CATALYST BASED ON Y-CETOVALERIC ACID AND USE THEREOF IN A HYDROTREATING AND / OR HYDROCRACKING PROCE

专利摘要:
The invention relates to a catalyst comprising a support based on alumina or silica or silica-alumina, at least one element of group VIII, at least one element of group VIB and γ-ketovaleric acid. The invention also relates to the process for preparing said catalyst and its use in a hydrotreatment and / or hydrocracking process.
公开号:FR3035600A1
申请号:FR1553913
申请日:2015-04-30
公开日:2016-11-04
发明作者:Pierre-Louis Carrette
申请人:IFP Energies Nouvelles IFPEN；
IPC主号:

专利说明:

[0001] The invention relates to an γ-ketovaleric acid additive catalyst, its method of preparation and its use in the field of hydrotreatment and / or hydrocracking. Usually, a hydrotreating catalyst for hydrocarbon cuts is intended to eliminate the sulfur or nitrogen compounds contained therein in order, for example, to bring a petroleum product to the required specifications (sulfur content, aromatic content, etc.) for a given application (motor fuel, gasoline or diesel, heating oil, jet fuel). It may also be pretreat this load in order to remove impurities or hydrogenate before subjecting it to various transformation processes to modify the physicochemical properties, such as for example reforming processes, d hydrocracking of vacuum distillates, catalytic cracking, hydroconversion of atmospheric residues or under vacuum. The composition and use of the hydrotreatment catalysts are particularly well described in the article by B. S Clausen, HT Topsee, and FE Massoth, from Catalysis Science and Technology, Volume 11 (1996), Springer- Verlag. The tightening of automobile pollution standards in the European Community (Official Journal of the European Union, L76, 22 March 2003, Directive 2003/70 / EC, pages L76 / 10-L76 / 19) has forced refiners to reduce very sharply sulfur content in diesel fuels and gasoline (up to 10 parts per million weight (ppm) of sulfur as of January 1, 2009, compared to 50 ppm as of January 1, 2005). In addition, refiners are forced to use loads that are more and more resistant to hydrotreatment processes because the crudes are heavier and therefore contain more and more impurities, on the other hand, because of the increase in conversion processes in refineries. Indeed, these generate cuts more difficult to hydrotreat than the cuts directly from the atmospheric distillation. More difficult to hydrotreat, usually means higher operating temperatures to achieve the same sulfur content in the effluent, and consequently lower cycle times that can be reduced. These fillers require catalysts having hydrodesulphurizing and hydrogenating functions which are greatly improved compared to conventional catalysts. In addition, conversion processes such as catalytic cracking or hydrocracking use catalysts having an acid function, which makes them particularly sensitive to the presence of nitrogenous impurities, and particularly basic nitrogen compounds. It is therefore necessary to use pretreatment catalysts of these fillers so as to remove these compounds.
[0002] Conventional hydrotreatment catalysts generally comprise an oxide support and an active phase based on Group VIB and VIII metals in their oxide forms as well as phosphorus. The preparation of these catalysts generally comprises a step of impregnating the metals and phosphorus on the support, followed by drying and calcination to obtain the active phase in their oxide forms. Before their use in a hydrotreatment and / or hydrocracking reaction, these catalysts are generally subjected to sulphidation in order to form the active species. The addition of an organic compound to the hydrotreatment catalysts to improve their activity has been recommended by those skilled in the art, especially for catalysts which have been prepared by impregnation followed by drying without subsequent calcination. These catalysts are often called "dried catalyst additives". Numerous documents describe the use of different ranges of organic compounds as additives, such as organic compounds containing nitrogen and / or organic compounds containing oxygen. A family of compounds now well known in the literature relates to chelating nitrogen compounds (EP0181035, EP1043069 and US6540908) with, for example, ethylenediaminetetraacetic acid (EDTA), ethylenediamine, diethylenetriamine or nitrilotriacetic acid ( NTA).
[0003] In the family of organic compounds containing oxygen, the use of optionally etherified mono-, di- or polyalcohols is described in documents WO96 / 41848, W001 / 76741, US4012340, US3954673, EP601722, and WO2005 / 035691. . The prior art more rarely refers to additives comprising ester functions (EP1046424, WO2006 / 077326). There are also several patents that claim the use of carboxylic acids (EP1402948, EP0482817). In particular, in EP0482817, citric acid, but also tartaric, butyric, hydroxyhexanoic, malic, gluconic, glyceric, glycolic, hydroxybutyric acids have been described. The specificity lies in the drying which must be conducted at a temperature below 200 ° C. However, none of the carboxylic acid literature describes the use of γ-ketovaleric acid. Whatever the compounds chosen, the induced modifications do not always make it possible to increase sufficiently the performance of the catalyst to meet the specifications relating to the sulfur and / or nitrogen contents of the fuels. In addition, it is often very difficult to proceed with their industrial deployment as the methods are complex to implement. Accordingly, it is essential for catalyst manufacturers to find new hydrotreatment and / or hydrocracking catalysts with improved performance. The invention relates to a catalyst comprising a support based on alumina or silica or silica-alumina, at least one element of group VIII, at least one element of group VIB and γ-ketovaleric acid.
[0004] The applicant has indeed found that the use of γ-ketovaleric acid as organic additive on a catalyst containing at least one element of group VIII and at least one element of group VIB, made it possible to obtain a 3035600 4 hydrotreating and / or hydrocracking catalyst showing improved catalytic performance. Indeed, the catalyst according to the invention shows an increased activity compared to the catalysts not additivés and dried catalysts additives known.
[0005] Typically, thanks to the increase in the activity, the temperature necessary to reach a desired sulfur or nitrogen content (for example 10 ppm of sulfur in the case of a diesel fuel charge, in ULSD or Ultra Low Sulfur Diesel mode according to Anglo-Saxon terminology) can be lowered. Likewise, the stability is increased because the cycle time is prolonged due to the necessary temperature reduction. The catalyst according to the present invention is also easier to prepare because of a high solubility of γ-ketovaleric acid in water or any other protic polar solvent. In addition, the catalyst according to the invention can be prepared from a biomass-containing raw material containing γ-ketovaleric acid while remaining at an acceptable or even advantageous cost depending on the method of preparation chosen. . According to one variant, the content of group VIB element is between 5 and 40 weight expressed as Group VIB metal oxide with respect to the total weight of the catalyst, the content of Group VIII element is between 1 and 10% by weight. expressed as Group VIII metal oxide with respect to the total weight of the catalyst. According to one variant, the molar ratio element of group VIII to group VIB element in the catalyst is between 0.1 and 0.8. According to one variant, the catalyst additionally contains phosphorus, the phosphorus content being between 0.1 and 20% by weight expressed as P2O5 with respect to the total weight of the catalyst and the phosphorus ratio on the Group VIB element in the catalyst is greater than or equal to 0.05. According to one variant, the γ-ketovaleric acid content is between 1 and 35% by weight relative to the total weight of the catalyst.
[0006] Alternatively, the catalyst further contains an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur. According to this variant, the organic compound is preferably chosen from a compound comprising one or more chemical functional groups chosen from a carboxylic function, alcohol, thiol, thioether, sulphone, sulphoxide, ether, aldehyde, ketone, ester, carbonate, amine, nitrile , imide, oxime, urea and amide. Preferably, it is chosen from triethylene glycol, diethylene glycol, ethylenediaminetetraacetic acid (EDTA), maleic acid, citric acid, dimethylformamide, bicine, or tricine.
[0007] According to one variant, the support contains from 0.1 to 50% by weight of zeolite. According to a variant, the catalyst is at least partially sulphurized. The invention also relates to the process for preparing said catalyst comprising the following steps: a) at least one component of a group VIB element, at least one component of a group VIII element, is brought into contact with γ-ketovaleric acid and optionally phosphorus with a support based on alumina or silica or silica-alumina, or is brought into contact a regenerated catalyst containing a support based on alumina or silica or silica-alumina, at least one component of a group VIB element, at least one component of a group VIII element and optionally phosphorus with γ-ketovaleric acid, so as to obtain a catalyst precursor, b) dry said catalyst precursor from step a) at a temperature below 200 ° C without calcining it later.
[0008] According to a variant, step a) is the following step: a ') impregnating a support based on alumina or silica or silica-alumina with at least one solution containing at least one group VIB element, at least one group VIII element, γ-ketovaleric acid and optionally phosphorus so as to obtain a catalyst precursor.
[0009] According to another variant, step a) comprises the following steps: a1) impregnating a support based on alumina or silica or silica-alumina with at least one solution containing at least one group VIB element, at least one group VIII element and optionally phosphorus to obtain an impregnated support, a2) the impregnated support obtained in step a1) is dried at a temperature below 200 ° C to obtain a dried impregnated support, and optionally calcine the dried impregnated support to obtain a calcined impregnated support, 10 a3) the dried and optionally calcined impregnated support obtained in step a2) is impregnated with an impregnating solution comprising at least γ-ketovaleric acid in order to obtain a catalyst precursor, a4) optionally, the catalyst precursor obtained in step a3) is allowed to mature. According to another variant, step a) comprises the following steps: a ') is prepared a support comprising at least γ-ketovaleric acid and optionally at least a portion of the phosphorus, a2') is impregnated with the support obtained at 1 step a1 ') by an impregnating solution comprising at least one element of group VIB, at least one element of group VIII and optionally phosphorus so as to obtain a catalyst precursor, a3') optionally, it is allowed to mature catalyst precursor obtained in step a2 ').
[0010] According to another variant, step a) comprises the following steps: a) a solution containing at least one element of group VIB, at least one element of group VIII, at least one compound, is contacted by co-impregnation organic material containing oxygen and / or nitrogen and / or sulfur, and optionally phosphorus with a support based on alumina or silica or silica-alumina so as to obtain an impregnated support, 3035600 7 a2 ") is dried the impregnated support from step a" ") at a temperature below 200 ° C, without subsequently calcining to obtain a dried impregnated support, a3") is brought into contact with the dried impregnated support from the step a2 ") with a solution of an organic compound containing oxygen and / or nitrogen and / or sulfur identical to or different from that used in step a1" ") so as to obtain a precursor of catalyst, a4 ") optionally, the catalyst precursor is allowed to mature ur obtained in step a3 "), and at least one of the organic compounds of step a1" - or step a3 ") is γ-ketovaleric acid. According to a variant, when it is desired to prepare the catalyst according to the invention from a regenerated catalyst, stage a) of the preparation process comprises the following steps: embedded image a regenerated catalyst containing a support is impregnated based on alumina or silica or silica-alumina, at least one component of a group VIB element, at least one component of a group VIII element and optionally phosphorus with an impregnation solution comprising at least γ-ketovaleric acid to obtain a catalyst precursor, a2 ") optionally, the catalyst precursor obtained in step a" ") is allowed to mature. -cétovalérique per element (s) of group VIII is between 0.1 and 5.0 mol / mol.
[0011] The invention also relates to the use of the catalyst according to the invention or prepared according to the preparation method according to the invention in a hydrotreatment and / or hydrocracking process for hydrocarbon cuts. In the following, groups of chemical elements are given according to the CAS classification (CRC Handbook of Chemistry and Physics, publisher CRC Press, editor-in-chief D. R. Lide, 81st edition, 2000-2001). For example, the group 3035600 8 VIII according to the classification CAS corresponds to the metals of the columns 8, 9 and 10 according to the new classification IUPAC. Hydroprocessing is understood to include reactions including hydrodesulfurization (HDS), hydrodenitrogenation (HDN) and aromatic hydrogenation (HDA). DETAILED DESCRIPTION OF THE INVENTION Catalyst The catalyst according to the invention is a catalyst additive at least with cetovaleric acid. More particularly, the catalyst according to the invention comprises a support based on alumina or silica or silica-alumina, at least one element of group VIII, at least one element of group VIB and γ-ketovaleric acid. The catalyst according to the invention may be a fresh catalyst, that is to say a catalyst which has not been used as catalyst previously in a catalytic unit and in particular in hydrotreatment and / or hydrocracking. The catalyst according to the invention may also be a rejuvenated catalyst. The term "rejuvenated catalyst" means a catalyst which has been used as a catalyst in a catalytic unit and in particular in hydrotreatment and / or hydrocracking and which has been subjected to at least one calcination step in order to burn the coke (regeneration). This regenerated catalyst is then additive at least with ycetovaleric acid to obtain the rejuvenated catalyst. This rejuvenated catalyst may contain one or more other organic additive (s) which may be added before, after or at the same time as γ-ketovaleric acid. The hydrogenating function of said catalyst, also called the active phase, is provided by at least one group VIB element and at least one group VIII element. The preferred group VIB elements are molybdenum and tungsten. The preferred group VIII elements are non-noble elements and in particular cobalt and nickel. Advantageously, the hydrogenating function is chosen from the group formed by the combinations of cobalt-molybdenum, nickel-molybdenum, nickel-tungsten or nickel-cobalt-molybdenum, or nickel-molybdenum-tungsten elements.
[0012] In the case where an important activity in hydrodesulphurization, or hydrodenitrogenation and hydrogenation of aromatics is desired, the hydrogenating function is advantageously provided by the combination of nickel and molybdenum; a combination of nickel and tungsten in the presence of molybdenum may also be advantageous. In the case of vacuum or heavier distillate fillers, cobalt-nickel-molybdenum combinations may be advantageously used. The total content of Group VIB and Group VIII elements is advantageously greater than 6% by weight expressed as oxide relative to the total weight of the catalyst.
[0013] The content of Group VIB element is between 5 and 40% by weight, preferably between 8 and 35% by weight, and more preferably between 10 and 30% expressed as Group VIB metal oxide with respect to the total weight of the product. catalyst. The group VIII element content is between 1 and 10% by weight, preferably between 1.5 and 9% by weight, and more preferably between 2 and 8% expressed as Group VIII metal oxide with respect to weight. total catalyst. The molar ratio of Group VIII element to Group VIB element in the catalyst is preferably between 0.1 and 0.8, preferably between 0.15 and 0.6 and even more preferably between 0.2. and 0.5. The catalyst according to the invention advantageously also comprises phosphorus as a dopant. The dopant is an added element which in itself has no catalytic character but which increases the catalytic activity of the active phase.
[0014] The phosphorus content in said catalyst is preferably between 0.1 and 20% by weight expressed as P2O5, preferably between 0.2 and 15% by weight expressed as P2O5, and very preferably between 0.3 and 10% by weight. % weight expressed in P2O5. The phosphorus molar ratio on the group VIB element in the catalyst is greater than or equal to 0.05, preferably greater than or equal to 0.07, preferably between 0.08 and 1, preferably between 0, 08 and 0.7 and very preferably between 0.08 and 0.5. The catalyst according to the invention may advantageously also contain at least one dopant chosen from boron, fluorine and a mixture of boron and fluorine.
[0015] When the catalyst contains boron, the boron content is preferably between 0.1 and 10% by weight expressed as boron oxide, preferably between 0.2 and 7% by weight, and very preferably between 0, 2 and 5% weight. When the catalyst contains fluorine, the fluorine content is preferably between 0.1 and 10% by weight, expressed as fluorine, preferably between 0.2 and 7% by weight, and very preferably between 0.2 and 10% by weight. 5% weight When the catalyst contains boron and fluorine, the total content of boron and fluorine is preferably between 0.1 and 10% by weight expressed as boron oxide and fluorine, preferably between 0.2 and 7% by weight, and very preferably between 0.2 and 5% by weight.
[0016] The catalyst according to the invention comprises a support based on alumina or silica or silica-alumina. When the support of said catalyst is based on alumina, it contains more than 50% of alumina and, in general, it contains only alumina or silica-alumina as defined below.
[0017] Preferably, the support comprises alumina, and preferably extruded alumina. Preferably, the alumina is gamma alumina. The alumina support advantageously has a total pore volume of between 0.1 and 1.5 cm3g-1, preferably between 0.4 and 1.1 cm3g-1. The total pore volume is measured by mercury porosimetry according to ASTM D4284 with a wetting angle of 140 °, as described in Rouquerol F .; 3035600 11 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 device of the brand MicromériticsTM. The specific surface of the alumina support is advantageously between 5 and 400 m 2 g -1, preferably between 10 and 350 m 2 g -1, more preferably between 40 and 350 m 2. The specific surface is determined in the present invention by the method B.E.T according to ASTM D3663, method described in the same work cited above. In another preferred case, the support of said catalyst is a silica-alumina containing at least 50% by weight of alumina. The silica content in the support is at most 50% by weight, most often less than or equal to 45% by weight, preferably less than or equal to 40%. Silicon sources are well known to those skilled in the art. By way of example, mention may be made of silicic acid, silica in powder form or in colloidal form (silica sol), tetraethylorthosilicate Si (OEt) 4. When the support of said catalyst is based on silica, it contains more than 50% by weight of silica and, in general, it contains only silica. According to a particularly preferred variant, the support consists of alumina, silica or silica-alumina.
[0018] The support may also advantageously contain from 0.1 to 50% by weight of zeolite. In this case, all the zeolite sources and all the associated preparation methods known to those skilled in the art can be incorporated. Preferably, the zeolite is chosen from the group FAU, BEA, ISV, IWR, IWW, MEI, UWY and, preferably, the zeolite is chosen from the group FAU and BEA, such as zeolite Y and / or beta. In some particular cases, the support may also contain at least a portion of metal (s) VIB and VIII, and / or at least a portion of dopant (s) including phosphorus and / or at least one part of organic compound (s) containing oxygen (γ-ketovaleric or other acid) and / or nitrogen and / or sulfur which have been introduced outside impregnations (introduced for example during the preparation of the support). The support is advantageously in the form of balls, extrudates, pellets, or irregular and non-spherical agglomerates whose specific shape can result from a crushing step. The catalyst according to the invention also comprises γ-ketovaleric acid. The γ-ketovaleric acid has the following formula: The source of γ-ketovaleric acid can be derived from the traditional chemical industry with generally high purities. The acid can also come from the treatment of biomass, the product preferably containing mainly y-ketovaleric acid being purified or not before use. By way of example, mention may be made of the Biofine process (DJ Hayes, J. Ross, Hayes MHB, S. Fitzpatrick, Bioref.ind.Prod Prod, 1, 139-164, 2006) which allows starting from lignocellulose to produce before purification a mixture containing at least 50% by weight of y-ketovaleric acid, one of the major by-products being formic acid. The presence of γ-ketovaleric acid on the catalyst makes it possible to observe an increased activity with respect to the non-additive catalysts and the known additivated dried catalysts. The γ-ketovaleric acid content on the catalyst according to the invention is between 1 and 35% by weight, preferably between 2 and 30% by weight, and more preferably between 3 and 25% by weight relative to the total weight of the catalyst. . During the preparation of the catalyst, the drying step (s) consecutive to the introduction of the acid is (are) carried out at a temperature below 200 ° C. so as to preferably preserve at least 30%, preferably at least 50%, and most preferably at least 70% of the amount of acid added calculated on the basis of the carbon remaining on the catalyst. The catalyst according to the invention may comprise, in addition to γ-ketovaleric acid, another organic compound or a group of organic compounds known for their role as additives. The function of the additives is to increase the catalytic activity compared to the non-additive catalysts. More particularly, the catalyst according to the invention may further comprise one or more oxygen-containing organic compounds other than γ-ketovaleric acid and / or one or more nitrogen-containing organic compounds and / or one or more several organic compounds containing sulfur. Preferably, the catalyst according to the invention may further comprise one or more oxygen-containing organic compounds other than γ-ketovaleric acid and / or one or more nitrogen-containing organic compounds. Preferably, the organic compound contains at least 2 carbon atoms and at least one oxygen and / or nitrogen atom. Generally, the organic compound is chosen from a compound comprising one or more chemical functional groups chosen from a carboxylic function, alcohol, thiol, thioether, sulphone, sulphoxide, ether, aldehyde, ketone, ester, carbonate, amine, nitrile, imide, oxime, urea and amide. Preferably, the organic compound is selected from a compound having two alcohol functions and / or two carboxylic functions and / or two ester functions and / or at least one amide function. The oxygen-containing organic compound may be one or more of compounds having one or more chemical functions selected from a carboxylic, alcohol, ether, aldehyde, ketone, ester or carbonate function. For example, the organic oxygen-containing compound may be one or more selected from the group consisting of ethylene glycol, diethylene glycol, triethylene glycol, polyethylene glycol (with a molecular weight between 200 and 1500 g mol), propylene glycol, 2-butoxyethanol, 2- (2-butoxyethoxy) ethanol, 2- (2-methoxyethoxy) ethanol, triethylene glycol dimethyl ether, glycerol, acetophenone, 2,4-pentanedione, pentanone, acetic acid, maleic acid, malic acid, malonic acid, malic acid, oxalic acid, gluconic acid, tartaric acid, citric acid, succinate C1-C4 dialkyl, methyl acetoacetate, lactone, dibenzofuran, crown ether, orthophthalic acid, glucose and propylene carbonate. The nitrogen-containing organic compound may be one or more selected from compounds having one or more chemical functions selected from an amine or nitrile function. For example, the nitrogen-containing organic compound may be one or more selected from the group consisting of ethylenediamine, diethylenetriamine, hexamethylenediamine, triethylenetetramine, tetraethylenepentamine, pentaethylenehexamine, and the like. acetonitrile, octylamine, guanidine or carbazole. The organic compound containing oxygen and nitrogen may be one or more of the compounds having one or more chemical functional groups selected from a carboxylic acid, alcohol, ether, aldehyde, ketone, ester or carbonate function. amine, nitrile, imide, amide, urea or oxime. By way of example, the organic compound containing oxygen and nitrogen may be one or more selected from the group consisting of 1,2-cyclohexane diamine tetraacetic acid, monoethanolamine (MEA), N-methylpyrrolidone , dimethylformamide, ethylenediaminetetraacetic acid (EDTA), alanine, glycine, nitrilotriacetic acid (NTA), N- (2-hydroxyethyl) ethylenediamine-N, N ', N'-triacetic acid (HEDTA ), diethylenetriaminepentaacetic acid (DTPA), tetramethylurea, glutamic acid, dimethylglyoxime, bicine or tricine, or a lactam. The sulfur-containing organic compound may be one or more selected from compounds having one or more chemical functions selected from a thiol, thioether, sulfone or sulfoxide function. For example, the sulfur-containing organic compound may be one or more selected from the group consisting of thioglycolic acid, 2-hydroxy-4-methylthiobutanoic acid, a sulfonated derivative of a benzothiophene or a sulfoxidized derivative of a benzothiophene. Preferably, the organic compound contains oxygen, preferably it is selected from triethylene glycol, diethylene glycol, ethylenediaminetetraacetic acid (EDTA), maleic acid, citric acid, dimethylformamide, bicine, or tricine. Where (s) is / are present, the content of organic compound (s) with additive function (s) containing oxygen (other than γ-ketovaleric acid) and / or nitrogen and / or sulfur on the catalyst according to the invention is between 1 and 30% by weight, preferably between 1.5 and 25% by weight, and more preferably between 2 and 20% by weight relative to the total weight of the catalyst. Preparation Process The catalyst according to the invention can be prepared according to any method of preparation of a supported catalyst additive with an organic compound known to those skilled in the art. The catalyst according to the invention may be prepared according to a preparation process comprising the following steps: a) at least one component of a group VIB element, at least one component of a group VIII element, is contacted with γ-ketovaleric acid and optionally phosphorus with a support based on alumina or silica or silica-alumina, or is brought into contact a regenerated catalyst containing a support based on alumina or silica or silica at least one component of a group VIB element, at least one component of a group VIII element and optionally phosphorus with γ-ketovaleric acid, so as to obtain a catalyst precursor, ) said catalyst precursor from step a) is dried at a temperature below 200 ° C, without calcining it in the future. The process of preparing a fresh catalyst, followed by the method of preparing a rejuvenated catalyst, will be described first.
[0019] Process for the Preparation of a Fresh Catalyst Step a) of bringing into contact comprises several modes of implementation which are distinguished in particular by the moment of the introduction of the γ-ketovaleric acid which can be carried out either by at the same time as the impregnation of the metals (co5 impregnation), either after the impregnation of the metals (post-impregnation), or finally before the impregnation of the metals (pre-impregnation). In addition, the contacting step can combine at least two modes of implementation, for example co-impregnation and post-impregnation. These different modes of implementation will be described later. Each mode, taken alone or in combination, may take place in one or more steps. It is important to emphasize that the catalyst according to the invention during its preparation process does not undergo calcination after the introduction of ycétovalérique acid or any other organic compound containing oxygen and / or nitrogen and / or sulfur to preserve at least a part of the y-ketovaleric acid or other organic compound in the catalyst. The term "calcination" here means a heat treatment under a gas containing air or oxygen at a temperature greater than or equal to 200 ° C. However, the catalyst precursor may undergo a calcination step before the introduction of γ-ketovaleric acid or any other organic compound containing oxygen and / or nitrogen and / or sulfur, especially after the impregnation of the elements of group VIB and VIII (post-impregnation) optionally in the presence of phosphorus and / or another dopant or during a regeneration of a catalyst already used. The hydrogenating function comprising the group VIB and group VIII elements of the catalyst according to the invention, also called the active phase, is then in an oxide form. According to another variant, the catalyst precursor does not undergo a calcination step after the impregnation of the elements of group VIB and VIII (post-impregnation), it is simply dried. The hydrogenating function comprising the elements of group VIB and group VIII of the catalyst according to the invention, also called the active phase, is not then in an oxide form.
[0020] Whatever the embodiment, the contacting step a) generally comprises at least one impregnation step, preferably a dry impregnation step, in which the support is impregnated with a solution. impregnation agent comprising at least one group VIB element, at least one group VIII element, and optionally phosphorus. In the case of the co-impregnation described below in detail, this impregnation solution further comprises at least γ-ketovaleric acid. Group VIB and group VIII elements are generally introduced by impregnation, preferably by dry impregnation or by impregnation in excess of solution. Preferably, all the elements of group VIB and group VIII are introduced by impregnation, preferably by dry impregnation and this irrespective of the mode of implementation. Group VIB and group VIII elements may also be introduced in part during the shaping of said support at the time of mixing with at least one alumina gel chosen as a matrix, the rest of the hydrogenating elements then being introduced later by impregnation. Preferably, when the Group VIB and Group VIII elements are introduced in part at the time of mixing, the proportion of Group VIB element introduced during this step is less than 5% by weight of the total amount of element. of the VIB group introduced on the final catalyst. Preferably, the group VIB element is introduced at the same time as the group VIII element, regardless of the mode of introduction. Molybdenum precursors that can be used are well known to those skilled in the art. For 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 ( H3PMo12040) and their salts, and optionally silicomolybdic acid (H4SiMo12040) and its salts. Molybdenum sources may also be heteropoly compounds of the Keggin, Keggin lacunary, Keggin substituted, Dawson, Anderson, Strandberg type, for example.
[0021] Preferably, molybdenum trioxide and heteropolyanions of the Strandberg, Keggin, Keggin lacunary or substituted Keggin type are 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, oxides and hydroxides, tungstic acids and their salts, in particular ammonium salts such as ammonium tungstate, ammonium metatungstate, phosphotungstic acid and their salts, and optionally silicotungstic acid (H4SiW12O40) and its salts. The sources of tungsten may also be 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 precursors of the group VIII elements which may be used are advantageously selected from the oxides, hydroxides, hydroxycarbonates, carbonates and nitrates of the group VIII elements, for example, nickel hydroxycarbonate, carbonate or the like. cobalt hydroxide are used in a preferred manner. Phosphorus, when present, may be introduced in whole or in part by impregnation. Preferably, it is introduced by an impregnation, preferably dry, using a solution containing the precursors of Group VIB elements and Group VIII. Said phosphorus may be advantageously introduced alone or in admixture with at least one of the group VIB and group VIII elements, and this during any of the impregnation steps of the hydrogenating function if this is introduced in several times. Said phosphorus may also be introduced, all or part, during the impregnation of γ-ketovaleric acid if it is introduced separately from the hydrogenating function (case of the post-and pre-impregnation described later) and this in presence or absence of an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur. It can also be introduced as soon as the synthesis of the support, at any stage of the synthesis thereof. It can thus be introduced before, during or after the kneading of the chosen alumina gel matrix, such as for example and preferably the aluminum oxyhydroxide (boehmite) precursor of alumina.
[0022] The preferred phosphorus precursor is orthophosphoric acid H 3 PO 4, but its salts and esters such as ammonium phosphates are also suitable. Phosphorus may also be introduced together with the group VIB element (s) as Keggin, Keggin lacunary, Keggin substituted or Strandberg heteropolyanions.
[0023] The γ-ketovaleric acid is advantageously introduced into an impregnating solution which, according to the method of preparation, may be the same solution or a solution different from that containing the group VIB and VIII elements, in a corresponding total amount: at a molar ratio of γ-ketovaleric acid to group VIB element (s) of the catalyst precursor of between 0.2 to 2.0 mol / mol, preferably of between 0.3 to 1.7 mol / mol, preferably between 0.5 and 1.5 mol / mol and very preferably between 0.8 and 1.2 mol / mol, calculated on the basis of the components introduced into the solution (s) ) impregnation, and at a molar ratio of γ-ketovaleric acid by element (s) of Group VIII catalyst precursor of between 0.1 to 5.0 mol / mol, preferably between 0, From 5 to 4.0 mol / mol, preferably from 1.0 to 3.0 mol / mol and very preferably from s between 1.5 and 3.0 mol / mol, calculated on the basis of the components introduced into the impregnating solution (s). Any impregnation solution described in the present invention may comprise any polar solvent known to those skilled in the art. Said polar solvent used is advantageously chosen from the group formed by methanol, ethanol, water, phenol and cyclohexanol, taken alone or as a mixture. Said polar solvent may also advantageously be selected from the group consisting of 3035600 propylene carbonate, DMSO (dimethylsulfoxide), N-methylpyrrolidone (NMP) or sulfolane, alone or in admixture. Preferably, a polar protic solvent is used. A list of the usual polar solvents as well as their dielectric constant can be found in the book Solvents and Solvent Effects in Organic Chemistry, C. Reichardt, Wiley-VCH, 3rd edition, 2003, pages 472474. Very preferably, the The solvent used is water or ethanol, and particularly preferably the solvent is water. In one possible embodiment, the solvent may be absent in the impregnating solution. When the catalyst further comprises a dopant selected from boron, fluorine or a mixture of boron and fluorine, the introduction of this dopant (s) can be done in the same manner as the introduction of phosphorus. at various stages of preparation and in various ways. Said dopant may advantageously be introduced alone or as a mixture with at least one of the group VIB and group VIII elements, and this during any of the hydrogenation function impregnation steps if this is introduced in several times. Said dopant may also be introduced, in whole or in part, during the impregnation of the γ-ketovaleric acid if it is introduced separately from the hydrogenating function (as in the case of the post-and pre-impregnation described later) and this in presence or absence of an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur. It can also be introduced as soon as the synthesis of the support, at any stage of the synthesis thereof. It can thus be introduced before, during or after the kneading of the chosen alumina gel matrix, such as for example and preferably the aluminum oxyhydroxide (boehmite) precursor of alumina.
[0024] Said dopant, when there is one, is advantageously introduced in admixture with the precursor (s) of the elements of group VIB and of group VIII, in whole or in part on the support formed by an impregnation dry of said support with a solution, preferably aqueous, containing the precursors of the metals, the phosphorus precursor and the precursor (s) of the dopant (s), (and also containing γ-ketovaleric acid in the co-impregnation mode).
[0025] The boron precursors may be boric acid, orthoboric acid H3B03, biborate or ammonium pentaborate, boron oxide, boric esters. Boron may be introduced for example by a boric acid solution in a water / alcohol mixture or in a water / ethanolamine mixture. Preferably the boron precursor, if boron is introduced, is orthoboric acid. The fluorine precursors that can be used are well known to those skilled in the art. For example, the fluoride anions can be introduced in the form of hydrofluoric acid or its salts. These salts are formed with alkali metals, ammonium or an organic compound. In the latter case, the salt is advantageously formed in the reaction mixture by reaction between the organic compound and the hydrofluoric acid. The fluorine may be introduced for example by impregnation with an aqueous solution of hydrofluoric acid, or ammonium fluoride or ammonium bifluoride. When the catalyst further comprises an additional additive (in addition to γ-ketovaleric acid) or a further group of additives selected from an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur, it can be introduced into the impregnating solution of step a). The molar ratio of organic compound (s) containing oxygen and / or nitrogen and / or sulfur by group VIB element (s) on the catalyst is between 0.05 and 5 mol. mol, preferably between 0.1 to 4 mol / mol, preferably between 0.2 and 3 mol / mol, calculated on the basis of the components introduced into the impregnating solution (s). The molar ratio of organic compound (s) containing oxygen and / or nitrogen and / or sulfur by γ-ketovaleric acid is between 0.05 and 5 mol / mol, preferably included between 0.1 and 4 mol / mol, preferably between 0.2 and 3 mol / mol, calculated on the basis of the components introduced into the impregnating solution (s).
[0026] Advantageously, after each impregnation step, the impregnated support is allowed to mature. The maturation allows the impregnating solution to disperse homogeneously within the support. Any maturation step described in the present invention is advantageously carried out at atmospheric pressure, in an atmosphere saturated with water and at a temperature of between 17 ° C. and 50 ° C., and preferably at room temperature. Generally a ripening time of between ten minutes and forty-eight hours and preferably between thirty minutes and five hours, is sufficient. Longer durations are not excluded, but do not necessarily improve. According to step b) of the preparation process according to the invention, the catalyst precursor obtained in step a) optionally matured is subjected to a drying step at a temperature below 200 ° C without subsequent calcination step.
[0027] Any drying step subsequent to the introduction of γ-ketovaleric acid described in the present invention is carried out at a temperature below 200 ° C, preferably between 50 and 180 ° C, preferably between 70 and 150 ° C and most preferably between 75 and 130 ° C. The drying step 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. This step is preferably carried out at atmospheric pressure. It is advantageously carried out in crossed bed using air or any other hot gas. Preferably, when the drying is carried out in a fixed 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 nitrogen and / or air. Preferably, the drying step has a short duration of between 5 minutes and 4 hours, preferably between 30 minutes and 4 hours and very preferably between 1 hour and 3 hours. Drying is then carried out so as to preferentially retain at least 30% of the γ-ketovaleric acid introduced during an impregnation step, preferably this amount is greater than 50% and even more preferably greater than at 70%, calculated on the basis of the carbon remaining on the catalyst. When an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur is present, the drying step is carried out so as to preferably retain at least 30 %, preferably at least 50%, and very preferably at least 70% of the amount added calculated on the basis of the carbon remaining on the catalyst. At the end of drying step b), a dried catalyst is obtained which is not subjected to any subsequent calcination step. Co-impregnation According to a first embodiment of step a) of the catalyst preparation process (fresh), the said components of the elements of group VIB, of group VIII, of y-ketovaleric acid are deposited. and optionally phosphorus on said support, by one or more steps of co-impregnation, that is to say that said components of the elements of group VIB, group VIII, y-ketovaleric acid and optionally phosphorus are introduced simultaneously into said support ("co-impregnation"). According to one variant, step a) is the following step: a) a support based on alumina or silica or silica-alumina is impregnated with at least one solution containing at least one group VIB element, at least one group VIII element, γ-ketovaleric acid and optionally phosphorus so as to obtain a catalyst precursor.
[0028] The co-impregnation stage (s) is (are) preferably carried out by dry impregnation or impregnation in excess of solution. When this first embodiment comprises the implementation of several co-impregnation steps, each co-impregnation step is preferably followed by an intermediate drying step at a temperature below 200 ° C., advantageously between 50 and 180 ° C. ° C, preferably between 70 and 150 ° C, very preferably between 75 and 130 ° C and optionally a period of maturation was observed between the impregnation and drying. Very preferably, during the preparation via co-impregnation, the elements of group VIB and of group VIII, γ-ketovaleric acid, optionally phosphorus, optionally another dopant selected from boron and / or fluorine and optionally an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur are introduced in step a) in full after the shaping of said support, by impregnation dry of said support with an aqueous impregnating solution containing the precursors of group VIB elements and of group VIII, γ-ketovaleric acid, optionally the phosphorus precursor, optionally the dopant precursor chosen from boron and / or fluorine and optionally the organic compound other than y-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur.
[0029] Post-impregnation According to a second embodiment of step a) of the process for preparing the (fresh) catalyst according to the invention, at least γ-ketovaleric acid is brought into contact with a dried impregnated support and optionally calcined comprising at least one component of a group VIB element, at least one component of a group VIII element and optionally phosphorus, said support being based on alumina or silica or silica-alumina, to obtain a catalyst precursor. This second embodiment is a "post-impregnation" preparation of γ-ketovaleric acid. This is carried out for example by dry impregnation. According to this second embodiment, the contacting according to step a) comprises the following successive steps which will be detailed below: 3035600 25 a1) is impregnated with a support based on alumina or silica or silica-alumina by at least one solution containing at least one element of group VIB, at least one element of group VIII and optionally phosphorus to obtain an impregnated support, 5 a2) the impregnated support obtained in step a1) is dried in a temperature below 200 ° C to obtain a dried impregnated support, and optionally the dried impregnated support is calcined to obtain a calcined impregnated support, a3) the dried and optionally calcined impregnated support obtained in step a2) is impregnated with impregnation solution comprising at least γ-ketovaleric acid so as to obtain a catalyst precursor, a4) optionally, the precursor of the catalyst obtained is allowed to mature. ape a3).
[0030] In step a1) of the implementation by post-impregnation, the introduction of the elements of group VIB and group VIII and possibly phosphorus on the support can be advantageously carried out by one or more impregnations in excess of solution on the support, or preferably by one or more dry impregnation, and, preferably, by a single dry impregnation of said support, using solution (s), preferably aqueous (s), containing the or metal precursors and preferably the phosphorus precursor. When carrying out several impregnation steps, each impregnation step is preferably followed by an intermediate drying step at a temperature below 200 ° C., advantageously between 50 and 180 ° C., preferably between 70 and 70 ° C. i50 ° C, very preferably between and i30 ° C and optionally a period of maturation was observed between the impregnation and drying. Each intermediate drying step, prior to the introduction of ycetovaleric acid may be followed by a calcination step under the conditions described below for step a2).
[0031] Very preferably, during the post-impregnation preparation, the elements of group VIB and group VIII and optionally phosphorus, optionally another dopant selected from boron and / or fluorine and optionally an organic compound other than the γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur are introduced in step a1) in their entirety after the shaping of said support, by dry impregnation of said support to using an aqueous impregnation solution containing the precursors of group VIB and group VIII elements, the phosphorus precursor, and optionally the dopant precursor chosen from boron and / or fluorine and optionally the organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur. According to another variant, the elements of group VIB and group VIII and optionally phosphorus, optionally another dopant selected from boron and / or fluorine and optionally an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur can be introduced in step a1) successively by several impregnating solutions containing one or more of the components. Advantageously, the impregnated support obtained in step a1) is allowed to mature under the conditions described for the above ripening.
[0032] According to step a2), the impregnated support obtained in step a1) is dried at a temperature below 200 ° C to obtain a dried impregnated support under the conditions described for drying above. Optionally, the dried impregnated support can then be calcined.
[0033] The calcination is generally carried out at a temperature between 200 ° C and 900 ° C, preferably between 250 ° C and 750 ° C. The calcination time is generally between 0.5 hours and 16 hours, preferably between 1 hour and 5 hours. It is usually done under air. Calcination makes it possible to convert the precursors of Group VIB and VIII metals into oxides.
[0034] According to step a3), the dried impregnated support obtained in step a2) is impregnated with an impregnating solution comprising at least γ-ketovaleric acid so as to obtain a catalyst precursor.
[0035] The γ-ketovaleric acid may advantageously be deposited in one or more stages either by excess impregnation, or by dry impregnation, or by any other means known to those skilled in the art. Preferably, the γ-ketovaleric acid is introduced in dry impregnation, in the presence or absence of a solvent as described above.
[0036] Preferably, the solvent in the impregnating solution used in step a3) is water, which makes it easier to use on an industrial scale. The γ-ketovaleric acid is advantageously introduced into the impregnation solution of step a3) with the molar ratios per element of group VIB or group VIII described above.
[0037] When it is desired to further introduce an additional additive (in addition to γ-ketovaleric acid) or a further group of additives selected from an organic compound containing oxygen and / or nitrogen and / or sulfur, it can be introduced into the impregnation solution of step a1) and / or into the impregnation solution of step a3) or by an additional impregnation step to any time of the preparation process before the final drying of step b) it being understood that no calcination step is carried out after its introduction. This compound is introduced in the proportions described above.
[0038] According to step a4), the catalyst precursor obtained in step a3) is optionally allowed to mature, and this under the ripening conditions described above. According to step b) of the preparation process according to the invention, the catalyst precursor which has optionally been matured in step a4) is subjected to a drying step at a temperature below 200 ° C. without subsequent calcination step as described above. Pre-impregnation According to a third embodiment of step a) of the catalyst preparation process (fresh) according to the invention, at least one component of a group VIB element is brought into contact, at least a component of a group VIII element, optionally phosphorus with the support based on alumina or silica or silica-alumina which contains γ-ketovaleric acid so as to obtain a catalyst precursor.
[0039] This third embodiment is a "pre-impregnation" preparation of γ-ketovaleric acid. This is carried out for example by dry impregnation. According to this third embodiment, the contacting according to step a) comprises the following successive steps which will be detailed hereinafter: a) is prepared a support comprising at least γ-ketovaleric acid and optionally at least a portion of the phosphorus, a2 ') is impregnated the support obtained in step a1') by an impregnating solution comprising at least one element of group VIB, at least one element of group VIII and optionally phosphorus of In order to obtain a catalyst precursor, a3 ') optionally, the catalyst precursor obtained in step a2') is allowed to mature. In step a1 ') of the implementation by pre-impregnation, a support comprising at least γ-ketovaleric acid and optionally at least part of the phosphorus is prepared. The γ-ketovaleric acid can be introduced at any time during the preparation of the support, and preferably during the shaping or by impregnation on a support already formed. If the introduction of γ-ketovaleric acid to the previously formed carrier is chosen, then this can be carried out as indicated for step a3) of post-impregnation. It will then be followed by an optional ripening step and drying at a temperature below 200 ° C under the conditions of ripening and drying as described above. If we choose the introduction during the shaping, preferably, said shaping is performed by extrusion kneading, by pelletizing, by the method of coagulation in drop (oil-drop according to the English terminology) , by rotating plate granulation or by any other method well known to those skilled in the art. In a very preferred manner, said shaping is carried out by extrusion kneading, the y-ketovaleric acid being able to be introduced at any time during extrusion kneading. The formed material obtained at the end of the shaping step is then advantageously subjected to a heat treatment step at a temperature such that at least a part of the γ-ketovaleric acid remains present. It is the same for the phosphorus possibly present in said support 15 of step a1 '). The phosphorus may be introduced at any time during the preparation of the support, and preferably during the shaping or by impregnation on a support already formed as described above. If the phosphorus is introduced alone to the shaping, that is to say without the γ-ketovaleric acid itself then introduced by impregnation, the calcination temperature subsequent to its introduction can then advantageously be carried out at a temperature of about 50.degree. temperature below 1000 ° C. In step a2 ') of the implementation by pre-impregnation, the introduction of group VIB and group VIII elements and optionally phosphorus can be advantageously carried out by one or more impregnations in excess of solution on the support, or preferably by one or more dry impregnations, and preferably by a single dry impregnation of said support, using solution (s), preferably aqueous (s), containing the precursor (s) metals and possibly the phosphorus precursor. Advantageously, the catalyst precursor obtained in step a2 ') is allowed to mature under the conditions of maturation described above.
[0040] When it is desired to further introduce an additional additive (in addition to γ-ketovaleric acid) or a further group of additives selected from an organic compound containing oxygen and / or nitrogen and / or sulfur, it can be introduced into the support of step a1 ') during shaping or impregnation, and / or in the impregnating solution of step a2') or by a additional impregnation stage at any time of the preparation process before the final drying of step b), it being understood that no calcination step is carried out after its introduction. The three modes described above may be carried out alone as described or mixed to give rise to other hybrid preparation modes depending on the technical and practical constraints. According to another alternative embodiment, the contacting according to step a) combines at least two contacting modes, for example the co-impregnation of an organic compound and the post-impregnation of an organic compound which can be identical or different from that used for co-impregnation, since at least one of the organic compounds is ycetovaleric acid. According to this alternative embodiment, the contacting according to step a) comprises the following successive steps: (a) a solution containing at least one element of group VIB is contacted by co-impregnation, at least a group VIII element, at least one organic compound containing oxygen and / or nitrogen and / or sulfur, and optionally phosphorus with a support based on alumina or silica or silica-alumina; in order to obtain an impregnated support, a2 ") the impregnated support from step a1" ") is dried at a temperature below 200 ° C., without subsequently calcining it to obtain a dried impregnated support, a3"). contact the dried impregnated support from step a2 ") with a solution of an organic compound containing oxygen and / or nitrogen and / or sulfur identical or different from that used in step a1 ") so as to obtain a catalyst precursor, a4") opti optionally, the catalyst precursor obtained in step a3 ") is allowed to mature. And at least one of the organic compounds of step a1 "- or step a3") is γ-ketovaleric acid. The operating conditions described above are of course applicable in the context of this latter embodiment. Process for preparing a rejuvenated catalyst The catalyst according to the invention may be a rejuvenated catalyst. This catalyst may be prepared according to the preparation process comprising the following steps: a) a regenerated catalyst containing a support based on alumina or silica or silica-alumina is contacted with at least one component of an element group VIB, at least one component of a group VIII element and optionally phosphorus, with γ-ketovaleric acid so as to obtain a catalyst precursor, b) drying said catalyst precursor resulting from the step a) at a temperature below 200 ° C, without calcining it later.
[0041] According to step a), a regenerated catalyst is contacted with ycetovaleric acid so as to obtain a catalyst precursor. The regenerated catalyst is a catalyst which has been used as a catalyst in a catalytic unit and in particular in hydrotreatment and / or hydrocracking and which has been subjected to at least one calcination step in order to burn the coke (regeneration). The regeneration allows the combustion of the carbon deposited on the catalyst during its industrial use. It can be performed by any means known to those skilled in the art. The regeneration is generally carried out at temperatures between 350 and 550 ° C, and most often between 400 and 520 ° C, or between 420 ° C and 520 ° C, or between 450 ° C and 520 ° C, lower temperatures. at 500 ° C being often advantageous. The regenerated catalyst contains a support based on alumina or silica or silica-alumina, at least one component of a group VIB element, at least one component of a group VIII element and optionally with phosphorus in the respective proportions indicated above. Following the regeneration (calcination step) the hydrogenating function comprising the elements of group VIB and group VIII of the regenerated catalyst is in an oxide form. It may also contain other dopants than phosphorus, as described above.
[0042] According to this embodiment, the contacting according to step a) comprises the following successive steps: a) a regenerated catalyst containing a support based on alumina or silica or silica-alumina is impregnated; at least one component of a group VIB element, at least one component of a Group VIII element and optionally phosphorus by an impregnating solution comprising at least γ-ketovaleric acid so as to obtain a precursor of catalyst, a2 ") optionally, the catalyst precursor obtained in step a" ') is allowed to mature.
[0043] Preferably, the contacting of step a) is carried out by impregnating the regenerated catalyst with an impregnating solution comprising at least γ-ketovaleric acid so as to obtain a catalyst precursor. The γ-ketovaleric acid may advantageously be deposited in one or more stages, either by excess impregnation or by dry impregnation, or by any other means known to those skilled in the art. Preferably, the γ-ketovaleric acid is introduced in dry impregnation, in the presence or absence of a solvent as described above. Preferably, the solvent in the impregnating solution used is water, which facilitates the implementation on an industrial scale.
[0044] The γ-ketovaleric acid is advantageously introduced into the impregnating solution with the molar ratios per element of group VIB or group VIII described above. When it is desired to further introduce an additional additive (in addition to γ-ketovaleric acid) or a further group of additives selected from an organic compound containing oxygen and / or nitrogen and / or sulfur, it can be introduced into the impregnation solution of step a "") or by a further impregnation step at any time of the preparation process before the final drying stage b) it being understood that no calcination step is carried out after it has been introduced This compound is introduced in the proportions described above According to step a 2 "), the catalyst precursor obtained is optionally allowed to mature. in step al '' '), and this under the ripening conditions described above.
[0045] According to step b) of the preparation process according to the invention, the catalyst precursor which has been optionally matured in step a2 ") is subjected to a drying step at a temperature below 200 ° C. without Subsequent calcination step, as described above Sulfurization Before use for the hydrotreatment and / or hydrocracking reaction, it is advantageous to convert the dried catalyst obtained according to any of the described modes of introduction. In the present invention, a sulphurized catalyst is used to form its active species.This activation or sulphurization step is carried out by methods well known to those skilled in the art, and advantageously under a sulpho-reducing atmosphere. presence of hydrogen and hydrogen sulfide.
[0046] At the end of step b) according to the different modes of preparation of the process according to the invention, said catalyst obtained is therefore advantageously subjected to a sulphidation step, without intermediate calcination step. Said dried catalyst is advantageously sulphurized ex situ or in situ.
[0047] The sulfurizing agents are H2S gas or any other sulfur-containing compound used for activating the hydrocarbon feeds to sulphurize the catalyst. Said sulfur-containing compounds are advantageously chosen from alkyl disulfides such as, for example, dimethyl disulphide (DMDS), alkyl sulphides, for example dimethyl sulphide, thiols such as, for example, dimethyl disulfide. butyl mercaptan (or 1-butanethiol), polysulfide compounds tertiononylpolysulfide type, or any other compound known to those skilled in the art for obtaining a good sulfuration of the catalyst. Preferably, the catalyst is sulfided in situ in the presence of a sulfurizing agent and a hydrocarbon feedstock. Most preferably the catalyst is sulfided in situ in the presence of a hydrocarbon feed additive of dimethyl disulfide. Process for hydrotreatment and / or hydrocracking Finally, another subject of the invention is the use of the catalyst according to the invention or prepared according to the preparation process according to the invention in hydrotreatment and / or hydrocracking processes. of hydrocarbon cuts.
[0048] The catalyst according to the invention, preferably having previously undergone a sulfurization step, is advantageously used for the hydrotreatment and / or hydrocracking reactions of hydrocarbonaceous feedstocks such as petroleum cuts, coal cuts or the hydrocarbons produced. from natural gas, optionally in mixtures or from a hydrocarbon fraction derived from biomass and more particularly for hydrogenation, hydrodenitrogenation, hydrodearomatization, hydrodesulphurization, hydrodeoxygenation, hydrogenation reactions, hydrodemetallization or hydroconversion of hydrocarbon feedstocks.
[0049] In these uses, the catalyst according to the invention and having preferably previously undergone a sulphurization step has an improved activity compared to the catalysts of the prior art. This catalyst can also advantageously be used during the pretreatment of catalytic cracking or hydrocracking feeds, or the hydrodesulfurization of residues or the high hydrodesulfurization of gas oils (ULSD Ultra Low Sulfur Diesel according to the English terminology). The feedstocks employed in the hydrotreatment process are, for example, gasolines, gas oils, vacuum gas oils, atmospheric residues, vacuum residues, atmospheric distillates, vacuum distillates, heavy fuels, oils, waxes and paraffins, waste oils, residues or deasphalted crudes, fillers derived from thermal or catalytic conversion processes, lignocellulosic fillers or more generally biomass feedstocks, alone or as a mixture. The feeds which are treated, and in particular those mentioned above, generally contain heteroatoms such as sulfur, oxygen and nitrogen and, for heavy feedstocks, they most often also contain metals. The operating conditions used in the processes employing the hydrotreatment reactions of hydrocarbon feedstocks described above are generally as follows: the temperature is advantageously between 180 and 450 ° C., and preferably between 250 and 440 ° C., the pressure is advantageously between 0.5 and 30 MPa, and preferably between 1 and 18 MPa, the hourly space velocity is advantageously between 0.1 and 20 h -1 and preferably between 0.2 and 5 h -1 and the ratio hydrogen / charge expressed as a volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid charge is advantageously between 501/50001 / let preferably 80 to 20001/1. According to a first mode of use, said hydrotreatment process according to the invention is a hydrotreatment process, and in particular hydrodesulfurization (HDS) of a gas oil fraction carried out in the presence of at least one catalyst according to the invention. 'invention. Said hydrotreatment process according to the invention aims at eliminating the sulfur compounds present in said diesel fuel cup so as to reach the environmental standards in force, namely an allowed sulfur content of up to 10 ppm. It also makes it possible to reduce the aromatics and nitrogen contents of the diesel fraction to be hydrotreated. Said gasoil fraction to be hydrotreated according to the process of the invention contains from 0.02 to 5.0% by weight of sulfur. It is advantageously derived from the direct distillation (or straight run diesel according to the English terminology), a coking unit (coking according to the English terminology), a visbreaking unit (visbreaking according to the English terminology). -saxonne), a steam cracking unit (steam cracking according to the English terminology), a hydrotreating unit and / or hydrocracking heavier charges and / or a catalytic cracking unit (Fluid Catalytic Cracking according to Anglo-Saxon terminology). Said gasoil fraction preferably has at least 90% of the compounds whose boiling point is between 250 ° C. and 400 ° C. at atmospheric pressure. The process for hydrotreating said diesel fuel cutter according to the invention is carried out under the following operating conditions: a temperature of between 200 and 400 ° C., preferably between 300 and 380 ° C., a total pressure of between 2 MPa and 10 ° C. MPa and more preferably between 3 MPa and 8 MPa with a volume ratio of hydrogen per volume of hydrocarbon feedstock, expressed as volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid feed, of between 100 and 600 liters per liter and more preferably between 200 and 400 liters per liter and an hourly space velocity of between 1 and 10 h -1, preferably between 2 and 8 1-1-1. The VVH corresponds to the inverse of the contact time expressed in hours and is defined by the ratio of the volume flow rate of the liquid hydrocarbon feedstock by the volume of catalyst charged to the reaction unit implementing the hydrotreatment process according to the invention. invention. The reaction unit implementing the hydrotreatment method of said gasoil fraction according to the invention is preferably carried out in a fixed bed, in a moving bed or in a bubbling bed, preferably in a fixed bed. According to a second mode of use, said hydrotreatment and / or hydrocracking process according to the invention is a hydrotreatment process (in particular hydrodesulfurization, hydrodeaazoation, hydrogenation of aromatics) and / or hydrocracking of a cut. vacuum distillate produced in the presence of at least one catalyst according to the invention. Said hydrotreatment and / or hydrocracking process, otherwise known as the hydrocracking or hydrocracking pretreatment method according to the invention, is intended, depending on the case, to eliminate the sulfur, nitrogen or aromatic compounds present in said distillate cut so as to perform pre-treatment before conversion to catalytic cracking or hydroconversion processes, or to hydrocrack the distillate cut that may have been previously pretreated if necessary.
[0050] A wide variety of feeds can be processed by the hydrotreatment and / or hydrocracking processes of vacuum distillates described above. Generally they contain at least 20% volume and often at least 80% volume of compounds boiling above 340 ° C at atmospheric pressure. The feedstock may be, for example, vacuum distillates as well as feeds from aromatic extraction units of lubricating oil bases or from solvent dewaxing of lubricating oil bases, and / or oils. deasphalted, or the filler may be a deasphalted oil or paraffins from the Fischer-Tropsch process or any mixture of the aforementioned fillers. In general, the feeds have a T5 boiling point of greater than 340 ° C at atmospheric pressure, and even better than 370 ° C at atmospheric pressure, ie 95% of the compounds present in the feed have a boiling point above 340 ° C, and more preferably above 370 ° C. The nitrogen content of the feeds treated in the processes according to the invention is usually greater than 200 ppm by weight, preferably between 500 and 10,000 ppm by weight. The sulfur content of the feeds treated in the processes according to the invention is usually between 0.01 and 5.0% by weight. The filler may optionally contain metals (for example nickel and vanadium). The asphaltene content is generally less than 3000 ppm by weight.
[0051] The hydrotreatment and / or hydrocracking catalyst is generally brought into contact, in the presence of hydrogen, with the charges described above, at a temperature above 200 ° C., often between 250 ° C. and 480 ° C., advantageously between 320 ° C. and 450 ° C., preferably between 330 ° C. and 435 ° C., under a pressure greater than 1 MPa, often between 2 and 10 MPa, preferably between 3 and 20 MPa, the speed volume ranging from 0.1 to 20.0 h -1 and preferably 0.1 to 6.0 h -1, preferably 0.2 to 3.0 h -1, and the amount of hydrogen introduced is such that the volume ratio hydrogen liter / liter of hydrocarbon, expressed as volume of hydrogen, measured under normal conditions of temperature and pressure, per volume of liquid charge, is between 80 and 5000 1/1 and most often between 100 and 2000 1/1. These operating conditions used in the processes according to the invention generally make it possible to achieve pass conversions, products having boiling points below 340 ° C. at atmospheric pressure, and better still below 370 ° C. at atmospheric pressure, which are higher than at 15% d even more preferably between 20 and 95%. The processes for hydrotreatment and / or hydrocracking of vacuum distillates using the catalysts according to the invention cover the pressure and conversion ranges from mild hydrocracking to high pressure hydrocracking. By mild hydrocracking is meant hydrocracking leading to moderate conversions, generally less than 40%, and operating at low pressure, generally between 2 MPa and 6 MPa. The catalyst according to the invention can be used alone, in one or more fixed bed catalytic beds, in one or more reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the unconverted fraction. or in a two-step hydrocracking scheme, optionally in combination with a hydrorefining catalyst located upstream of the catalyst of the present invention. According to a third mode of use, said hydrotreatment and / or hydrocracking process according to the invention is advantageously used as pretreatment in a fluidized-bed catalytic cracking process (or FCC method for Fluid Catalytic Cracking according to US Pat. Anglo-Saxon terminology). The pretreatment operating conditions in terms of temperature range, pressure, hydrogen recycle rate, hourly space velocity are generally the same as those described above for hydrotreatment and / or hydrocracking processes of vacuum distillates. . The FCC process can be carried out in a conventional manner known to those skilled in the art under the appropriate cracking conditions to produce lower molecular weight hydrocarbon products. For example, a brief description of catalytic cracking can be found in ULLMANS ENCYCLOPEDIA OF INDUSTRIAL CHEMISTRY VOLUME A 18, 1991, pages 61 to 64. According to a fourth mode of use, said process for hydrotreatment and / or hydrocracking according to US Pat. The invention is a process for hydrotreating (in particular hydrodesulphurization) a gasoline cut in the presence of at least one catalyst according to the invention.
[0052] In contrast with other hydrotreatment processes, the hydrotreatment (in particular the hydrodesulfurization) of the species must 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 in order to limit the loss of octane number.
[0053] The feedstock is generally a hydrocarbon cut having a distillation range of from 30 to 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).
[0054] The hydrotreatment process consists of bringing the hydrocarbon fraction into contact with the catalyst according to the invention and with hydrogen under the following conditions: at a temperature of between 200 and 400 ° C., preferably between 230 and At 330 ° C., at a total concentration of between 1 and 5 MPa, preferably between 1.5 and 2.5 MPa, at a Time Volumetric Velocity (VVH), defined as the volume flow rate of charge relative to the volume of catalyst, between 1 and 10 h -1, preferably between 2 and 6 h -1 and at a volume ratio hydrogen / gasoline load between 100 and 600 NI / 1, preferably between 200 and 400 NI / 1.
[0055] The process for the hydrotreatment of gasolines 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 hydrodesulphurization reactor. The following examples demonstrate the significant increase in activity on the catalysts prepared according to the process according to the invention compared to the catalysts of the prior art and specify the invention without however limiting its scope.
[0056] EXAMPLES EXAMPLE 1 Preparation of CoMoP catalysts on alumina without organic compounds C1 and C2 (not in accordance with the invention). On an alumina support having a BET surface of 230 m 2 / g, a pore volume obtained by mercury porosimetry of 0.78 ml / g and a mean pore diameter of 11.5 nm defined as the median diameter by volume. by mercury porosimetry and which is in the form "extruded", cobalt, molybdenum and phosphorus are added. The impregnating solution is prepared by dissolving 90 ° C. of molybdenum oxide (2434 g) and cobalt hydroxide (5.34 g) in 7.47 g of a 85% phosphoric acid solution. % in water. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 90 ° C for 16 hours. The dried catalyst precursor thus obtained is denoted C1. Calcination of catalytic precursor Cl at 450 ° C for 2 hours leads to calcined catalyst C2. The final composition of the catalysts C1 and C2 expressed in the form of oxides and referred to the dry catalyst mass is then as follows: MoO3 = 22.5 ± 0.2% by weight, CoO = 4.1 ± 0.1% by weight and P2O5 = 4.0 ± 0.1% by weight. EXAMPLE 2 Preparation of CoMoP catalysts on alumina C3 and C4 (not in accordance with the invention), and C5 (in accordance with the invention) by co-impregnation.
[0057] On the alumina support previously described in Example 1 and which is in the "extruded" form, cobalt, molybdenum and phosphorus are added. The impregnating solution is prepared by dissolving molybdenum oxide (28.13 g) and cobalt hydroxide (6.62 g) at 90 ° C. in 7.88 g of a phosphoric acid solution. 85% in water. After homogenization of the above mixture, 37.79 g of citric acid was added before adjusting the volume of solution to the pore volume of the support by addition of water. The molar ratio (citric acid) / Mo is equal to 1 mol / mol and that (citric acid) / Co is equal to 2.8 mol / mol. After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 120 ° C for 16 hours. The dried catalyst precursor thus obtained is denoted C3. The final composition of the catalyst C3, expressed as oxides and relative to the dry catalyst mass is then as follows: MoO3 = 22.7 ± 0.2% by weight, CoO = 4.2 ± 0.1% by weight and P2O5 = 3.8 ± 0.1% by weight. Catalyst C4 is prepared analogously to catalyst C3, but after homogenization of the metal solution containing cobalt, molybdenum and phosphorus, triethylene glycol (TEG) is added, again in a proportion of 1 mole per mole of molybdenum. or 2.8 moles per mole of cobalt. Catalyst C4 was allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 120 ° C for 16 hours. The final composition of the catalyst C4, expressed in the form of oxides and based on the dry catalyst mass, is then as follows: Mo03 = 22.6 ± 0.2% by weight, CoO = 4.1 ± 0.1% by weight and P2O5 = 3.9 ± 0.1% by weight.
[0058] Catalyst C5 according to the invention is prepared as follows. On the alumina support described in Example 1 and which is in the "extruded" form, cobalt, molybdenum and phosphorus are added. An impregnating solution was prepared by dissolving 90 ° C of molybdenum oxide (78.75 g) and cobalt hydroxide (18.54 g) in 22.08 g of an acid solution. 85% phosphoric in water. After homogenization of the above mixture, γ-ketovaleric acid was added to the solution in equimolar proportion relative to the molybdenum, ie 2.8 moles per mole of cobalt before adjusting the volume of the solution to the pore volume of the support by addition. of water. After dry impregnation, the catalyst extrudates were allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 120 ° C for 16 hours. The final composition of the catalyst C5, expressed in oxide form and relative to the dry catalyst mass, is then as follows: MoO 3 = 22.4 ± 0.2% by weight, CoO = 4.0 ± 0.1% by weight and P2O 5 = 4.0 ± 0.1% by weight. Example 3 Preparation of the CoMoP catalyst on C6 alumina (according to the invention) by pre-impregnation. On the alumina support described above in Example 1 and which is in the "extruded" form, 24.7 g of the y-ketovaleric acid diluted in water are added in order to obtain a volume solution. total equal to the pore volume of the support. The solution thus formed is then dry-impregnated onto the support before a maturation time of 3 hours in a saturated atmosphere of water and at room temperature, followed by drying at 120 ° C. for 2 hours. The modified support is then impregnated with a new impregnating solution prepared by hot dissolving molybdenum oxide (27.00 g) and 3035600 cobalt (6.36 g) hydroxide in 7.57 g. 85% phosphoric acid solution in water, taking care to adjust by adding water the volume of the latter solution to the pore volume of the previous modified support. After dry impregnation, the extrudates were allowed to mature in a saturated water atmosphere for 3 h at room temperature and then dried at 120 ° C for 16 hours to yield catalyst C6. The final composition of the catalyst C6, expressed in oxide form and relative to the mass of dry catalyst, is then as follows: MoO 3 = 22.5 ± 0.2% by weight, CoO = 4.1 ± 0.1% by weight and P2O5 = 4.0 ± 0.1 (wt%) The quantities involved are such that the amount of γ-ketovaleric acid is one mole per mole of molybdenum and 2.8 moles per mole of cobalt. Preparation of CoMoP catalysts on alumina C7 (not in accordance with the invention) and C8 (according to the invention) by co-impregnation (low organic compound ratio / Mo) On the alumina support described above in Example 1 and In the "extruded" form, cobalt, molybdenum and phosphorus are added as for the preparation of the catalyst C 3, but when preparing the impregnating solution, the citric acid / molybdenum molar ratio is here equal to 0.25 mol / mol, ie 0.70 mole of citric acid per mole of cobalt After dry impregnation, the extrudates are allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 120 ° C for 16 hours. The dried catalyst precursor thus obtained is denoted C7. The final composition of catalyst C7, expressed in the form of oxides and based on the dry catalyst mass, is then as follows: Mo03 = 22.5 ± 0.2% by weight, CoO = 4.0 ± 0.1% by weight and P2O5 = 3.9 ± 0.1% by weight).
[0059] On the alumina support described above in Example 1 and which is in the "extruded" form, cobalt, molybdenum and phosphorus are added as for the preparation of catalyst C5. However, during the preparation of the impregnation solution, the mole ratio of γ-ketovaleric acid to molybdenum relative to 3035600 was set at 0.25 mol / mol, ie 0.70 mole of γ-ketovaleric acid. per mole of cobalt. After dry impregnation, the extrudates were allowed to mature in a saturated water atmosphere for 12 hours at room temperature and then dried at 120 ° C for 16 hours. The dried catalyst precursor thus obtained is denoted C8. The final composition of the catalyst C8 expressed in the form of oxides and based on the mass of dry catalyst is then as follows: MoO 3 = 22.3 ± 0.2% by weight, CoO = 4.1 ± 0.1% by weight and P2O 5 = 4.3 ± 0.1% by weight. EXAMPLE 5 Evaluation of Diesel Catalyst HDS Catalysts C1, C2, C3, C4, and C7 (not in Accordance with the Invention) and C5, C6 and C8 (in Accordance with the Invention) Catalysts C1, C2, C3 C4 and C7 (not in accordance with the invention) and C5, C6, C8 (in accordance with the invention) were tested in diesel HDS. Characteristics of the diesel fuel used: - Density at 15 ° C: 0.8522 g / cm3 15 - Sulfur: 1.44% by weight - Simulated Distillation: - PI: 155 ° C - 10%: 247 ° C - 50% : 315 ° C 20 - 90%: 392 ° C - mp: 444 ° C The test is conducted in a fixed bed isothermal pilot reactor crossed, the fluids flowing from bottom to top. After sulfurization in situ at 350 ° C. in the unit under pressure using the test gas oil, to which 2% by weight of dimethyl disulphide is added, the hydrodesulfurization test was carried out under the following operating conditions: a total pressure of 7 MPa, a catalyst volume of 30 cm3, a temperature of 330 to 360 ° C, a hydrogen flow rate of 241 / h and a feed rate of 60 cm3 / h.
[0060] The catalytic performances of the catalysts tested are given in Table 1. They are expressed in degrees Celsius from a comparative catalyst chosen as reference (C2): they correspond to the temperature difference to be applied to reach 50 ppm of sulfur. in the effluent. A negative value means that the sulfur target is reached for a lower temperature and thus there is a gain in activity. A positive value means that the target of sulfur content is reached for a higher temperature and that there is therefore a loss of activity. The results obtained are reported in Table 1.
[0061] Table 1 clearly shows the gain on the catalytic effect provided by ycetovaleric acid. Indeed, the catalysts C5 and C6 (according to the invention) have higher activities than those obtained for all other catalysts evaluated at the same molar proportions of organic compound (1 mol / molmo). The gain is also maximized, at the same amount of additive, the catalyst C5 is more active than the catalysts C3 and C4 respectively obtained with citric acid or TEG and which are 4.7 ° C and 2.5 ° C less active. The activity of the catalyst C6 remains much greater than that of the base catalyst C2 or of a dried catalyst C1 without γ-ketovaleric acid. The advantage of the catalyst according to the invention remains significant at a lower proportion of organic compound, as shown by the catalyst C8, with an intrinsic efficiency of γ-ketovaleric acid higher than that of the other compounds for which it is necessary to introduce a greater proportion of compound to observe a significant catalytic effect.
[0062] Table 1: Activity relative to iso-volume in gas oil hydrodesulfurization of catalysts C1, C2, C3, C4 and C7 (not in accordance with the invention) and C5, C6, C8 (in accordance with the invention) with respect to to the catalyst C2 (non-compliant) Catalyst Compound Mode of introduction of the organic compound Heat treatment HDS activity (organic comparison used and (post- / co- / pre-impregnation or according to molar ratio / Mo the invention) Cl (comp) none Without object Dried 120 ° C Base + 1.1 ° C C2 (comp) n / a N / A Calcium Base C3 (comp) Citric acid - 1.0 CO Dry 120 ° C Base - 3.1 ° C C4 (comp) TEG - 1.0 CO Dried 120 ° C Base - 5.3 ° C C5 (inv) y-ketovaleric acid -1.0 CO Dried 120 ° C Base - 7.8 ° C C6 (inv) y-ketovaleric acid -1.0 PRE Dried 120 ° C Base - 6.5 ° C C7 (comp) Citric Acid - 0.25 CO Dry 120 ° C Base - 2.2 ° C C8 (inv) y-ketovaleric acid - 0.25 CO Dry 120 ° C Base - 4 , 2 ° C 5

权利要求:
Claims (18)
[0001]
REVENDICATIONS1. Catalyst comprising a support based on alumina or silica or silica-alumina, at least one group VIII element, at least one group VIB element, and γ-ketovaleric acid.
[0002]
2. The catalyst according to claim 1, wherein the element content of group VIB is between 5 and 40% by weight expressed as Group VIB metal oxide relative to the total weight of the catalyst and the element content of group VIII is included between 1 and 10% weight expressed as Group VIII metal oxide relative to the total weight of the catalyst.
[0003]
3. Catalyst according to claim 1 or 2, wherein the molar ratio of Group VIII element to Group VIB element in the catalyst is between 0.1 and 0.8.
[0004]
4. Catalyst according to one of claims 1 to 3, which further contains phosphorus, the phosphorus content being between 0.1 and 20% by weight expressed in P2O5 relative to the total weight of the catalyst and the phosphorus ratio on the Group VIB element in the catalyst is greater than or equal to 0.05.
[0005]
5. Catalyst according to one of claims 1 to 4, wherein the γ-ketovaleric acid content is between 1 and 35% by weight relative to the total weight of the catalyst.
[0006]
6. Catalyst according to one of claims 1 to 5, which further contains an organic compound other than γ-ketovaleric acid containing oxygen and / or nitrogen and / or sulfur.
[0007]
7. Catalyst according to claim 6, wherein the organic compound is chosen from a compound comprising one or more chemical functional groups chosen from a carboxylic function, alcohol, thiol, thioether, sulfone, sulfoxide, ether, aldehyde, ketone, ester, carbonate, amine, nitrile, imide, oxime, urea and amide.
[0008]
The catalyst of claim 7, wherein the organic compound is selected from triethylene glycol, diethylene glycol, ethylenediaminetetraacetic acid, maleic acid, citric acid, dimethylformamide, bicine, or tricine.
[0009]
9. Catalyst according to one of claims 1 to 8, wherein the carrier contains from 0.1 to 50% by weight of zeolite.
[0010]
10. Catalyst according to one of claims 1 to 9, characterized in that it is at least partially sulphurized.
[0011]
11. Process for the preparation of a catalyst according to one of claims 1 to 10 comprising the following steps: a) at least one component of a group VIB element is brought into contact with at least one component of an element of group VIII, γ-ketovaleric acid and optionally phosphorus with a support based on alumina or silica or silica-alumina, or is brought into contact a regenerated catalyst containing a support based on alumina or silica or silica-alumina, at least one component of a group VIB element, at least one component of a group VIII element and optionally phosphorus with γ-ketovaleric acid, so as to obtain a precursor catalyst, b) said catalyst precursor from step a) is dried at a temperature below 200 ° C, without calcining it later.
[0012]
12. The process as claimed in claim 11, in which step a) is the following step: a ') is impregnated with a support based on alumina or silica or silica-alumina by at least one solution containing at least a group VIB element, at least one group VIII element, γ-ketovaleric acid and optionally phosphorus so as to obtain a catalyst precursor. 3035600 49
[0013]
13. The method of claim 11, wherein step a) comprises the following steps: a1) impregnating a support based on alumina or silica or silica-alumina by at least one solution containing at least one element of group VIB, at least one group VIII element and optionally phosphorus to obtain an impregnated support, a2) the impregnated support obtained in step a1) is dried at a temperature below 200 ° C to obtain a dried impregnated support, and optionally drying the dried impregnated support to obtain a calcined impregnated support, a3) impregnating the dried and optionally calcined impregnated support obtained in step a2) with an impregnating solution comprising at least ycetovaleric acid so as to To obtain a catalyst precursor, a4) optionally, the catalyst precursor obtained in step a3) is allowed to mature.
[0014]
14. The process as claimed in claim 11, wherein step a) comprises the following steps: a) preparing a support comprising at least γ-ketovaleric acid and optionally at least part of the phosphorus, impregnates the support obtained in step a1 ') with an impregnating solution comprising at least one group VIB element, at least one group VIII element and optionally phosphorus so as to obtain a catalyst precursor, a3') optionally the catalyst precursor obtained in step a2 ') is allowed to mature.
[0015]
15. The method of claim 11, wherein step a) comprises the following steps: a) a solution containing at least one element of group VIB, at least one element of group VIII, is contacted by co-impregnation, at least one organic compound containing oxygen and / or nitrogen and / or sulfur, and optionally phosphorus with a support based on alumina or silica or silica-alumina so as to obtain an impregnated support, a2 ") the impregnated support from step a1" ") is dried at a temperature below 200 ° C, without subsequently calcining it to obtain a dried impregnated support, a3") the impregnated support is brought into contact with dried from step a2 ") with a solution of an organic compound containing oxygen and / or nitrogen and / or sulfur identical or different from that used in step a1") so as to obtain a catalyst precursor, 10 a4 ") optionally, it is allowed to mature catalyst precursor obtained in step a3 "), and at least one of the organic compounds of step a1" - or step a3 ") is γ-ketovaleric acid.
[0016]
16. The process according to claim 11, wherein step a) comprises the following steps: a) regenerating a regenerated catalyst containing a support based on alumina or silica or silica-alumina, at least one component of a group VIB element, at least one component of a Group VIII element and optionally phosphorus by an impregnating solution comprising at least γ-ketovaleric acid so as to obtain a catalyst precursor, a2 Optionally, the catalyst precursor obtained in step a1 '') is allowed to mature.
[0017]
17. The process as claimed in one of claims 11 to 16, wherein the molar ratio of γ-ketovaleric acid to group VIII element (s) is between 0.1 and 5.0 mol / mol.
[0018]
18. Use of the catalyst according to one of claims 1 to 10 or prepared according to one of claims 10 to 17 in a process for hydrotreating and / or hydrocracking of hydrocarbon cuts.

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2022-01-07| ST| Notification of lapse|Effective date: 20211205 |

优先权:

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申请号 | 申请日 | 专利标题

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FR1553913A|FR3035600B1|2015-04-30|2015-04-30|CATALYST BASED ON Y-CETOVALERIC ACID AND USE THEREOF IN A HYDROTREATING AND / OR HYDROCRACKING PROCESS|FR1553913A| FR3035600B1|2015-04-30|2015-04-30|CATALYST BASED ON Y-CETOVALERIC ACID AND USE THEREOF IN A HYDROTREATING AND / OR HYDROCRACKING PROCESS|

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JP2017556726A| JP6726688B2|2015-04-30|2016-03-11|γ-Ketovaleric acid-based catalysts and their use in hydrotreating and/or hydrocracking processes|

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RU2017134404A| RU2698326C2|2015-04-30|2016-03-11|CATALYST BASED ON γ-KETOVALERIC ACID AND USE THEREOF IN HYDROTREATMENT AND/OR HYDROCRACKING|

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EP16709457.2A| EP3288679B1|2015-04-30|2016-03-11|Gamma-ketovaleric acid-based catalyst and use thereof in a hydroprocessing and/or hydrocracking method|

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US15/569,783| US10464054B2|2015-04-30|2016-03-11|Catalyst based on γ-ketovaleric acid and use thereof in a hydrotreatment and/or hydrocracking process|

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PCT/EP2016/055329| WO2016173760A1|2015-04-30|2016-03-11|Γ-ketovaleric acid-based catalyst and use thereof in a hydroprocessing and/or hydrocracking method|

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DK16709457.2T| DK3288679T3|2015-04-30|2016-03-11|CATALYST BASED ON? ketoVALERIAN ACID AND ITS USE IN A HYDROGEN TREATMENT AND / OR HYDROGEN PROCESSING METHOD|

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TW105110123A| TWI700123B|2015-04-30|2016-03-30|CATALYST BASED ON γ-KETOVALERIC ACID AND USE THEREOF IN A HYDROTREATMENT AND/OR HYDROCRACKING PROCESS|

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ZA2017/06247A| ZA201706247B|2015-04-30|2017-09-14|G¿ketovaleric acid¿based catalyst and use thereof in a hydroprocessing and/or hydrocracking method|