumina is obtained by contacting an aqueous solution of acid salts of aluminum with an alkaline solution of aluminum salts. The alumina gel obtained after the precipitation step is then subjected to a kneading step, preferably in an acidic medium. The acid used can be, for example, nitric acid. This step is carried out by means of known tools such as Z-arm kneaders, grinders, continuous mono or bi-screws allowing the transformation of the gel into a product having the consistency of a paste. According to an advantageous embodiment, one or more compounds known as "porogenic agents" are added to the mixing medium. These compounds have the property of degrading by heating and thus create a porosity in the support. For example, wood powders, charcoal, tars, plastics can be used as pore-forming compounds. The paste thus obtained after kneading is for example passed through an extrusion die when it is desired to obtain a support in the form of an extrusion. Generally, the extrudates have a diameter of between 0.4 and 100 mm, preferably between 0.5 and 100 mm, more preferably between 0.5 and 10 mm and even more preferably between 0.4 and 4 mm. These extrusions may be cylindrical, multilobed (for example trilobed or quadrilobed). After shaping, the carrier is optionally dried before undergoing heat treatment. For example, the drying is carried out at a temperature between 100 and 200 ° C. The dried support then undergoes a heat treatment step which makes it possible to confer on it physical properties corresponding to the intended application. According to a first embodiment, the heat treatment comprises at least one hydrothermal treatment step and at least one calcination step. The term "hydrothermal treatment" means treatment in the presence of water at a temperature above room temperature. Preferably the hydrothermal treatment is conducted at a temperature between 100 and 300 ° C, for 0.5 to 8 hours. During this hydrothermal treatment, the alumina support can be treated in different ways. Thus, the alumina can be pre-impregnated with an acidic solution and then subjected to hydrothermal treatment either in the vapor phase or in the liquid phase. This impregnation, before the hydrothermal treatment, can be carried out dry or by immersion of the alumina in an acidic aqueous solution. Dry impregnation means contacting the alumina with a volume of solution less than or equal to the volume of water recovery of the treated alumina. Preferably, the impregnation is carried out dry. It is also possible to treat the alumina support without prior impregnation with an acid solution, the acidity being in this case provided by an aqueous solution implemented during the actual hydrothermal treatment. The acidic aqueous solution comprises at least one acid compound for dissolving at least a portion of the alumina. The term "acid compound for dissolving at least a portion of the alumina", any acid compound which, contacted with alumina, carries out the dissolution of at least a portion of the aluminum ions. The acid preferably makes it possible to dissolve at least 0.5% by weight of alumina of the alumina support. Preferably, this acid is chosen from strong acids such as nitric acid, hydrochloric acid, perchloric acid, sulfuric acid or a weak acid used at a concentration such that its aqueous solution has a pH value. less than 4, such as acetic acid, or a mixture of these acids. In a preferred embodiment, the hydrothermal treatment is carried out in the presence of nitric acid and acetic acid alone or as a mixture. This treatment can be carried out in an autoclave and in this case preferably in a rotary basket autoclave such as that defined in the patent application EP-A-0 387 109. The hydrothermal treatment can also be carried out under saturated vapor pressure or under a partial steam pressure at least equal to 70% of the saturation vapor pressure corresponding to the treatment temperature. The calcination step which takes place after the hydrothermal treatment according to this first embodiment is carried out at a temperature generally of between 400 and 1500 ° C., preferably between 800 and 1300 ° C., for 1 and 8 hours in air, of which Water content is usually between 0 and 50% weight. According to a variant of the first embodiment of the heat treatment step, the dried support may also successively undergo a first calcination step, followed by a hydrothermal treatment step and finally a second calcination step. In this case, the two calcination steps are carried out in the ranges of operating conditions described above, the operating conditions being identical or different in each of the calcination steps. According to a second alternative embodiment of heat treatment, the support undergoes a heat treatment of calcination, that is to say that there is no hydrothermal treatment before or after this calcination. This is carried out at a temperature generally between 400 and 1500 ° C, preferably between 500 and 1200 ° C, for 1 and 8 hours in air with a water content generally between 0 and 50% by weight. In this embodiment the calcination step may be carried out in several stages in increasing temperature increments until the desired final calcination temperature is reached. At the end of the final heat treatment, the support has a specific surface area generally between 20 and 200 m 2 / g. The support has a crystallographic structure of the delta alumina, gamma or theta type, alone or as a mixture. The existence of the various crystallographic structures is related in particular to the conditions of implementation of the heat treatment and in particular to the final calcination temperature.
    [0010] The catalyst according to the invention is composed of a support of alumina, phosphorus and an active phase formed of at least one Group VIB metal and at least one Group VIII metal. During its preparation the catalyst does not undergo calcination, that is to say that the impregnated catalytic precursor is not subjected to a heat treatment step at a temperature above 200 ° C. The total metal content of group VIII is between 0.1 and 10% by weight of oxide of the group VIII metal relative to the total weight of the catalyst, preferably between 0.6 and 8% by weight, preferably between 2 and 7%, very preferably between 2 and 6% by weight and even more preferably between 3 and 6% by weight of the Group VIII metal oxide relative to the total weight of the catalyst. The group VIB metal content is between 3 and 35% by weight of the Group VIB metal oxide relative to the total weight of the catalyst, preferably between 5 and 30% by weight, preferably between 7 and 28% by weight. very preferably between 10 and 25% by weight of the Group VIB metal oxide relative to the total weight of the catalyst. The catalyst according to the invention has a phosphorus content generally of between 0.3 and 10% by weight of P2O5 relative to the total weight of catalyst, preferably between 2 and 8% by weight of P2O5 relative to the total weight of catalyst. For example, the phosphorus present in the catalyst is combined with the Group VIB metal and optionally also with the Group VIII metal in the form of heteropolyanions. The hydrotreatment catalyst according to the invention, in oxide form, is characterized by a specific surface area of between 20 and 150 m 2 / g, preferably between 30 and 120 m 2 / g, preferably between 40 and 95 m 2 / g, very preferably between 50 and 90 m 2 / g. In addition, the catalyst has a group VIB metal density, expressed as the number of atoms of said metal per unit area of the catalyst, which is between 7 and 30 Group VIB metal atoms per nm 2 of catalyst, more preferably from 7 to 25 Group VIB metal atoms per nm 2 of catalyst and very preferably from 7 to 20 Group VIB metal atoms per nm 2 of catalyst. Even more preferably, the group VIB metal density, expressed as the number of atoms of said metal per unit area of the catalyst, is between 7 and 15 Group VIB metal atoms per nm 2 of catalyst. By way of example, if the catalyst contains 20% by weight of molybdenum oxide MoO 3 (ie 13.33% by weight of Mo) and has a specific surface area of 100 m 2 / g, the density d (Mo) is equal to: (13.33 x NA) d (Mo) = = (100 x 1018 x 100 x 96) 8.3 atoms of Mo / nm 2 of catalyst The molar ratio of Group VIII metal to Group VIB metal of the catalyst is generally between 0.1 and 0.8, preferably between 0.2 and 0.6. Moreover, the phosphorus / (Group VIB metal) molar ratio is generally between 0.1 and 0.7, preferably between 0.2 and 0.6. The Group VIB metal present in the active phase of the catalyst is preferably selected from molybdenum and tungsten. The Group VIII metal present in the active phase of the catalyst is preferably selected from cobalt, nickel and the mixture of these two elements. The active phase of the catalyst is preferably selected from the group formed by the combination of nickel-molybdenum, cobalt-molybdenum and nickel-cobalt-molybdenum elements and very preferably the active phase is cobalt and molybdenum. The catalyst according to the invention is prepared according to a process comprising the following steps: a) at least one component of a Group VIB metal, at least one component of a Group VIII metal, is brought into contact with phosphorus with the support, so as to obtain a catalyst precursor; b) drying said catalyst precursor from step a) at a temperature below 200 ° C without subsequently calcining it. The step a) of contacting the support comprises several modes of implementation. According to a first embodiment of step a) of the catalyst preparation process, said components of the Group VIB, group VIII and phosphorus metals are deposited on said support, by one or more steps of co-impregnations, that is to say that said components of Group VIB metals, Group VIII and phosphorus are introduced simultaneously into said support. The co-impregnation step (s) is (are) preferably carried out by dry impregnation or impregnation in excess of solution. When this first mode comprises the implementation of several co-impregnation steps, each co-impregnation step is preferably followed by an intermediate drying step generally at a temperature below 200 ° C., advantageously between 50 and 180 ° C. ° C, preferably between 60 and 150 ° C, very preferably between 75 and 140 ° C.
    [0011] According to a preferred embodiment by co-impregnation, the aqueous impregnation solution when it contains cobalt, molybdenum and phosphorus is prepared under pH conditions favoring the formation of heteropolyanions in solution. For example, the pH of such an aqueous solution is between 1 and 5.
    [0012] According to a second embodiment of step a) of the process for preparing the catalyst, the catalyst precursor is prepared by proceeding with the successive and indifferent deposits of a component of a metal of group VIB, d. a component of a group VIII metal and phosphorus on said support. The deposits can be made by dry impregnation, by excess impregnation or by deposition-precipitation according to methods well known to those skilled in the art. In this second embodiment, the deposition of the components of groups VIB and VIII metals and phosphorus can be carried out by several impregnations with an intermediate drying step between two successive impregnations generally at a temperature of between 50 and 180 ° C. preferably between 60 and 150 ° C, very preferably between 75 and 140 ° C.
    [0013] Whatever the mode of deposition of the metals and phosphorus used, the solvent which enters the composition of the impregnating solutions is chosen so as to solubilize the metal precursors of the active phase, such as water or a solvent organic (eg an alcohol). By way of example, among the sources of molybdenum, it is possible to use oxides and hydroxides, molybdic acids and their salts, in particular ammonium salts such as ammonium molybdate, ammonium heptamolybdate, phosphomolybdic acid (H3PM012040), and their salts, and optionally silicomolybdic acid (H4SiMo12040) and its salts. The sources of molybdenum may also be any heteropolycomposed Keggin type, Keggin lacunary, Keggin substituted, Dawson, Anderson, Strandberg, for example.
    [0014] Molybdenum trioxide and heteropoly compounds of the Keggin, Keggin lacunary, Keggin substituted and Strandberg type are preferably used. The tungsten precursors that can be used are also well known to those skilled in the art. For example, among the sources of tungsten, it is possible to use oxides and hydroxides, tungstic acids and their salts, in particular ammonium salts such as ammonium tungstate, ammonium metatungstate, phosphotungstic acid and their salts. salts, and optionally silicotungstic acid (H4SiW12O40) and its salts. Tungsten sources can also be any heteropolycomposed Keggin type, Keggin lacunary, Keggin substituted, Dawson, for example. Oxides and ammonium salts such as ammonium metatungstate or heteropolyanions of the Keggin, Keggin lacunary or substituted Keggin type are preferably used. The cobalt precursors that can be used are advantageously chosen from oxides, hydroxides, hydroxycarbonates, carbonates and nitrates, for example. Cobalt hydroxide and cobalt carbonate are preferably used.
    [0015] The nickel precursors that can be used are advantageously chosen from oxides, hydroxides, hydroxycarbonates, carbonates and nitrates, for example. Nickel hydroxide and nickel hydroxycarbonate are preferably used. Phosphorus can advantageously be introduced into the catalyst at various stages of its preparation and in various ways. Phosphorus may be introduced during the shaping of said alumina support, or preferably after this shaping. It may for example be introduced just before or just after peptization of the chosen matrix, such as for example and preferably aluminum oxyhydroxide (boehmite) precursor of alumina. It may also advantageously be introduced alone or in admixture with at least one of Group VIB and VIII metals. The phosphorus is preferably introduced in admixture with the Group VIB and Group VIII metal precursors, in whole or in part on the shaped alumina support, by dry impregnation of said alumina support using of a solution containing the precursors of metals and the precursor of phosphorus. The preferred phosphorus source is orthophosphoric acid H 3 PO 4, but its salts and esters such as ammonium phosphates or mixtures thereof are also suitable. Phosphorus may also be introduced together with Group VIB element (s) in the form of, for example, Keggin, Keggin lacunary, Keggin substituted or Strandberg heteropolyanions. At the end of the impregnation step or metals group VIII, group VIB and phosphorus, the precursor of the catalyst is subjected to a drying step b) performed by any technique known to those skilled in the art. It is advantageously carried out at atmospheric pressure or under reduced pressure. Preferably, this step is carried out at atmospheric pressure. This step b) is carried out at a temperature below 200 ° C, preferably between 50 and 180 ° C, preferably between 60 ° C and 150 ° C and very preferably between 75 ° C and 140 ° C .
    [0016] Step b) is advantageously carried out in crossed bed using air or any other hot gas. Preferably, when the drying is carried out in a traversed bed, the gas used is either air or an inert gas such as argon or nitrogen. In a very preferred manner, the drying is carried out in a bed traversed in the presence of air.
    [0017] Preferably, this drying step has a duration of between 30 minutes and 4 hours, and preferably between 1 hour and 3 hours. At the end of step b) of the process according to the invention, a dried catalyst is obtained which is not subjected to any subsequent calcination step, for example in air, at a temperature above 200 ° C.
    [0018] Prior to its use as a hydrotreatment catalyst, it is advantageous to subject the catalyst to a sulfurization step (activation phase). This activation phase is carried out by methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere in the presence of hydrogen and hydrogen sulphide. The hydrogen sulfide can be used directly or generated by a sulfide agent (such as dimethyl disulphide). According to another aspect of the invention, the hydrotreatment catalyst as described above further comprises one or more organic compounds containing oxygen and / or nitrogen. Such a catalyst is referred to as "additive catalyst" in the following description. The organic compound present in the catalyst contains more than 2 carbon atoms and at least one oxygen and / or nitrogen atom. The oxygen-containing organic compound may be selected from a carboxylic acid, an alcohol, an aldehyde or an ester. By way of example, the organic compound containing oxygen may be chosen from the group consisting of ethylene glycol, triethylene glycol, glycerol, polyethylene glycol having a molecular weight of 150 to 1500, acetophenone, 2,4-pentanedione, pentanole, acetic acid, maleic acid, oxalic acid, tartaric acid, formic acid, citric acid, a cyclic oligosaccharide composed of at least 6 units glucopyranose bound in a (1-4), a dialkyl succinate. The dialkyl succinate is preferably a C1-C4 dialkyl succinate, preferably selected from the group consisting of dimethyl succinate, diethyl succinate, dipropyl succinate and dibutyl succinate. Preferably, the C1-C4 dialkyl succinate used is dimethyl succinate or diethyl succinate. Very preferably, C1-C4 dialkyl succinate is dimethyl succinate. According to one embodiment, the organic compound comprises at least the combination of C1-04 dialkyl succinate, in particular dimethyl succinate, and acetic acid. The nitrogen-containing organic compound may be selected from an amine. By way of example, the nitrogen-containing organic compound may be ethylene diamine or tetramethylurea. The organic compound containing oxygen and nitrogen may be selected from an amino carboxylic acid, an amino alcohol, a nitrile or an amide. By way of example, the organic compound containing oxygen and nitrogen may be aminotriacetic acid, 1,2-cyclohexane diamine tetraacetic acid, monoethanolamine, acetonitrile, N-methylpyrrolidone, dimethylformamide or ethylene diamine tetraacetic acid (EDTA). The additive catalyst according to the invention is prepared according to a process comprising the following steps: i) at least one component of a Group VIB metal, at least one component of a Group VIII metal, is contacted with phosphorus and at least one organic compound containing oxygen and / or nitrogen with the support, so as to obtain an additivated catalyst precursor, ii) drying said added catalyst precursor from step i) to a temperature below 200 ° C without subsequently calcining it. The molar ratio of organic compound (s) containing oxygen and / or nitrogen by element (s) of group VIB engaged on the added catalyst precursor is between 0.05 to 9 mol / mol preferably between 0.1 to 8 mol / mol, preferably between 0.2 and 7 mol / mol before drying of step ii). For example, when the organic component is a mixture of dialkyl succinate 01C4 (and in particular dimethyl succinate) and acetic acid, said components are advantageously introduced in an amount corresponding to: - a molar ratio of dialkyl succinate ( for example dimethyl) per element (s) of group VIB of the additive-containing catalytic precursor of between 0.05 to 2 mol / mol, preferably of between 0.1 to 1.8 mol / mol, preferably of between 0, 15 and 1.5 mol / mol, at a molar ratio of acetic acid per element (s) of the group VIB of the catalytic precursor additive comprised between 0.1 to 5 mol / mol, preferably between 0.5 to 4 mol / mol, preferably between 1.3 and 3 mol / mol and very preferably between 1.5 and 2.5 mol / mol. The step i) of contacting comprises several modes of implementation.
    [0019] According to a first embodiment of step i) of the process for preparing the additivated catalyst, the components of the Group VIB and Group VIII metals, phosphorus and the organic compound are deposited on the support, by at least one co-impregnation step, preferably by dry impregnation. According to this embodiment, said components of the Group VIB and Group VIII metals, the phosphorus and the organic compound are introduced simultaneously into said support. This first embodiment of step i) comprises the implementation of one or more co-impregnation steps, each co-impregnation step is preferably followed by an intermediate drying step generally at a temperature below 200 ° C, advantageously between 50 and 180 ° C, preferably between 60 and 150 ° C, very preferably between 75 and 140 ° C. According to a second embodiment of step i) of the process for preparing the additivated catalyst, at least one organic compound containing oxygen and / or nitrogen is brought into contact with at least one catalytic precursor comprising at least one Group VIII metal, at least one Group VIB metal, phosphorus and the support. This second embodiment is a preparation called "post-impregnation of the organic compound". This is carried out for example by dry impregnation. According to this second embodiment, the contacting according to step i) comprises the following successive steps which will be detailed below: it) impregnates an alumina support with at least one solution containing at least one metal of the group VIB, at least one Group VIII metal and phosphorus to obtain an impregnated support, i2) the impregnated support obtained in step II) is dried at a temperature below 200 ° C. without subsequent calcination to obtain a dried catalyst, i3) the dried catalyst obtained in step i2) is impregnated with an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an additivated catalyst precursor, i4) optionally, the additivated catalyst precursor obtained in step i3) is allowed to mature. In step II), the introduction of the Group VIB and Group VIII metals onto the alumina support can advantageously be carried out by one or more impregnations in excess of solution on the support based on alumina, or preferably by one or more dry impregnations of said alumina-based support, using an aqueous or organic solution containing precursors of metals. Group VIB, group VIII and phosphorus precursors are those described above. The introduction of Group VIB and Group VIII metals and phosphorus onto the alumina support is then followed by a drying step i2) during which the solvent (which is usually water) is removed, at a temperature below 200 ° C, preferably between 50 and 180 ° C, preferably between 60 and 150 ° C or between 75 and 140 ° C. The step of drying the impregnated support thus obtained is never followed by a step of calcination in air at a temperature greater than or equal to 200 ° C. It will be noted that steps i1) and i2) respectively correspond to steps a) and b) of the process for preparing the "non-additive" catalyst according to the invention described above.
    [0020] According to step i3), the dried catalyst is impregnated with an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen. The impregnating solution comprising at least one organic compound is preferably an aqueous solution. The said organic compound (s) can (advantageously) be deposited in one or more stages either by excess impregnation, or by dry impregnation, or by any other known means of the skilled person. Preferably, the introduction of the organic compound is carried out by a single impregnation step, and particularly preferably by a single dry impregnation step. According to step i4) of the preparation process, the additive-containing catalyst precursor from step i3) can be subjected to a maturation stage which is advantageously carried out at atmospheric pressure, at a temperature of between 17 ° C. and 50 ° C. ° C. The duration of the maturation is generally between 10 minutes and 48 hours and preferably between 30 minutes and 5 hours. In accordance with step ii) of the preparation process, the additive catalyst precursor, optionally after a maturation step, is subjected to a drying step at a temperature below 200 ° C, without subsequent calcination. The drying step ii) of the process according to the invention is advantageously carried out by any technique known to those skilled in the art. It is advantageously carried out at atmospheric pressure or under reduced pressure. Preferably, this step is carried out at atmospheric pressure. This step ii) is advantageously carried out at a temperature between 50 and 180 ° C, preferably between 60 ° C and 150 ° C and very preferably between 75 ° C and 140 ° C. Step ii) can advantageously be carried out in crossed bed using air or any other hot gas. Preferably, when the drying is carried out in a traversed bed, the gas used is either air or an inert gas such as argon or nitrogen. In a very preferred manner, the drying is carried out in a bed traversed in the presence of air. Preferably, this step ii) has a duration between 30 minutes and 4 hours, and preferably between 1 hour and 3 hours. At the end of step ii) of the process according to the invention, an additive catalyst is obtained which is not subjected to any subsequent calcination step at a temperature greater than or equal to 200 ° C. According to another alternative embodiment, the process for the preparation of the additivated catalyst combines the co-impregnation of an organic compound and the post-impregnation of an organic compound which may be identical or different from that used for the co-impregnation. This embodiment comprises the following steps: i) a solution containing at least one component of a Group VIB metal, at least one component of a Group VIII metal, phosphorus and at least one component is contacted by co-impregnation; at least one organic compound containing oxygen and / or nitrogen with the support, so as to obtain an additivated catalyst precursor, i ') drying said added catalyst precursor from step i) to a Below 200 ° C, without subsequently calcining it, i ") the added and dried catalyst precursor from step i ') is brought into contact with a solution of an organic compound containing oxygen and / or nitrogen, ii) drying the post-impregnated additive catalyst precursor from step i ") at a temperature below 200 ° C, without subsequently calcining it to provide an additive catalyst. The operating conditions described above are of course applicable in the context of this embodiment.
    [0021] Before use, it is advantageous to activate the additivated catalyst. This activation phase corresponds to a sulphurization which is carried out by the methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere in the presence of hydrogen and hydrogen sulphide.
    [0022] The additive catalyst obtained is therefore advantageously subjected to a sulphurization step, without intermediate calcination step. Said additivated catalyst is advantageously sulphured ex situ or in situ. The same sulfurizing agents as those described for the dried catalyst according to the invention can be used.
    [0023] The invention also relates to a process for hydrotreating a hydrocarbon cut. In particular the process is a hydrodesulfurization of a hydrocarbon fraction having a distillation range of between 30 and 260 ° C. Preferably, this hydrocarbon cut is a gasoline type cut. In a very preferred manner, the gasoline cut is an olefinic gasoline cut resulting for example from a catalytic cracking unit (Fluid Catalytic Cracking according to the English terminology). The hydrodesulfurization process according to the invention makes it possible to convert the organo-sulfur compounds of the hydrocarbon feedstock into hydrogen sulphide (H2S) while limiting as much as possible the hydrogenation of the olefins present in said feedstock. The hydrotreatment process consists in bringing the hydrocarbon fraction into contact with the catalyst according to the invention and with hydrogen under the following conditions: a temperature of between 200 and 400.degree. C., preferably of between 230.degree. 330 ° C; at a total pressure of between 1 and 3 MPa, preferably between 1.5 and 2.5 MPa; - a Hourly Volumetric Velocity (VVH), defined as the volume flow rate of charge relative to the catalyst volume, between 1 and 10 h -1, preferably between 2 and 611 -1; a hydrogen / petrol charge volume ratio of between 100 and 600 Nl / l, preferably between 200 and 400 Nl / l. The catalytic hydrodesulfurization process can be carried out in one or more series reactors of the fixed bed or bubbling bed type. If the process is carried out using at least two reactors in series, it is possible to provide a device for removing the H2S from the effluent from the first hydrodesulfurization reactor before treating said effluent in the process. second hydrodesulfurization reactor. EXAMPLES Example 1 - Preparation of calcined catalyst A (not in accordance with the invention) The support S1 of catalyst A is a surface-specific transition alumina of 80 m 2 / g. This transition alumina is obtained after the following steps: thermal decomposition of gibbsite at 800 ° C. (with a low residence time of 0.8 seconds), making it possible to obtain a transition alumina powder. A washing with water allowing the reduction of the sodium content is carried out on the powder which is followed by a second rapid dehydration treatment similar to the previous one. The alumina powder thus obtained is then shaped in a bezel to form beads which are then dried at 150 ° C. This support is finally subjected to a hydrothermal treatment at high partial pressure of water (100%) for 8 hours and then calcined at 850 ° C.
    [0024] Catalyst A is prepared by dry impregnation of the support with an aqueous solution containing molybdenum trioxide, cobalt hydroxide and phosphoric acid. The volume of the solution containing the precursors of metals and phosphorus being strictly equal to the volume of water uptake of the support (0.97 ml / g). The concentration of the metal precursors in aqueous solution is adjusted to obtain the desired weight percent of molybdenum, cobalt and phosphorus on the final catalyst. In order to obtain complete dissolution of the metal precursors, the impregnating solution is refluxed at 90 ° C. for 2 hours. After dry impregnation on the support, the catalyst is left to mature for 1.5 hours in a chamber saturated with water, dried under air in an oven at 90 ° C. and then calcined in air at 450 ° C.
    [0025] The catalyst A obtained after calcination has a content of 15.5% by weight of molybdenum (Mo03 equivalent), 3.4% by weight of cobalt (CoO equivalent) and 3.9% by weight of phosphorus (P2O5 equivalent), a specific surface area of 62 m 2 / g and thus a surface density in molybdenum of 10.6 atoms per square nanometer of catalyst. This catalyst has atomic ratios Co / Mo of 0.42 and P / Mo of 0.51.
    [0026] EXAMPLE 2 Preparation of a Dried Catalyst B Additive to Urea and Citric Acid and Containing No Phosphorus (Not in Accordance with the Invention) The support S2 of catalyst B is a transition alumina with a specific surface area of 44 m 2 / g obtained by recalcination in air at 1100 ° C of a support alumina SO shaped extruded.
    [0027] The SO support was synthesized by precipitation reaction via a mixture of sodium aluminate and aluminum sulphate. This reaction is carried out at a temperature of 60 ° C, at a pH of 9, for 60 minutes and with stirring of 200 rpm. The gel thus obtained is kneaded on a Z-arm kneader to provide a paste. The extrusion is carried out by passing the dough through a die provided with a trilobe shaped orifice 1.6 mm in diameter. The extrudates thus obtained are dried at 150 ° C. and then calcined at 450 ° C. under dry air. The support SO is then calcined in air at 1100 ° C. and the support S 2 is thus obtained. Catalyst B is prepared by dry impregnation of support S2 with an aqueous solution containing cobalt and molybdenum precursors, respectively cobalt carbonate and ammonium heptamolybdate. This solution also contains urea and citric acid. The concentration of urea and citric acid is determined so as to obtain a molar ratio of urea / molybdenum and citric acid / molybdenum of 3.8 and 0.6, respectively. The volume of impregnation solution is adjusted with water so as to strictly reach the volume of water uptake of the support (0.62 mUg). The concentration of cobalt and molybdenum in solution is adjusted to obtain the desired weight percent of molybdenum, cobalt and phosphorus on the final catalyst. After impregnation, the catalyst is dried in an oven under air at 110 ° C. No calcination under air is carried out subsequently. The catalyst B obtained after drying has a content of 15.3% by weight of molybdenum (MoO 3 oxide equivalent), 3.3% by weight of cobalt (CoO oxide equivalent), a specific surface area of 34 m2 / g, and thus a surface density. in molybdenum of 18.7 atoms per square nanometer of catalyst (denoted "dMo"). This catalyst has a Co / Mo atomic ratio of 0.41 and does not contain phosphorus.
    [0028] EXAMPLE 3 Preparation of Dried Catalysts C to I (in Accordance with the Invention) Catalysts C to J are obtained by dry impregnation according to the same protocol as catalyst A and on various supports based on transition alumina, followed by same stages of ripening and drying. No calcination step under air is performed after drying. Aqueous impregnation solutions are obtained by dissolving molybdenum trioxide, cobalt hydroxide and phosphoric acid. The amounts of precursors to be introduced in solution are adjusted according to the desired weight contents on the final catalyst. The aluminas S3, S4 and S5 are prepared by post-treatment of the alumina SO under different conditions. The support S3 is obtained by calcination in humid air at 850 ° C. (at 50% water / kg of dry air). The support S4 is obtained after hydrothermal treatment at 100 ° C. in the presence of 6.5% acetic acid for 3 hours in an autoclave and then calcination at 1000 ° C. under air. The support S5 is obtained by calcining in air S4 support at 1150 ° C. Table 1 gives the characteristics of the supports S1, S2, S3, S4 and S5 used.
    [0029] Table 1 Alumina Phases SBET (m2 / g) Diameter Total median crystallographic pore volume (cm3 / g) volume (nm) S1 theta, delta 81 44 1.03 S2 alpha, theta 44 56 0.63 S3 gamma 137 18.4 0.71 S4 theta, delta 78 40.7 0.84 S5 alpha, theta 37 58 0.62 The crystallographic phases are obtained from diffractogram obtained by X-ray diffraction. The BET surface area is determined by the method of nitrogen adsorption-desorption according to ASTM D3663-03. The median volume diameter and the total pore volume are obtained by mercury porosimetry according to the ASTM D4284-03 standard.
    [0030] Table 2 groups together the metal contents of the catalysts obtained as well as the density (dMo) of Group VIB metal (molybdenum), expressed as the number of molybdenum atoms per unit area of the catalyst (at / nm 2). 2 Support Catalysts MoO3 CoO P2O5 SBET dMo (% wt) (% wt) (wt%) (m2 / g) (at / n m2) A (not 51 15.5 3.4 3.9 62 10.6 compliant) B (not S2 15.3 3.3 0 34 18.7 compliant) C S3 22 4.6 6 92 10.0 (compliant) D (compliant) S3 28 5.8 7.6 82 14.6 E (compliant) ) S4 11.4 2.2 3.1 65 7.3 F (consistent) S4 16.2 3.3 4.3 59 11.3 G (compliant) S4 22.2 4.5 6.1 52 17, 7 H S4 24.1 4.7 6.5 51 20.0 (consistent) I S4 28 5.8 7.6 46 25.6 (compliant) Example 4 - Evaluation of Catalytic Performance of Catalysts A to I Model Load representative of a catalytic cracking gasoline (FCC) containing 10% by weight of 2,3-dimethylbut-2-ene and 0.33% by weight of 3-methylthiophene (ie 1000 ppm wt sulfur in the feedstock) is used to the evaluation of the catalytic performances different catalysts. The solvent used is heptane. The hydrodesulphurization reaction (HDS) is carried out in a fixed bed reactor passed under a total pressure of 1.5 MPa, at 210 ° C., at VVH = 6 11-1 (VVH = volume flow rate of charge / volume of catalyst), and a volume ratio H 2 / feed of 300 Nl / l, in the presence of 4 ml of catalyst. Prior to the HDS reaction, the catalyst is sulfided in situ at 350 ° C. for 2 hours under a stream of hydrogen containing 15 mol% of H25 at atmospheric pressure. Each of the catalysts is successively placed in said reactor. Samples were taken at different time intervals and analyzed by gas chromatography to observe the disappearance of the reagents and the formation of the products.
    [0031] The catalytic performances of the catalysts are evaluated in terms of catalytic activity and selectivity. The hydrodesulphurization (HDS) activity is expressed from the rate constant for the HDS reaction of 3-methylthiophene (kHDS), normalized by the volume of catalyst introduced and assuming a first order kinetics with respect to sulfur compound. The activity of hydrogenation of olefins (HydO) is expressed from the rate constant of the hydrogenation reaction of 2,3-dimethylbut-2-ene, normalized by the volume of catalyst introduced and assuming kinetics of order 1 with respect to the olefin. The selectivity of the catalyst is expressed by the normalized ratio of the rate constants 10 kHDS / kHydO. The ratio kHDS / kHydO will be higher as the catalyst becomes more selective. The values obtained are normalized by taking catalyst A as a reference (relative HDS activity and relative selectivity equal to 100). The performances are thus the relative HDS activity and the relative selectivity. Table 3 Catalysts Supports HDS activity Relative relative selectivity A (comparative) 51 100 100 B (comparative) S2 78 98 C (compliant) S3 238 114 D (compliant) S3 195 118 E (compliant) S4 125 143 F (compliant) S4 183 163 G (in conformity) S4 200 169 H (compliant) S4 213 175 I (compliant) S4 215 178 The catalysts according to the invention all have improved selectivity in hydrodesulphurization with respect to the hydrogenation of olefins compared with non-catalytic catalysts. according to the invention A (calcined) and B (the catalyst does not contain phosphorus). This improvement in the selectivity of the catalysts is particularly advantageous in the case of an implementation in an olefin-containing gasoline hydrodesulphurization process for which it is desired to limit as much as possible the loss of octane due to hydrogenation. olefins. Catalysts C to I are also more active in hydrodesulfurization than non-compliant catalysts A and B. Example 5 - Preparation of a dried catalyst K1 and K2 (in accordance with the invention), in the presence of an organic molecule co-impregnation The catalysts K1 and K2 are obtained by dry impregnation of the support S4. The volume of the aqueous impregnating solution containing the precursors of the metals and phosphorus being strictly equal to the volume of water uptake of the support (0.91 mUg). The concentration of the metal precursors in aqueous solution is adjusted to obtain the desired weight percent of molybdenum, cobalt and phosphorus on the final catalyst. Two solutions of impregnation were prepared from the solution obtained by dissolving molybdenum trioxide, cobalt hydroxide and phosphoric acid by adding as organic molecule citric acid for the first solution and triethylene glycol for the second solution. The first impregnation solution has a citric acid / molybdenum molar ratio of 0.4. The second impregnating solution has a triethylene glycol / molybdenum molar ratio of 0.4. The impregnating solutions are refluxed at 90 ° C. for 2 hours to obtain complete dissolution of the metal precursors in solution. These solutions are then impregnated on the support S4. After dry impregnation, the catalysts are left to mature for 1.5 hours in a closed chamber saturated with water and then dried under air in an oven at 120 ° C. For the catalyst K1 which contains citric acid, the weight contents, in oxide equivalent, in molybdenum (MoO3), cobalt (CoO) and phosphorus (P2O5) are respectively 10.5; 2.2 and 2.9. For the catalyst K2 which contains triethylene glycol, the weight contents, in oxide equivalent, in molybdenum (MoO3), cobalt (CoO) and phosphorus (P2O5) are respectively 10.4; 2.2 and 2.9.
    [0032] Table 4 Catalysts Support MoO3 CoO P2O5 SBET dMo additive (co- (% wt) (% wt) (% wt) (m2 / g) (for m2) impregnation) K1 S4 10.5 2.2 2.9 58 7, Example 6 - Preparation of Dried Catalysts L1, L2 and L3 (in Accordance with the Invention) in the Presence of an Organic Molecule in Post-Additivation Catalysts L1, L2 and L3 are obtained from the dried catalyst E. An additional step of dry impregnation is performed by an aqueous solution comprising one or more organic molecules in a mixture. The volume of the solution is determined from the water recovery volume of the dried catalyst E (at 0.76 ml / g), and as a function of the mass quantity of catalyst to be prepared. The additive catalyst precursor L1 is obtained by dry impregnation of an aqueous solution, containing citric acid. The concentration of citric acid in solution is determined so as to obtain a citric acid / molybdenum molar ratio of 0.4. The L2 additive catalyst precursor is obtained by dry impregnation of an aqueous solution, containing triethylene glycol. The concentration of triethylene glycol in solution is determined so as to obtain a triethylene glycol / molybdenum molar ratio of 0.4. The additive catalyst precursor L3 is obtained by dry impregnation of an aqueous solution containing dimethyl succinate and acetic acid. The concentration of dimethyl succinate is determined so as to obtain a molar ratio of dimethyl succinate to molybdenum of 0.7 and the volume ratio between acetic acid and dimethyl succinate is set at 0.75. After dry impregnation, each of the catalyst precursors additives L1, L2, L3 are left to mature in air at room temperature for 1 h 30 in a closed chamber in a saturated water and then dried at 140 ° C for 2 hours on a rotary evaporator. . Before additivation, the characteristics of catalyst precursors L1, L2 and L3 are identical to that of catalyst E.
    [0033] EXAMPLE 7 Evaluation of the Performance of Catalysts K1, K2, L1, L2, L3 Compared with Catalysts A and B (Non-Compliant) The performances of the catalysts are determined under the conditions of Example 4. The results are shown in the table. 6.
    [0034] Table 6 Catalysts Supports HDS activity Relative relative selectivity A (comparative) S1 100 100 B (comparative) S2 78 98 K1 (compliant) S4 255 187 K2 (compliant) S4 303 214 L1 (conform) S4 273 189 L2 (conform) S4 255 182 L3 (in conformity) S4 288 188 The catalysts according to the invention all have an improved selectivity in hydrodesulphurization with respect to the hydrogenation of olefins with respect to catalysts A 10 (calcined) and B (no calcination, and no phosphorus) not in accordance with the invention. This improvement of selectivity of the catalysts is particularly advantageous in the case of an implementation in a gasoline hydrodesulfurization process containing olefins for which it is sought to limit as much as possible the loss of octane due to the hydrogenation of olefins.
    [0035] In addition, these catalysts exhibit a greatly improved relative HDS activity relative to the catalysts A (calcined) and B (no calcination and no phosphorus) not in accordance with the invention. Thus, without being bound to any theory, the addition of an organic molecule, either in co-impregnation or post-additivation, also makes it possible to greatly increase the relative HDS activity. 20
    权利要求:
    Claims (17)
    [0001]
    REVENDICATIONS1. Hydrotreating catalyst comprising a support based on alumina, at least one group VIB metal, at least one group VIII metal and phosphorus in which: the specific surface area of the catalyst is between 20 and 150 m 2 / g; the group VIB metal density, expressed as the number of Group VIB metal atoms per unit area of the catalyst, is between 7 and 30 Group VIB metal atoms per nm 2 of catalyst; the catalyst being prepared by impregnating the Group VIB, Group VIII and phosphorus metals on the support so as to obtain an impregnated catalytic precursor and then drying said impregnated catalytic precursor at a temperature below 200 ° C and without subsequent calcination.
    [0002]
    2. Catalyst according to claim 1, wherein: the group VIB metal content is between 3 and 35% by weight of oxide of said group VIB metal relative to the total weight of the catalyst; the group VIII metal content is between 0.1 and 10% by weight of oxide of said group VIII metal relative to the total weight of the catalyst; the phosphorus content is between 0.3 and 10% by weight of P2O5 relative to the total weight of the catalyst.
    [0003]
    3. Catalyst according to one of the preceding claims, wherein the molar ratio (Group VIII metal) / (Group VIB metal) is between 0.1 and 0.8 and the molar ratio phosphorus / (Group VIB metal) ) is between 0.1 and 0.7.
    [0004]
    4. Catalyst according to one of the preceding claims, wherein the specific surface area of the catalyst is between 30 and 150 m 2 / g, preferably between 40 and 95 m 2 / g and very preferably between 50 and 90 m 2 / g. boy Wut.
    [0005]
    5. Catalyst according to one of the preceding claims, wherein the group VIB metal density is between 7 and 25 Group VIB metal atoms per nm 2 of catalyst, preferably between 7 and 20 metal atoms of the VIB group by nm 2 of catalyst, preferably between 7 and 15 Group VIB metal atoms per nm 2 of catalyst.
    [0006]
    6. Catalyst according to one of the preceding claims, wherein the Group VIB metal is selected from tungsten and molybdenum and the Group VIII metal is selected from nickel and cobalt.
    [0007]
    The catalyst of claim 6, wherein the Group VIB metal is molybdenum and the Group VIII metal is cobalt.
    [0008]
    8. Catalyst according to one of the preceding claims, wherein the support based on alumina is obtained from alumina gel kneaded, shaped and calcined.
    [0009]
    9. Catalyst according to one of the preceding claims, further comprising at least one organic compound containing oxygen and / or nitrogen.
    [0010]
    The catalyst of claim 9, wherein the organic compound is selected from carboxylic acid, alcohol, aldehyde, ester, amine, amino carboxylic acid, amino alcohol, nitrile and amide.
    [0011]
    The catalyst according to claim 10, wherein the organic compound is selected from ethylene glycol, triethylene glycol, glycerol, polyethylene glycol having a molecular weight of 150 to 1500, acetophenone, 2,4-pentanedione, pentanole, acetic acid, maleic acid, oxalic acid, tartaric acid, formic acid, citric acid, C1-C4 dialkyl succinate, a cyclic oligosaccharide composed of at least 6 1- (1-4) -linked glucopyranose units, ethylene diamine, tetramethylurea, aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, monoethanolamine, acetonitrile, N-methylpyrrolidone, dimethylformamide and ethylene diamine tetraacetic acid.
    [0012]
    12. Catalyst according to one of the preceding claims, characterized in that it is sulphurized.
    [0013]
    13. Process for the preparation of a catalyst according to one of claims 1 to 8, comprising the following steps: a) is deposited on a support based on alumina by one or more impregnations group VIII metals, group VIB and phosphorus so as to obtain an impregnated catalyst precursor; b) the impregnated precursor is dried at a temperature below 200 ° C without subsequent calcination so as to provide a dried catalyst.
    [0014]
    14. Process for the preparation of a catalyst according to one of claims 9 to 11, comprising the following steps: i) is deposited on a support based on alumina by one or more impregnations group VIII metals, group VIB phosphorus and at least one organic compound containing oxygen and / or nitrogen so as to obtain an impregnated catalytic precursor; ii) the impregnated precursor is dried at a temperature below 200 ° C without subsequent calcination so as to provide a dried catalyst.
    [0015]
    15. The method according to claim 14, wherein step i) comprises the following successive steps: il) an alumina support is impregnated with at least one solution containing at least one Group VIB metal, at least one metal of the group VIII and phosphorus to obtain an impregnated support, i2) the impregnated support obtained in step i1) is dried at a temperature below 200 ° C without subsequent calcination to obtain a dried catalyst, i3) the dried catalyst is impregnated obtained in step i2) by an impregnating solution comprising at least one organic compound containing oxygen and / or nitrogen to obtain an additivated catalyst precursor, i4) optionally the catalyst precursor is allowed to mature additive obtained in step i3).
    [0016]
    16. A process for the hydrodesulphurization of a petrol cut in which said petrol cut is brought into contact with hydrogen and a catalyst according to one of claims 1 to 11 or prepared according to one of claims 13 to 15, said catalyst being sulphurized and the bringing into contact being carried out at: a temperature of between 200 and 400 ° C., a total pressure of between 1 and 3 MPa; - A Hourly Volumetric Speed, defined as the volume flow rate of charge relative to the catalyst volume, between 1 and 1011-1; a hydrogen volume / gasoline charge ratio of between 100 and 600 Nl / l.
    [0017]
    The process of claim 16, wherein the gasoline is a gasoline from a catalytic cracking unit. 10
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    US10058852B2|2018-08-28|
    CN105312069A|2016-02-10|
    BR102015015930B1|2020-12-22|
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    EP2962753A1|2016-01-06|
    BR102015015930A2|2016-01-05|
    JP6642986B2|2020-02-12|
    EP2962753B1|2019-03-20|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US5290429A|1990-05-25|1994-03-01|Union Oil Company Of California|Catalytic aromatic saturation in the presence of halide|
    EP0483923A1|1990-10-31|1992-05-06|Shell Internationale Researchmaatschappij B.V.|Hydrodenitrification process|
    WO2007084471A1|2006-01-17|2007-07-26|Exxonmobil Research And Engineering Company|Selective catalysts for naphtha hydrodesulfurization|
    WO2007084437A2|2006-01-17|2007-07-26|Exxonmobil Research And Engineering Company|Selective catalysts having high temperature alumina supports for naphtha hydrodesulfurization|
    RU2313389C1|2006-10-13|2007-12-27|Институт Катализа Им. Г.К. Борескова Сибирского Отделения Российской Академии Наук|Catalyst, method for preparation thereof, method for preparing carrier for this catalyst, and diesel fraction desulfurization process|
    WO2014013154A1|2012-07-17|2014-01-23|IFP Energies Nouvelles|Method of petrol desulphurisation|
    WO2014173878A1|2013-04-23|2014-10-30|Shell Internationale Research Maatschappij B.V.|Process for preparing a sulphided catalyst|EP3228683A1|2016-04-08|2017-10-11|IFP Énergies nouvelles|Method for treating a gasoline|
    EP3312260A1|2016-10-19|2018-04-25|IFP Energies nouvelles|Method for hydrodesulphurisation of olefinic gasoline|FR2642414B1|1989-02-01|1991-04-26|Rhone Poulenc Chimie|PROCESS FOR THE MANUFACTURE OF AGGLOMERATES OF ACTIVE ALUMIN, AGGLOMERATES OBTAINED BY THE PROCESS AND DEVICE FOR IMPLEMENTING SAME|
    US5318690A|1991-08-15|1994-06-07|Mobil Oil Corporation|Gasoline upgrading process|
    US6409913B1|1996-02-02|2002-06-25|Exxonmobil Research And Engineering Company|Naphtha desulfurization with reduced mercaptan formation|
    US5968346A|1998-09-16|1999-10-19|Exxon Research And Engineering Co.|Two stage hydroprocessing with vapor-liquid interstage contacting for vapor heteroatom removal|
    JP4689198B2|2004-06-16|2011-05-25|財団法人石油産業活性化センター|Hydrocarbon hydrotreating catalyst, process for producing the same, and hydrotreating process for hydrocarbon oil|
    FR2875419B1|2004-09-22|2007-02-23|Inst Francais Du Petrole|ALUMINO-SILICATE DOPE CATALYST AND IMPROVED PROCESS FOR TREATING HYDROCARBON LOADS|
    FR2880823B1|2005-01-20|2008-02-22|Total France Sa|HYDROTREATING CATALYST, PROCESS FOR PREPARING THE SAME AND USE THEREOF|
    DK2823886T3|2005-12-14|2019-09-23|Advanced Refining Technologies Llc|Process for preparing a hydrotreating catalyst|
    FR2904242B1|2006-07-28|2012-09-28|Inst Francais Du Petrole|PROCESS FOR HYDRODESULFURING CUTS CONTAINING SULFUR COMPOUNDS AND OLEFINS IN THE PRESENCE OF A SUPPORTED CATALYST COMPRISING ELEMENTS OF GROUPS VIII AND VIB|
    WO2011029716A2|2009-09-10|2011-03-17|Albemarle Europe Sprl|Concentrated solutions comprising group vi metal, group viii metal, and phosphorus|
    JP5635752B2|2009-09-25|2014-12-03|日本ケッチェン株式会社|Method for producing hydrotreating catalyst, and hydrotreating method for hydrocarbon oil using the catalyst|
    DK2512662T3|2009-12-16|2014-08-11|IFP Energies Nouvelles|Catalyst for use in hydrotreating comprising metals of groups VIII and VIB and preparation with acetic acid and dialkyl succinate C1-C4|
    CN103769220B|2012-10-24|2016-04-27|中国石油化工股份有限公司|A kind of preparation method of catalyst for hydrogenation of fraction oil|
    CN103769221B|2012-10-24|2016-04-27|中国石油化工股份有限公司|The preparation method of catalyst for hydrogenation of fraction oil|
    JP6378902B2|2014-03-10|2018-08-22|日本ケッチェン株式会社|Hydrotreating catalyst, method for producing the catalyst, and hydrotreating method for hydrocarbon oil using the catalyst|US10604709B2|2017-02-12|2020-03-31|Magēmā Technology LLC|Multi-stage device and process for production of a low sulfur heavy marine fuel oil from distressed heavy fuel oil materials|
    US20190233741A1|2017-02-12|2019-08-01|Magēmā Technology, LLC|Multi-Stage Process and Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil|
    FR3075072B1|2017-12-14|2021-11-26|Ifp Energies Now|FCC GASOLINE SELECTIVE HYDRODESULFURATION CATALYST|
    CN110064405B|2018-01-23|2022-03-01|中国石油天然气股份有限公司|Preparation method of hydrotreating catalyst with desulfurization activity|
    FR3083131A1|2018-06-27|2020-01-03|IFP Energies Nouvelles|CATALYST BASED ON IMIDAZOLIDINONES, IMIDAZOLIDINEDIONES, PYRIMIDINONES AND / OR PYRIMIDINETRIONES AND ITS USE IN A HYDROPROCESSING AND / OR HYDROCRACKING PROCESS|
    FR3083132A1|2018-06-27|2020-01-03|IFP Energies Nouvelles|CATALYST BASED ON 1--2-PYRROLIDONE AND / OR 1--2,5-PYRROLIDINEDIONE AND ITS USE IN A HYDROTREATMENT AND / OR HYDROCRACKING PROCESS|
    FR3083134A1|2018-06-27|2020-01-03|IFP Energies Nouvelles|CATALYST BASED ON 1-VINYL-2-PYRROLIDONE AND / OR 1-ETHYL-2-PYRROLIDONE AND ITS USE IN A HYDROTREATMENT AND / OR HYDROCRACKING PROCESS|
    FR3083139A1|2018-06-27|2020-01-03|IFP Energies Nouvelles|CATALYST BASED ON PIPERIDINONES, PIPERIDINEDIONES AND / OR AZEPANONES AND ITS USE IN A HYDROTREATMENT AND / OR HYDROCRACKING PROCESS|
    EP3822332A1|2019-11-13|2021-05-19|Indian Oil Corporation Limited|Catalyst for selective hydrogenation of diolefins and method for preparing catalyst|
    FR3104463B1|2019-12-17|2021-12-17|Ifp Energies Now|HYDROGENOLYSIS CATALYST OBTAINED FROM MOLTEN SALTS AND AN ORGANIC ADDITIVE|
    FR3105931A1|2020-01-06|2021-07-09|IFP Energies Nouvelles|CATALYST BASED ON 2-HYDROXY-BUTANEDIOIC ACID OR 2-HYDROXY-BUTANEDIOIC ACID ESTERS AND ITS USE IN A HYDROTREATMENT AND / OR HYDROCRACKING PROCESS|
    法律状态:
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    2020-07-28| PLFP| Fee payment|Year of fee payment: 7 |
    2021-07-26| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
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    FR1456464|2014-07-04|
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    BR102015015930-7A| BR102015015930B1|2014-07-04|2015-07-01|hydrotreating catalyst with high molybdenum density, its preparation processes and hydrodesulfurization process of a gasoline cut|
    JP2015133593A| JP6642986B2|2014-07-04|2015-07-02|Hydrodesulfurization method|
    US14/790,678| US10058852B2|2014-07-04|2015-07-02|Hydrotreatment catalyst with a high density of molybdenum, and process for its preparation|
    CN201510383660.7A| CN105312069B|2014-07-04|2015-07-03|Hydroprocessing catalysts with high molybdenum density and methods of making the same|
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