EP2097169A2 - Catalyst based on a silicon-containing material with hierarchical porosity and method for the hydrocracking/hydroconversion and hydroprocessing of hydrocarbon feedstocks - Google Patents

Abstract

The invention relates to a catalyst including at least one silicon-containing material with hierarchical porosity and at least one hydro-dehydrogenating element from the VIB group and/or the VIII group of the periodic table. The silicon-containing material with hierarchical porosity is formed by at least two spherical elementary particles each comprising zeolitic nanocrystals having a pore size of between 0.2 and 2 nm and a mesostructured silicon-oxide-based matrix having a pore size of between 1.5 and 30 nm and having amorphous walls with a thickness of between 1 and 30 nm, said spherical elementary particles having a maximum diameter of 100 μm. The silicon-oxide-based matrix can contain aluminium. The catalyst can also optionally contain a controlled amount of at least one dopant selected from among phosphorous, boron and silicon, at least one element from the VB group of the periodic table of elements and an element from the VIIA group. The invention also relates to hydrocracking/hydroconversion and hydroprocessing methods using said catalyst.

Description

 CATALYST BASED ON HIERARCHISED POROSITY MATERIAL COMPRISING SILICON AND METHOD FOR HYDROCRACKING / HYDROCONVERSION AND HYDROCARBING LOADS

HYDROCARBON

The present invention relates to the field of bifunctional catalysts characterized by hydro-dehydrogenating and acidity properties. It relates more particularly to a catalyst comprising at least one metallosilicate material and more specifically aluminosilicate having a hierarchized porosity in the field of microporosity and mesoporosity and at least one hydro-dehydrogenating element. It also relates to the preparation of such a catalyst.

The invention also relates to hydrocracking, hydroconversion and hydrotreatment processes using this catalyst.

In particular, the invention relates to the hydrocracking of hydrocarbonaceous feeds containing, for example, aromatic and / or olefinic and / or naphthenic and / or paraffinic compounds, with the exception of feedstocks resulting from the Fischer-Tropsch process and possibly containing metals, and / or nitrogen, and / or oxygen and / or sulfur.

The objective of the hydrocracking process is essentially the production of middle distillates, ie cuts with initial boiling point of at least 150 ^° C. and final up to the boiling point. initial residue, for example less than 340 ⁰ C, or 370 ⁰ C.

The invention also relates to the hydrotreatment of hydrocarbon feedstocks such as petroleum cuts, cuts from coal or hydrocarbons produced from natural gas. These hydrocarbon feedstocks comprise nitrogen and / or sulfur and / or aromatic and / or olefinic and / or naphthenic and / or paraffinic compounds, said feeds possibly containing metals and / or oxygen and / or sulfur. . Hydroprocessing is understood to mean hydrogenation, hydrodesulfurization, hydrodenitrogenation, hydrodeoxygenation, hydrodearomatization and hydrodemetallation reactions.

State of the art

Hydrocracking of heavy oil cuts is a very important process of refining which makes it possible to produce lighter fractions, such as gasolines, light fuel oils and fuels, which the refiner seeks in order to adapt his production to heavy surpluses which can not be upgraded. the structure of the request. Certain hydrocracking processes also make it possible to obtain a highly purified residue that can provide excellent bases for oils. Compared to catalytic cracking, the advantage of catalytic hydrocracking is to provide middle distillates, jet fuels and gas oils, of very good quality. Conversely, the gasoline produced has a much lower octane number than that resulting from catalytic cracking.

Hydrocracking is a process which derives its flexibility from three main elements which are the operating conditions used, the types of catalysts employed and the fact that the hydrocracking of hydrocarbon feeds can be carried out in one or two stages.

The hydrocracking catalysts used in the hydrocracking processes are all of the bifunctional type associating an acid function with a hydro-dehydrogenating function. The acid function is provided by supports whose surfaces generally vary from 150 to 800 m2.g-1 and having surface acidity, such as halogenated alumina (chlorinated or fluorinated in particular), combinations of boron oxides and aluminum, amorphous mesoporous aluminosilicates and zeolites. The hydro-dehydrogenating function is provided either by one or more metals of group VIB of the periodic table of elements, or by a combination of at least one metal of group VIB of the periodic table with at least one metal of group VIII.

The balance between the two acid and hydro-dehydrogenating functions is one of the parameters that govern the activity and the selectivity of the catalyst. A weak acid function and a strong hydro-dehydrogenating function give low active catalysts, working at a generally high temperature (greater than or equal to 390-400 ^° C.) and with a low feed-in space velocity (the WH expressed in volume charge to be treated per unit volume of catalyst per hour is generally less than or equal to 2), but with a very good selectivity in middle distillates. Conversely, a strong acid function and a low hydro-dehydrogenating function give active catalysts, but having lower selectivities in middle distillates (jet fuels and gas oils).

One type of conventional hydrocracking catalyst is based on moderately acidic amorphous supports, such as mesoporous aluminosilicates, for example. These systems are used to produce middle distillates of good quality and, possibly, oil bases. These catalysts are for example used in one-step processes. The disadvantage of these catalysts based on an amorphous mesoporous support is their low activity. Catalysts comprising, for example, zeolite Y of FAU structural type, or catalysts comprising, for example, a beta zeolite (BEA structural type), have a higher catalytic activity than amorphous mesoporous aluminosilicates, but have selectivities. in middle distillates (jet fuels and gas oils) which are lower.

One of the scientific challenges of recent years is to develop new aluminosilicate supports crystallized or not that would present an acceptable compromise between catalytic activity and selectivity in middle distillates and which would be midway between a zeolite-like behavior and a type of behavior. amorphous mesoporous aluminosilicate.

On the other hand, the proportion of so-called "heavy" compounds in the raw feeds to be treated becoming increasingly important, the development of catalysts with textural properties adapted to these new loads also represents a major challenge.

In this quest for new aluminosilicate materials, the so-called "mesostructured" materials, discovered in the early 90's, represent an attractive alternative (GJ AA Soler-lllia, C. Sanchez, B. Lebeau, J. Patarin, Chem Rev. , 2002, 102, 4093). Indeed, thanks to so-called "soft chemistry" synthesis methods, amorphous mesoporous materials whose size and pore morphology are controlled have been obtained. These mesostructured materials are thus generated at low temperature by the coexistence in aqueous solution or in polar solvents of inorganic precursors with structuring agents, generally molecular or supramolecular, ionic or neutral surfactants. The control of electrostatic or hydrogen bonding interactions between the inorganic precursors and the structuring agent together with hydrolysis / condensation reactions of the inorganic precursor leads to a cooperative assembly of the organic and inorganic phases generating micellar aggregates of uniformly sized surfactants. and controlled within an inorganic matrix. This phenomenon of cooperative self-assembly, governed inter alia by the concentration of structuring agent, can be induced by progressive evaporation of a solution of reagents whose concentration of structuring agent is lower than the critical micelle concentration, which can lead by example to the formation of a mesostructured powder after atomization of the solution (aerosol technique). The release of the porosity is then obtained by removal of the surfactant, which is conventionally carried out by chemical extraction processes or by heat treatment. Depending on the nature of the inorganic precursors and the structuring agent used as well as the operating conditions imposed, several families of mesostructured materials have been developed. For example, the M41S family originally developed by Mobil (JS Beck, JC Vartuli, WJ Roth, ME Leonowicz, CT Kresge, KD Schmitt, CT-W Chu, DH Oison, EW Sheppard, SB McCullen, JB Higgins, JL Schlenker, J. Am Chem Soc, 1992, 114, 27, 10834), consisting of mesoporous materials obtained via the use of ionic surfactants such as quaternary ammonium salts, having a generally hexagonal, cubic or lamellar structure, pores of uniform size in a range of 1.5 to 10 nm and amorphous walls of the order of 1 to 2 nm thick has been extensively studied. Similarly, the use of amphiphilic macromolecular structuring agents of the block copolymer type has led to the development of the family of materials called SBA, these solids being characterized by a generally hexagonal, cubic or lamellar structure, large pores uniform in a range of 4 to 50 nm and amorphous walls of thickness in a range of 3 to 7 nm.

However, it has been shown that, although having particularly interesting textural and structural properties (in particular for the treatment of heavy loads), the mesostructured aluminosilicate materials thus obtained developed a catalytic activity which was in all respects similar to that of their porous counterparts. unorganized (D. Zaho, J. Feng, Q. Huo, N. Melosh, GH Fredrickson, BF Chmelke, GD Stucky, Science, 1998, 279, 548, Y.-H. Yue, A. Gideon, J.- L Bonardet, Espinose JB, Melosh N., Fraissard J., Surf Stud Sci.Catal., 2000, 129, 209). Much work has therefore been undertaken to develop aluminosilicate materials with both the advantages of an organized mesoporous structure and those of a microcrystalline network.

A large number of synthetic techniques for the preparation of mixed materials or mesostructured composites / zeolites have thus been listed in the open literature (US 6,669,924, Z. Zhang, Han Y., F. Xiao, S. Qiu, L Zhu, R. Wang, Y. Yu, Zhang Z., Zou Y., Wang Y., Sun H, Zhao D, Wei Y., J. Am Chem Soc, 2001, 123, 5014; Karlsson, M. Stocker, R. Schmidt, Micropor, Mesopor, Mater., 1999, 27, 181, P. Prokesova, S. Mintova, J. Cejka, T. Bein, Micropor, Mesopor, Mater., 2003, 64 165, DT On, S. Kaliagin, Angew Chem Int.Ed., 2002, 41, 1036). From an experimental point of view, in contrast to the "aerosol" technique mentioned above, the aluminosilicate materials with hierarchical porosity thus defined are not obtained by a progressive concentration of the inorganic precursors and the structuring agent (s). (s) within the solution where they are present but are conventionally obtained by direct precipitation in an aqueous solution or in polar solvents by varying the value of the critical micelle concentration of the structuring agent. In addition, the synthesis of these materials obtained by precipitation requires a curing step in an autoclave and a filtration step of the generated suspension. The elementary particles usually obtained do not have a regular shape and are generally characterized by a size generally ranging between 200 and 500 nm and sometimes more.

Summary of the invention

The invention relates to a catalyst comprising at least one material having a hierarchical porosity comprising silicon and at least one group VIB and / or group VIII hydro-dehydrogenating element of the periodic table. Said hierarchical porosity material comprising silicon consists of at least two elementary spherical particles, each of said spherical particles comprising zeolitic nanocrystals having a pore size of between 0.2 and 2 nm and a matrix based on silicon oxide , mesostructured, having a pore size of between 1.5 and 30 nm and having amorphous walls of thickness between 1 and 30 nm, said elementary spherical particles having a maximum diameter of 100 microns. Said matrix based on silicon oxide optionally further comprises at least one element X selected from the group consisting of aluminum, titanium, tungsten, zirconium, gallium, germanium, phosphorus, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum and yttrium, preferably in the group consisting of aluminum, titanium, zirconium, niobium, germanium and gallium and more preferably aluminum. Said zeolite nanocrystals present in each of the elementary spherical particles constituting the material according to the invention may be generated by any zeolite or related solid developing acidity properties and in particular by aluminosilicate and / or silicoaluminophosphate solids. Said material having a hierarchical porosity comprising silicon is the subject of the patent application FR 2 872 152 A. The catalyst according to the invention also optionally contains at least one doping element in a controlled quantity chosen from phosphorus, boron and silicon. optionally at least one member of group VB of the periodic table of elements, preferably niobium, and optionally at least one group VIIA element, preferably fluorine. The present invention also relates to the preparation of catalyst according to the invention. In addition, the present invention relates to hydrocracking, hydroconversion and hydrotreatment processes using said catalyst.

Interest of the invention

The material having a hierarchical porosity comprising silicon and consisting of at least two elementary spherical particles, which comprises a mesostructured inorganic matrix, based on silicon oxide, with amorphous walls in which zeolitic nanocrystals are trapped, and present in the catalyst according to the invention, simultaneously exhibits the structural, textural and acid-base properties of materials of the family of zeolites and / or solid relatives and materials based on silicon oxide, specifically mesostructured aluminosilicate materials. The development at the nanometer scale of a mesostructured / zeolite silicon-based composite material leads to a privileged connection of the microporous and mesoporous zones within the same spherical particle. In addition, the material present in the catalyst according to the invention consists of spherical elementary particles, the maximum diameter of these particles being 100 μm, advantageously ranging from 50 nm to 100 μm, preferably from 50 nm to 10 μm, preferred way from 50 nm to 1 micron, more preferably from 50 to 600 nm and very preferably between 50 and 300 nm, the limited size of these particles and their homogeneous shape makes it possible to have a better diffusion of the reagents and products of the reaction when the material is used as the basic element of the catalyst according to the invention in hydrocracking, hydroconversion and hydrotreatment processes compared with catalysts known from the state of the art. On the other hand, the zeolite nanocrystals dispersed within said hierarchical porosity material have a maximum size equal to 500 nm. The use of small zeolite crystals thus makes it possible to obtain hydrocracking activity gains and selectivity gains in middle distillates.

The set of properties specific to the material having a hierarchical porosity comprising silicon thus induces specific catalytic properties of the catalyst according to the invention comprising said material when it is used in hydrocracking, hydroconversion and hydrotreatment processes. Indeed, the research work carried out by the applicant on these innovative solids and on the hydro-dehydrogenating active phases led him to discover that a hydrocracking, hydroconversion and hydrotreatment process for hydrocarbon feedstocks comprising at least said hierarchical porosity material comprising silicon, at least one hydro-dehydrogenating metal selected from the metals of groups VIB and VIII _1, optionally at least one doping element chosen from the group formed by boron, silicon and phosphorus, optionally at least one element of group VB of the periodic table of elements (preferably niobium), and optionally a group VIIA element (preferably fluorine), makes it possible to obtain activities (c ' that is to say high conversion levels compared to those generated by conventional catalysts based on amorphous aluminosilicates with unorganized porosity and selectivities in middle distillates (jet fuel and gas oil) higher than with the zeolitic catalysts known in the art. prior art.

Characterization techniques

The catalyst according to the invention as well as the support formed of said material having a hierarchical porosity present in the catalyst according to the invention are characterized by several analysis techniques and in particular by X-ray diffraction at low angles (low angle XRD), by X-ray diffraction at high angles (XRD), nitrogen adsorption isotherm, Transmission Electron Microscopy (TEM) optionally coupled to energy-selective X-ray spectrometry (EDX) analysis by microprobe Castaing, electron microprobe and X Fluorescence (FX) or

Atomic Absorption (AA).

The technique of X-ray diffraction at large angles (values of the angle 2Θ between 5 and 70 °) makes it possible to characterize a crystallized solid defined by the repetition of a unitary unit or elementary cell at the molecular scale. In the following discussion, the X-ray analysis is performed on powder with a diffractometer operating in reflection and equipped with a rear monochromator using copper radiation (wavelength 1.5406 A). The peaks usually observed on the diffractograms corresponding to a given value of the angle 2Θ are associated with inter-reticular distances d ^ w ₎ characteristic of the structural symmetry (s) of the material, ((hkl) being the Miller indices of the reciprocal lattice) by the Bragg relation: 2 d _(h ι _< i ₎ * sin (θ) = n * λ. This indexing then allows the determination of the mesh parameters (abc) of the direct network. The wide-angle XRD analysis is therefore adapted to the structural characterization of the zeolite nanocrystals present in each of the elementary spherical particles of the hierarchical porosity material comprising silicon and present in the catalyst according to the invention. In particular, it provides access to the pore size of zeolitic nanocrystals. Following the same principle, the X-ray diffraction technique at low angles (values of the angle 2Θ between 0.5 and 3 °) makes it possible to characterize the periodicity at the nanoscale generated by the organized mesoporosity of the catalyst according to the invention. 'invention. The value of the mesh parameters (abc) depends on the hexagonal, cubic or vermicular structure obtained. The value of the angle obtained on the diffractogram RX makes it possible to go back to the correlation distance d according to the Bragg law: 2 d * sin (θ) = n * λ.

The nitrogen adsorption isothermal analysis corresponding to the physical adsorption of nitrogen molecules in the porosity of the material via a progressive increase of the pressure at constant temperature provides information on the textural characteristics (pore diameter, porosity type, specific surface area) of the catalyst according to the invention. In particular, it provides access to the specific surface and the mesoporous distribution of the catalyst according to the invention. By specific surface is meant the specific surface B. AND. (S _B AND in m ² / g) determined by nitrogen adsorption according to the ASTM D 3663-78 standard established from the method BRU NAU ER-EM M ETT-TELLER described in the journal "The Journal of American Society The representative porous distribution of a mesopore population centered in a range of 1.5 to 50 nm is determined by the Barrett-Joyner-Halenda model (BJH). Nitrogen desorption according to the BJH model is described in the periodical "The Journal of American Society", 1951, 73, 373, written by EP Barrett, LG Joyner and PP Halenda In the following discussion, the diameter of the mesospores φ the catalyst according to the invention corresponds to the average diameter at the nitrogen desorption defined as being a diameter such that all pores less than this diameter constitute 50% of the pore volume (Vp) measured on the desorption branch of the nitrogen isotherm In addition, the appearance of the nitrogen adsorption isotherm and the hysteresis loop can provide information on the presence of microporosity related to zeolite nanocrystals and the nature of mesoporosity.

The transmission electron microscopy (TEM) analysis is a technique also widely used to characterize the mesostructuration of the catalyst according to the invention. This allows the formation of an image of the studied solid, the observed contrasts being characteristic of the structural organization, the texture, the morphology or the zeolite / mesostructured composition of the particles observed, the resolution of the technique reaching at most 0.2 nm. The analysis of the image also makes it possible to access the parameters d _(hk i ₎ and φ characteristics of the catalyst according to the invention defined above. It is also possible to visualize, on this same plate, more or less opaque spherical objects representing the zeolitic nanocrystals trapped in the mesostructured matrix forming the spherical particles of the hierarchically porous material present in the catalyst according to the invention.

The distribution and location of the elements constituting the hydrogenating phase can be determined by techniques such as the Castaing microprobe (distribution profile of the various elements), Transmission Electron Microscopy coupled with an X analysis of the catalyst components (EDX), or else by establishing a distribution map of the elements present in the catalyst by electron microprobe. These techniques make it possible to demonstrate the presence of these exogenous elements added after synthesis of the hierarchically porous material comprising silicon and present in the catalyst according to the invention. The distribution and location of group VIB elements such as group VIII mobydene or tungsten, such as iron, cobalt, nickel, platinum, or palladium, group VB such as niobium, group VIIA such as fluorine, can be determined according to these techniques. Similarly, the distribution and location of boron, silicon and phosphorus can be determined using these techniques.

The overall composition of the catalyst according to the invention can be determined by Fluorescence X (FX) on said catalyst in the pulverulent state or by Atomic Absorption (AA) after acid attack of said catalyst.

Detailed exposition of the invention

More specifically, the invention relates to a catalyst comprising:

at least one support formed of at least one material with hierarchical porosity comprising silicon and consisting of at least two elementary spherical particles, each of said spherical particles comprising zeolitic nanocrystals having a pore size of between 0.2 and 2 nm and a mesostructured silicon oxide-based matrix having a pore size of 1.5 to 30 nm and having amorphous walls of thickness between 1 and 30 nm, said elementary spherical particles having a maximum diameter of 100 μm,

at least one active phase containing at least one hydro-dehydrogenating element of group VIB and / or group VIII of the periodic table. According to the invention, the group VIB element is advantageously present at a metal mass content of between 0.1 and 40%, preferably between 1.5 and 35%, and even more preferably between 3 and 25%, the percentages being expressed in% by weight with respect to the total mass of the catalyst and the element of the group

VIII is advantageously present at a mass content of metal of between 0.1 and 25%, preferably between 0.1 and 20% and even more preferably between 0.1 and 15%, said hierarchically porous material is advantageously present at a mass content of between 20 and 99.9%, preferably between 30 and 99.9% and even more preferably between 40 and 99.9%.

The catalyst according to the invention comprises:

optionally, at least one doping element chosen from the group consisting of silicon (in addition to the silicon contained in said material with hierarchical porosity present in the catalyst according to the invention), boron and phosphorus, present at a mass content between 0 and 20%, preferably between 0.1 and 15%, preferably between 0.1 and 10% and even more preferably between 0.2 and 4%,

- optionally at least one group VB element, preferably niobium, present at a mass content of between 0 and 60%, preferably between 0.1 and 50%, and even more preferably between 0.1 and 40%, - optionally at least one group VIIA element, preferably fluorine, present at a mass content of between 0 and 20%, preferably between 0.1 and 15% and even more preferably between 0.1 and 10%,

optionally a binder such as silica, alumina, clays, titanium oxide, boron oxide and zirconia and any mixture of the binders mentioned above. The preferred binders are silica and alumina and even more preferably alumina. The weight content of binder on the catalyst is between 0 and 30%, preferably between 0 and 20%. The catalyst according to the invention is preferably free of binder.

According to a first embodiment of the catalyst according to the invention, the hydro-dehydrogenating element of said active phase included in said catalyst is a member selected from the group consisting of group VIB elements and is preferably selected from molybdenum and tungsten. According to a preferred embodiment of said first embodiment of the catalyst according to the invention, the hydro-dehydrogenating element of said active phase included in said catalyst is a member selected from the group formed by the elements of group VIB of the periodic table is the molybdenum.

According to another preferred embodiment of said first embodiment of the catalyst according to the invention, the hydro-dehydrogenating element chosen from the group formed by the elements of group VIB of the periodic table is tungsten.

According to a second embodiment of said catalyst according to the invention, the hydro-dehydrogenating element of said active phase included in said catalyst is a member selected from the group consisting of Group VIII elements and is preferably selected from iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium or platinum, taken alone or as a mixture, very preferably selected from iron, cobalt, nickel, platinum, palladium and ruthenium, taken alone or as a mixture, and even more preferably chosen from cobalt, nickel and platinum, taken alone or as a mixture.

According to a preferred embodiment of said second embodiment of the catalyst according to the invention, the hydro-dehydrogenating element chosen from the group formed by the elements of group VIII of the periodic table is cobalt.

According to another preferred embodiment of said second embodiment of the catalyst according to the invention, the hydro-dehydrogenating element chosen from the group formed by the elements of group VIII of the periodic table is nickel.

According to yet another even more preferred embodiment of said second embodiment of the catalyst according to the invention, the hydro-dehydrogenating element chosen from the group formed by the elements of group VIII of the periodic table is platinum.

According to a third embodiment of the catalyst according to the invention, said active phase included in said catalyst is formed of at least one element of group VIB and at least one element of group VIIl. According to said third embodiment of the catalyst according to the invention, and advantageously the following combinations of metals are used as active phase: nickel-molybdenum, cobalt-molybdenum, iron-molybdenum, iron-tungsten, nickel-tungsten, cobalt-tungsten, platinum-palladium, preferably the combinations nickel-molybdenum, cobalt-molybdenum, cobalt-tungsten, nickel-tungsten and even more preferably the nickel-moybdenum and nickel-tungsten combinations.

It is also possible to use as the active phase combinations of three metals, for example nickel-cobalt-molybdenum, nickel-molybdenum-tungsten, nickel-cobalt-tungsten, etc. Advantageously, the following metal combinations are used. nickel-niobium-molybdenum, cobalt-niobium-molybdenum, iron-niobium-molybdenum, nickel-niobium-tungsten, cobalt-niobium-tungsten, iron-niobium-tungsten and preferably the nickel-niobium-molybdenum, cobalt-niobium combinations -molybdenum.

It is also possible to use as the active phase combinations of four metals, for example nickel-cobalt-niobium-molybdenum. It is also possible to use combinations containing a noble metal such as ruthenium-niobium-molybdenum or ruthenium-nickel-niobium-molybdenum.

Said material having a hierarchical porosity comprising silicon, present in the catalyst according to the invention, consists of at least two elementary spherical particles, each of said spherical particles comprising zeolitic nanocrystals having a pore size of between 0.2 and 2 nm. and a mesostructured silicon oxide matrix having a pore size in the range of 1.5 to 30 nm and having amorphous walls having a thickness in the range of 1 to 30 nm, said elementary spherical particles having a maximum diameter of 100 μm.

For the purposes of the present invention, the term "hierarchically porous material" means a material having a double porosity on the scale of each of said spherical particles: a mesoporosity, that is to say an organized porosity at the mesopore scale having a uniform size of between 1.5 and 30 nm and preferably between 1.5 and 10 nm, homogeneously and uniformly distributed in each of said particles (mesostructuration) and a zeolite type microporosity whose characteristics (type structural zeolite and / or related solid, chemical composition of the zeolite framework) are a function of the choice of zeolitic nanocrystals.

According to the invention, said zeolitic nanocrystals have a pore size of between 0.2 and 2 nm, preferably between 0.2 and 1 nm and very preferably between 0.2 and 0.8 nm. Said nanocrystals generate the microporosity in each of the elementary spherical particles constituting the hierarchical porosity material comprising silicon and present in the catalyst according to the invention.

The matrix based on silicon oxide, included in each of the spherical particles constituting said hierarchically porous material present in the catalyst according to the invention, is mesostructured: it has mesopores having a uniform size of between 1.5 and 30 nm and preferably between 1, 5 and 10 nm, distributed homogeneously and evenly in each of said particles. The material located between the mesopores of each of said spherical particles is amorphous and forms walls, or walls, whose thickness is between 1 and 30 nm. The thickness of the walls corresponds to the distance separating one pore from another pore. The organization of the mesoporosity described above leads to a structuring of the matrix based on silicon oxide, which may be hexagonal, vermicular or cubic and preferably vermicular.

According to a particular embodiment of the catalyst according to the invention, the matrix based on silicon oxide, mesostructured, is entirely silicic.

According to another particular embodiment of the catalyst according to the invention, the mesostructured silicon oxide matrix further comprises at least one element X selected from the group consisting of aluminum, titanium, tungsten and zirconium. gallium, germanium, phosphorus, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum and yttrium, preferably from the group consisting of aluminum, titanium, zirconium, niobium, germanium and gallium and more preferably aluminum. Preferably, the element X is aluminum: the matrix of the material according to the invention is in this case an aluminosilicate. Said aluminosilicate has an Si / Al molar ratio of at least 1, preferably of between 1 and 1000 and very preferably of between 1 and 100. According to the invention, the zeolitic nanocrystals advantageously represent from 0.1 to 40% by weight, preferably from 0.1 to 20% by weight and very preferably from 0.1 to 10% by weight of the material with hierarchical porosity comprising silicon and present in the catalyst according to the invention. Any zeolite or related solid developing acidity properties and in particular but not limited to those listed in "Atlas of zeolite framework types", 5 ^fh revised Edition, 2001, Baerlocher C., WM Meier, DH Oison can be used in the zeolitic nanocrystals present in each of the elementary spherical particles constituting the hierarchical porosity material comprising silicon and present in the catalyst according to the invention.

The term zeolite or related solid well known to those skilled in the art means all crystallized microporous oxide solids whose atomic elements constituting the inorganic framework have an IV coordination. By definition, the name "zeolite" is attributed to said microporous silicic or aluminosilicic oxide solids. Similarly, the term "related solid" refers to all crystallized microporous oxide solids whose atomic elements constituting the inorganic framework have an IV coordination, said microporous silicic or aluminosilicic oxide solids being excluded. Any zeolite or related solid having at least one trivalent atomic element at the origin of the presence of a negative charge of said framework and which can be compensated by a positive charge of protonic nature can develop acidity properties. In particular, aluminosilicate zeolites and related solids of silicoaluminophosphate type develop such properties.

The zeolitic nanocrystals preferably comprise at least one zeolite chosen from aluminosilicates ZSM-5, ZSM-48, ZSM-22, ZSM-23, ZBM-30, EU-1, EU-2, ElM 1, beta, zeolite A, Y, USY, VUSY, SDUSY, mordenite, NU-87, NU-88, NU-86, NU-85, IM-5, IM-12 and Ferrierite and / or at least one related solid selected from SAPO silicoaluminophosphates -11 and SAPO-34. Very preferably, the zeolitic nanocrystals comprise at least one zeolite chosen from aluminosilicates of structural type MFI, BEA, FAU, LTA and / or at least one related solid chosen from silicoaluminophosphates of structural type AEL, CHA. Nanocrystals of different zeolites and / or different related solids and in particular zeolites and / or structurally related solids of different structural type may be present in each of the spherical particles constituting the material with hierarchical porosity comprising silicon and present in the catalyst according to the invention. In particular, each of the spherical particles constituting the material having a hierarchical porosity comprising silicon and present in the catalyst according to the invention may advantageously comprise at least first zeolitic nanocrystals derived from a zeolite chosen from aluminosilicates ZSM-5, ZSM -48, ZSM-22, ZSM-23, ZBM-30, EU-1, EU-2, ElM 1, Beta, zeolite A, Y, USY, VUSY, SDUSY, mordenite, NU-87, NU-88, NU -86, NU-85, IM-5, IM-12 and Ferrierite and / or first zeolitic nanocrystals derived from a related solid selected from SAPO-11 and SAPO-34 silicoaluminophosphates, preferably from MFI structural type zeolites , BEA, FAU, LTA and / or structurally related solids AEL, CHA and at least second zeolitic nanocrystals derived from a zeolite and / or a related solid different from the one having generated (e) ) the first zeolitic nanocrystals and chosen from aluminosilicates ZSM-5, ZSM-4 8, ZSM-22, ZSM-23, ZBM-30, EU-2, EU-11, Beta, zeolite A, Y, USY, VUSY, SDUSY, mordenite, NU-87, NU-88, NU-86, NU -85, IM-5, IM-12, Ferrierite and EU-1, preferably among the structural type zeolites MFI, BEA, FAU, and LTA and / or related solids selected from SAPO-11 and SAPO-34 silicoaluminophosphates preferably among the structurally related solids AEL, CHA.

According to the invention, said elementary spherical particles constituting the material having a hierarchical porosity comprising silicon and present in the catalyst according to the invention have a maximum diameter of 100 μm, said diameter advantageously being between 50 nm and 100 μm, preferably between 50 nm and 10 μm and more preferably between 50 and 600 nm and even more preferably between 50 and 300 nm. More specifically, they are present in the material having a hierarchical porosity comprising silicon and present in the catalyst according to the invention in the form of aggregates.

The material having a hierarchical porosity comprising silicon and present in the catalyst according to the invention advantageously has a specific surface area of between 100 and 1100 m ² / g and very advantageously between 200 and 800 m ² / g.

The catalyst according to the invention advantageously has a specific surface area of between 70 and 1000 m ² / g and very advantageously between 80 and 800 m ² / g.

The catalyst according to the invention advantageously has a mean mesoporous diameter of between 1.5 and 30 nm and very advantageously of between 3 and 15 nm. The present invention also relates to the preparation of the catalyst according to the invention.

The material with a hierarchical porosity comprising silicon and present in the catalyst according to the invention is obtained according to two possible methods of preparation. A first embodiment of the process for preparing said hierarchically porous material, hereinafter referred to as "the first method for preparing said material with hierarchical porosity", comprises: a) the synthesis, in the presence of a structuring agent, of zeolitic nanocrystals of maximum nanometer size equal to 500 nm in order to obtain a colloidal solution in which said nanocrystals are dispersed; b) the solution mixture of at least one surfactant, at least one silicic precursor, optionally at least one precursor of at least one element X selected from the group consisting of aluminum, titanium, tungsten , zirconium, gallium, germanium, phosphorus, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum and yttrium, and at least one colloidal solution obtained according to a); c) the aerosol atomization of the solution obtained in step b) to lead to the formation of spherical droplets with a diameter of less than 200 μm; d) drying said droplets and e) removing said structuring agent and said surfactant to obtain a hierarchically porous material.

According to step a) of said first process for preparing the material with a hierarchical porosity comprising constituent silicon of the catalyst according to the invention, the zeolitic nanocrystals are synthesized according to operating protocols known to those skilled in the art. In particular, the synthesis of zeolite Beta nanocrystals has been described by T. Bein et al., Micropor. Mesopor. Mater., 2003, 64, 165. The synthesis of zeolite Y nanocrystals has been described by TJ Pinnavaia et al., J. Am. Chem. Soc., 2000, 122, 8791. The synthesis of ZSM-5 zeolite nanocrystals has been described by R. Mokaya et al., J. Mater. Chem., 2004, 14, 863, etc. Zeolitic nanocrystals are generally synthesized by preparing a reaction mixture containing at least one silicic source, at least one aluminum source, optionally at least one phosphorus source and at least one structuring agent. The reaction mixture is either aqueous or aquo-organic, for example a water-alcohol mixture. The reaction mixture is advantageously placed under hydrothermal conditions under autogenous pressure, optionally by adding gas, for example nitrogen, at a temperature of between 50 and 200 ^° C., preferably between 60 and 170 ^° C. and still preferential at a temperature which does not exceed .12O ⁰ C until the formation of zeolitic nanocrystals. At the end of said treatment hydrothermal, a colloidal solution is obtained in which the nanocrystals are in the dispersed state. The structuring agent may be ionic or neutral depending on the zeolite and / or the related solid to be synthesized. It is common to use the structuring agents of the following non-exhaustive list: nitrogenous organic cations, elements of the family of alkalis (Cs, K, Na, etc.), ethercouronnes, diamines and any other structuring agent well known to the Man of Art. According to step b) of said first preparation process according to the invention, the element X is preferably selected from the group consisting of aluminum, titanium, zirconium, niobium, germanium and gallium and so most preferred X is aluminum.

In a second embodiment of the process for preparing said hierarchically porous material, hereinafter referred to as "the second method for preparing said hierarchically porous material", crystals of zeolites and / or related solids, which have the characteristic, are initially used. to disperse in the form of nanocrystals of maximum nanometric size equal to 500 nm in solution, for example in aqueous-organic acid solution. Said second method for preparing the material with hierarchical porosity comprises: a ') mixing in solution at least one surfactant, at least one silicic precursor, optionally at least one precursor of at least one element X chosen from the group consisting of aluminum, titanium, tungsten, zirconium, gallium, germanium, phosphorus, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum and yttrium, and crystals of zeolites and / or related solids dispersing in the form of nanocrystals of maximum nanometric size equal to 500 nm in said solution; b ') aerosol atomizing said solution obtained in step a ¹ ) to lead to the formation of spherical droplets of diameter less than 200 microns; c ¹ ) the drying of said droplets and the) elimination of at least said surfactant.

In step a ') of said second method for preparing the hierarchically porous material, crystals of zeolites and / or related solids are used. Any zeolite or related solid developing acidity properties known in the state of the art which has the property of dispersing in solution, for example in aquo-organic acid solution, in the form of nanocrystals of maximum nanometric size equal to 500 nm is suitable for the implementation of step a '). Said crystals of zeolites and / or related solids are synthesized by methods known to those skilled in the art. The crystals of zeolites and / or related solids used in step a ') may already be in the form of nanocrystals. It is also advantageous to use crystals of zeolites and / or related solids greater than 500 nm in size, for example between 500 nm and 200 μm, which are dispersed in solution, for example in aqueous-organic solution, preferably in aqueous-organic solution. acid, in the form of nanocrystals of maximum nanometric size equal to 500 nm. Obtaining crystals of zeolites and / or related solids dispersing in the form of nanocrystals of maximum nanometric size equal to 500 nm is also possible by performing functionalization of the surface of the nanocrystals. The element X is preferably selected from the group consisting of aluminum, titanium, zirconium, niobium, germanium and gallium and more preferably X is aluminum. The crystals of zeolites and / or related solids used are either in their raw form of synthesis, that is to say still containing the structuring agent, or in their calcined form, that is to say freed of said structuring agent. When the crystals of zeolites and / or related solids used are in their raw form of synthesis, said structuring agent is removed during step d) of said second process for preparing the material with hierarchical porosity.

In accordance with the two processes for preparing said hierarchically porous material, the silicic precursor and optionally the precursor of at least one element X, preferably the aluminum precursor, used in step b) of the first process for preparing said hierarchically porous material respectively in step a ¹ ) of the second process for preparing said hierarchically porous material are precursors of inorganic oxides well known to those skilled in the art. The silicic precursor is obtained from any source of silica and advantageously a sodium silicate precursor of formula SiO ₂ , NaOH ₁ of a chlorinated precursor of formula SiCl ₄ , an organometallic precursor of formula Si (OR) ₄ where R = H, methyl, ethyl or a chloroalkoxide precursor of formula Si (OR) ₄ . _x Cl _x wherein R = H, methyl, ethyl, x being between 0 and 4. The silicic precursor can also advantageously be an organometallic precursor of the formula Si (OR) _{4. X} R _X where R = H, methyl, ethyl and R 'is an alkyl chain or a functionalized alkyl chain, for example by a thiol, amino, β diketone or sulfonic acid, x being between 0 and 4. The precursor of the element X can be any compound comprising the element X and able to release this element in solution, for example in aqueous-organic solution, preferably in aqueous-organic acid solution, in reactive form. In the preferred case where X is aluminum, the aluminum precursor is advantageously an inorganic aluminum salt of formula AlZ ₃ , Z being a halogen or the NO ₃ group. Preferably, Z is chlorine. The aluminum precursor can also be a precursor organometallic compound of formula AI (OFT) ₃ or R "= ethyl, isopropyl, n-butyl, s-butyl or t-butyl or a chelated precursor such as aluminum acetylacetonate (Al (CH ₇ O ₂ ) ₃ ). aluminum may also be an aluminum oxide or hydroxide.

The surfactant used for the preparation of the mixture according to step b) of the first process for preparing said material with hierarchical porosity or step a ') of the second process for preparing said hierarchically porous material is an ionic or nonionic surfactant or a mix of both. Preferably, the ionic surfactant is chosen from phosphonium or ammonium ions and very preferably from quaternary ammonium salts such as ethyltrimethylammonium bromide (CTAB). Preferably, the nonionic surfactant may be any copolymer having at least two parts of different polarities conferring properties of amphiphilic macromolecules. These copolymers may be part of the non-exhaustive list of the following families of copolymers: fluorinated copolymers (- [CH ₂ -CH ₂ -CH ₂ -CI-I ₂ -O-CO-RI- with R 1 = C ₄ F ₉ , C ₈ F ₁₇ , etc.), biological copolymers such as polyamino acids (poly-lysine, alginates, etc.), dendrimers, block copolymers consisting of poly (alkylene oxide) chains and any other copolymer with character amphiphilic known to those skilled in the art (S. Fôrster, M. Antionnetti, Adv.Mater, 1998, 10, 195-217, S. Fôrster, T.PIantenberg, Angew Chem Int.Ed, 2002, 41, 688 -714, H. Colfen, Macromol Rapid Rapid, 2001, 22, 219-252). In the context of the present invention, a block copolymer consisting of poly (alkylene oxide) chains is preferably used. Said block copolymer is preferably a block copolymer having two, three or four blocks, each block consisting of a poly (alkylene oxide) chain. For a two-block copolymer, one of the blocks consists of a poly (alkylene oxide) chain of hydrophilic nature and the other block consists of a poly (alkylene oxide) chain of a nature hydrophobic. For a three-block copolymer, two of the blocks consist of a chain of poly (alkylene oxide) of hydrophilic nature while the other block, located between the two blocks with the hydrophilic parts, consists of a chain of poly (alkylene oxide) hydrophobic nature. Preferably, in the case of a three-block copolymer, the hydrophilic poly (alkylene oxide) chains are poly (ethylene oxide) chains denoted by (PEO) _x and (PEO) ₂ and the Poly (alkylene oxide) chains of hydrophobic nature are chains of poly (propylene oxide) denoted (PPO) _y , poly (butylene oxide) chains, or mixed chains, each chain of which is a mixture of several alkylene oxide monomers. Very preferably, in the case of a three-block copolymer, there is used a compound of formula (PEO) _x - (PPO) _y - (PEO) _z where x is between 5 and 300 and y is between 33. and 300 and z is between 5 and 300. Preferably, the values of x and z are the same. We use very advantageously a compound in which x = 20, y = 70 and z = 20 (P123) and a compound in which x = 106, y = 70 and z = 106 (F127). Commercial nonionic surfactants known as Pluronic (BASF), Tetronic (BASF), Triton (Sigma), Tergitol (Union Carbide), Brij (Aldrich) are useful as nonionic surfactants in step b ) of the first method for preparing the material having a hierarchical porosity comprising silicon constituting the catalyst according to the invention, respectively in step a ') of the second process for preparing said hierarchically porous material. For a four-block copolymer, two of the blocks consist of a chain of poly (alkylene oxide) hydrophilic nature and the other two blocks consist of a chain of poly (oxides) of alkylene hydrophobic nature.

The solution in which are mixed at least one silicic precursor, optionally at least one precursor of at least one element X, preferably an aluminum precursor, at least one surfactant and, according to step b) of the first process for preparing said material hierarchically porous, the colloidal solution in which are dispersed said zeolite nanocrystals previously synthesized, respectively according to step a ') of the second method of preparation of said hierarchically porous material, crystals of zeolites and / or related solids dispersing in said solution, in the form of nanocrystals of maximum nanometric size equal to 500 nm, can be acidic, neutral or basic. Preferably, said solution is acidic and has a maximum pH equal to 2, preferably between 0 and 2. The acids used to obtain an acid solution of maximum pH equal to 2 are, without limitation, hydrochloric acid, sulfuric acid and nitric acid. Said solution may be aqueous or may be a water-organic solvent mixture, the organic solvent preferably being a polar solvent, especially an alcohol, preferably ethanol. Said solution may also be substantially organic, preferably substantially alcoholic, the amount of water being such that the hydrolysis of the inorganic precursors is ensured (stoichiometric amount). Very preferably, said solution in which at least one silicic precursor is mixed, optionally at least one precursor of at least one element X, preferably an aluminum precursor, at least one surfactant and, according to step b) of the first process for the preparation of said material with hierarchical porosity, the colloidal solution in which said zeolite nanocrystals previously synthesized are dispersed, respectively according to step a ') of the second process for preparing said hierarchically porous material with crystals of zeolites and / or related solids, dispersant, in said solution, in the form of nanocrystals of maximum nanometric size equal to 500 nm, is an acidic aqueous-organic mixture, very preferably an acid-alcohol water mixture. In the preferred case where the matrix of said hierarchically porous material contains aluminum, the silicic and aluminic precursor concentrations in step b) of the first process for preparing said hierarchically porous material, respectively in step a ') of the second method of preparation of said hierarchically porous material are defined by the Si / Al molar ratio, the latter being at least 1, preferably between 1 and 1000, and very preferably between 1 and 100. quantity of zeolitic nanocrystals dispersed in the colloidal solution introduced during step b) of the first process for preparing said material with hierarchical porosity, respectively that of the crystals of zeolites and / or related solids introduced during step a ') of the second method of preparation of said hierarchically porous material is such that the zeolite nanocrystals r preferably represent from 0.1 to 40% by weight, preferably from 0.1 to 20% by weight and very preferably from 0.1 to 10% by weight of said material with hierarchical porosity.

The initial concentration of surfactant introduced into the mixture according to step b) of the first process for preparing said material with hierarchical porosity, respectively in step a ') of the second process for preparing said material with hierarchical porosity is defined by c ₀ and c _Q is defined with respect to the critical micelle concentration (c _mc ) well known to those skilled in the art. The c _max is the limit concentration beyond which occurs the phenomenon of self-arranging molecules of the surfactant in the solution. The concentration C ₀ can be lower, equal to or greater than the c _mc , preferably it is lower than the c _mc . In a preferred implementation of one or other of the methods of said hierarchically porous material, the concentration c ₀ is less than the c _mc and said solution referred to in step b) of the first process for preparing said material to hierarchical porosity, respectively in step a ') of the second method for preparing said hierarchically porous material is an acid-alcohol water mixture.

The step of atomizing the mixture according to step c) of the first process for preparing said hierarchically porous material, respectively according to step b ') of the second process for preparing said hierarchically porous material, produces spherical droplets of diameter preferably in the range of 2 to 200 μm. The size distribution of these droplets is lognormal. The aerosol generator used here is a commercial model 3078 device provided by TSI. The atomization of the solution is carried out in a chamber in which a carrier gas, an O ₂ / N ₂ mixture (dry air), is sent at a pressure P equal to 1.5 bar. In accordance with step d) of the first method for preparing said hierarchically porous material, respectively in step c ') of the second method of preparation of said hierarchically porous material, said droplets are dried. This drying is carried out by transporting said droplets via the carrier gas, the O ₂ / N ₂ mixture, in glass tubes, which leads to the gradual evaporation of the solution, for example from the aquo-organic acid solution, and thus to obtaining spherical elementary particles. This drying is perfect by a passage of said particles in a furnace whose temperature can be adjusted, the usual range of temperature ranging from 50 to 600 ⁰ C and preferably from 80 to 400 ° C, the residence time of these particles in the oven being of the order of 3 to 4 seconds. The particles are then collected in a filter and constitute the hierarchized porosity material comprising silicon and present in the catalyst according to the invention. A pump placed at the end of the circuit promotes the routing of species in the aerosol experimental device.

In the case where the solution referred to in step b) of the first process for preparing said hierarchically porous material, respectively in step a ') of the second process for preparing said hierarchically porous material is a water-organic solvent mixture, preferably acid, it is essential during step b) of the first method of preparation of said hierarchically porous material, respectively of step a ') of the second method of preparation of said hierarchical porosity material that the surfactant concentration at the origin of the mesostructuration of the matrix is below the critical micellar concentration so that the evaporation of said aqueous-organic solution, preferably acidic, during step c) of the first process for preparing said hierarchically porous material , respectively of step b ') of the second process for preparing said hierarchically porous material by the aerosol technique induces a miceilization or self-assembly phenomenon leading to the mesostructuration of the matrix of said hierarchically porous material around the zeolitic nanocrystals which remain unchanged in their shape and their size during steps c) and d ) of the first method of preparing said hierarchically porous material, respectively b ') and c') of the second method for preparing said material with hierarchical porosity. When c _o <c _mc , the mesostructuration of the matrix of said hierarchically porous material and prepared according to one or other of the processes described above is consecutive to a progressive concentration, within each droplet, of the silicic precursor, optionally the precursor of the element X, preferably the aluminum precursor and the surfactant, up to a concentration of surfactant c> c _mc resulting from evaporation of the aqueous-organic solution, preferably acidic. In general, the increase in the combined concentration of the silicic precursor and optionally the precursor of the element X, preferably of the aluminum precursor, and the surfactant cause the precipitation of the silicic precursor and possibly the. precursor of the element X, preferably of the aluminic precursor, around the self-organized surfactant and consequently the structuring of the matrix of said hierarchically porous material. The inorganic / inorganic phase interactions, organic / organic phases and organic / inorganic phases lead by a cooperative self-assembly mechanism to the hydrolysis / condensation of the silicic precursor and optionally of the precursor of the element X, preferably of the aluminum precursor, around the surfactant. During this self-assembly phenomenon, the zeolitic nanocrystals are trapped in the mesostructured silicon oxide-based matrix included in each of the elementary spherical particles constituting said hierarchically porous material. The aerosol technique is particularly advantageous for the implementation of step c) of the first process for preparing said hierarchically porous material, respectively of step b ') of the second method for preparing said material with hierarchical porosity, so as to to constrain the reagents present in the initial solution to interact with each other, no loss of material except the solvents, that is to say the solution, preferably the aqueous solution, preferably acidic, and optionally added with a polar solvent, n being possible, all the silicon, possibly the element X, and the zeolite nanocrystals initially present are thus perfectly preserved throughout each of the processes for preparing said material with hierarchical porosity instead of being potentially eliminated during the steps of filtration and washes encountered in conventional synthesis processes known to those skilled in the art. The drying of the droplets according to step d) of the first process for preparing said hierarchically porous material respectively according to step c ') of the second process for preparing said hierarchically porous material is advantageously followed by a passage in the oven at a temperature of between 50 and 150 ° C. The removal of the structuring agent and the surfactant in accordance with step e) of the first process for the preparation of said material with hierarchical porosity, respectively the elimination of at least one surfactant according to step d) of the second process for preparing said hierarchically porous material in order to obtain said hierarchically porous material according to the invention is advantageously carried out by chemical extraction processes or by thermal treatment and preferably by calcination under air in a temperature range of 300 to 1000 ° C and more precisely in a range of 500 to 600 ⁰ C for a period of 1 to 24 hours and preferably for a period of 2 to 6 hours.

The material having a hierarchical porosity comprising silicon and present in the catalyst according to the invention can be obtained in the form of powder or crushed compacted powder. sieved, ground powder, suspension, balls, pellets, wheels, tablets, spheres, granules, or extrudates, the shaping operations being carried out by conventional techniques known to man of the occupation (for example by extrusion, pelletizing, by the method of drop coagulation (oil-drop), by rotating plate granulation, etc.). In particular, it is possible to add to said hierarchically porous material a porous mineral binder amorphous or poorly crystallized oxide type. Said porous inorganic binder, usually amorphous, generally consists of at least one refractory oxide chosen from the group formed by alumina, silica, clays, titanium oxide, boron oxide and zirconia. The binder can consist of a mixture of at least two of the oxides mentioned above, for example an aluminosilicate. It is also possible to choose aluminates. It is preferred to use binders containing alumina, in all its forms known to those skilled in the art, for example gamma-alumina. It is also advantageous to use mixtures of alumina and silica, mixtures of alumina and aluminosilicate. Preferably, said material having a hierarchical porosity is obtained in the form of powder, crushed compacted sieved powder or extrudates, consisting of elementary spherical particles having a maximum diameter of 100 μm.

It should be noted that steps e) of the first method for preparing said material with hierarchical porosity and d) of the second method for preparing said material with hierarchical porosity can be performed before or after any shaping step described above of said material having a hierarchical porosity and comprising silicon, as well as any step of preparation of the catalyst according to the invention described below.

The catalyst according to the invention is prepared according to a process comprising mixing said hierarchically porous material with at least one active phase containing at least one group VIB and / or VIII hydro-dehydrogenating element.

The material having a hierarchical porosity present in the catalyst according to the invention is calcined during the preparation of said catalyst, advantageously before mixing with said active phase. The calcination treatment is usually performed in air at a temperature of at least 150 ° C, preferably at least 300 ⁰ C ₁ more preferably between about 350 and 1000 ⁰ C and even more preferably between 350 and 800 ⁰ C. In the rest of the text, said hierarchically porous material, optionally shaped and possibly having undergone a heat treatment will be called "support" of the catalyst according to the invention. The elements of group VIB and / or the elements of group VIII and optionally those chosen from phosphorus, boron, silicon and possibly elements of groups VB and VIIB may optionally be introduced, in whole or in part, before, during or after formatting said hierarchically porous material by any method known to those skilled in the art. Said elements may be introduced after shaping said hierarchical porosity material and after or before the drying and calcination of said shaped material.

According to a preferred embodiment of said process for preparing the catalyst according to the invention, the active phase containing at least one hydrodehydrogenating element of group VIB and / or VIII, optionally the elements chosen from phosphorus, boron, silicon and optionally the elements of Groups VB and VIIB may be introduced during the shaping of said hierarchically porous material.

According to another preferred embodiment of the process for preparing the catalyst according to the invention, the active phase containing at least one group VIB hydrodehydrogenating element and / or VIII ₁ optionally the elements selected from phosphorus, boron, silicon and optionally the elements groups VB and VIIB may be introduced by one or more impregnation operations of the support, by a solution containing the precursors of these elements.

The introduction of (the) metal (ux) is preferably carried out by impregnation of the support.

In a preferred manner, the support is impregnated with an aqueous solution. The impregnation of the support is preferably carried out by the "dry" impregnation method well known to those skilled in the art. The impregnation can be carried out in a single step by a solution containing all the constituent elements of the final catalyst.

In the case where the catalyst of the present invention contains a group VIII metal and a group VIB metal, the Group VIII metals are preferably introduced by one or more impregnation operations of the shaped and calcined support, after those Group VIB or at the same time as the latter.

According to another preferred embodiment of the process for preparing the catalyst according to the present invention, the deposition of boron and silicon can also be carried out simultaneously in for example using a solution containing a boron salt and a silicon-type silicon compound.

The impregnation of niobium can be facilitated by the addition of oxalic acid and optionally ammonium oxalate in the solutions of niobium oxalate. Other compounds can be used to improve the solubility and facilitate the impregnation of niobium as is well known to those skilled in the art.

In the particular case of the final production of the catalyst according to the invention in the form of extrudates, it is advantageous to prepare catalysts having homogeneous concentrations of elements of groups VIB and / or of elements of group VIII, and possibly of phosphorus. , boron, silicon and optionally elements of groups VB, and VIIB along them. It is also advantageous to prepare catalysts having concentrations of elements of groups VIB and / or elements of group VIIl ₁ and possibly phosphorus, boron, silicon and possibly elements of groups VB, and VIIB at the heart and periphery. different. These catalysts have distribution profiles called "cuvette" or "dome". Another type of distribution is that in crust where the elements of the active phase are distributed on the surface.

In general, the ratio of the core / edge of the concentrations of elements of groups VIB and / or elements of group VIII, and optionally phosphorus, boron, silicon and optionally elements of groups VB, and VIIB is between 0, 1 and 3. In a variant of the invention, it is between 0.8 and 1.2. In another variant of the invention, it is between 0.3 and 0.8.

The Group VIB and Group VIII metals of the catalyst of the present invention may be present in whole or in part in metallic form and / or oxide and / or sulfide.

Among the sources of molybdenum and tungsten, it is possible to use oxides and hydroxides, molybdic and tungstic acids and their salts, in particular ammonium salts such as ammonium molybdate, ammonium heptamolybdate, tungstate and ammonium, phosphomolybdic acid, phosphotungstic acid and their salts, silicomolybdic acid, silicotungstic acid and their salts. Oxides and ammonium salts such as ammonium molybdate, ammonium heptamolybdate and ammonium tungstate are preferably used. The sources of group VIII elements that can be used are well known to those skilled in the art. For example, for non-noble metals, nitrates such as cobalt nitrate, nickel nitrate, sulphates, hydroxides such as cobalt hydroxides, nickel hydroxides, phosphates, halides (for example chlorides, bromides and fluorides), carboxylates (eg acetates and carbonates). For the noble metals will be used halides, for example chlorides, nitrates such as palladium nitrate, acids such as chloroplatinic acid, oxychlorides such as ammoniacal oxychloride ruthenium.

The preferred phosphorus source, phosphorus being used as a doping element, is orthophosphoric acid H ₃ PO ₄ , but its salts and esters such as ammonium phosphates are also suitable. The phosphorus may for example be introduced in the form of a mixture of phosphoric acid and a basic organic compound containing nitrogen such as ammonia, primary and secondary amines, cyclic amines, compounds of the family of pyridine and quinolines and compounds of the pyrrole family. Tungstophosphoric or tungstomolybdic acids can be used.

The phosphorus content, phosphorus being used as a doping element, is adjusted, without limiting the scope of the invention, so as to form a mixed compound in solution and / or on the support, for example tungsten - phosphorus or molybdenum-tungsten-phosphorus. These mixed compounds may be heteropolyanions. These compounds may be Anderson heteropolynanions, for example.

The source of boron, boron both used as a doping element, may be boric acid, preferably orthoboric acid H ₃ BO ₃ , biborate or ammonium pentaborate, boron oxide, boric esters. Boron may for example be introduced in the form of a mixture of boric acid, hydrogen peroxide and a basic organic compound containing nitrogen such as ammonia, primary and secondary amines, cyclic amines, compounds of the family of pyridine and quinolines and compounds of the pyrrole family. Boron may be introduced for example by a boric acid solution in a water / alcohol mixture.

Many silicon sources, silicon being used as a doping agent, can be employed. Thus, it is possible to use tetraethylorthosilicate Si (OEt) ₄ , siloxanes, polysiloxanes, silicones, silicone emulsions, halide silicates such as ammonium fluorosilicate (NH ₄ ) ₂ SiF ₆ or sodium fluorosilicate Na ₂ SiF ₆ . Silicomolybdic acid and its salts, silicotungstic acid and its salts can also be advantageously employed. The silicon may be added, for example, by impregnation of ethyl silicate in solution in a water / alcohol mixture. Silicon can be added, for example, by impregnating a silicon-type silicon compound or silicic acid suspended in water.

Group VB element sources that can be used are well known to those skilled in the art. For example, among the sources of niobium, it is possible to use oxides, such as diniobium pentoxide Nb ₂ Os, niobic acid Nb ₂ Os, H ₂ O, niobium hydroxides and polyoxoniobates, niobium alkoxides of formula Nb (ORi) ₃ where R1 is an alkyl radical, niobium oxalate NbO (HC ₂ O ₄ ) ₅ , ammonium niobate. Niobium oxalate or ammonium niobate is preferably used.

Sources of VIIA group elements 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. It is also possible to use hydrolyzable compounds which can release fluoride anions in water, such as ammonium fluorosilicate (NH ₄ ) ₂ SiF _B , silicon tetrafluoride SiF ₄ or sodium tetrafluoride Na ₂ SiFe. The fluorine may be introduced for example by impregnation with an aqueous solution of hydrofluoric acid or ammonium fluoride.

The impregnation of the material with a hierarchical porosity with the active phase and the possible metals of group VB, VIIB and those chosen from Si, B, P, is followed by drying at a temperature of between 50 and 300 ^° C. and calcination at a temperature between 300 and 1000 ⁰ C and more precisely between 500 and 600 ⁰ C for a period of 1 to 24 hours and preferably for a period of 2 to 6 hours.

The catalysts according to the invention can be manufactured and used in the form of powder, crushed compacted pressed powder, pellets, granules, tablets, rings, balls, wheels, spheres or extrudates, preferably in the form of sieved crushed compacted powder, spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm. The shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings. The cylindrical shape is preferably used, but any other shape may be used.

Hydrocarbon Charge Treatment Methods According to the Invention

The invention also relates to processes for the treatment of hydrocarbon cuts using the catalyst according to the invention.

More particularly, the invention relates to a hydrocracking and / or hydroconversion process as well as to a process for the hydrotreatment of hydrocarbon feedstocks using the catalyst according to the invention.

The hydrocracking and / or hydroconversion process and the hydrotreatment process according to the invention operate in the presence of hydrogen, at a temperature greater than 200 ^° C., at a pressure greater than 1 MPa, the space velocity being included between 0.1 and 20 h ^-1 and the amount of hydrogen introduced is such that the volume ratio by volume of hydrogen / liter of hydrocarbon is between 80 and 5000 l / l.

The catalysts according to the invention are advantageously used for hydrocracking and / or hydroconversion of hydrocarbon cuts.

The catalysts according to the invention can be used for the hydrotreatment of hydrocarbon feedstocks, said hydrotreating process can be placed alone or upstream of a hydrocracking and / or hydroconversion process on a hydrocracking catalyst based on zeolite or alumina-silica, preferably comprising nickel and tungsten.

Sulphidation of catalysts

Prior to the injection of the feedstock, the catalysts used in the process according to the present invention are preferably subjected beforehand to a sulphurization treatment making it possible, at least in part, to convert the metal species into sulphide before they come into contact with the feedstock. load to be processed. This activation treatment by sulfurization is well known to those skilled in the art and can be performed by any method already described in the literature either in-situ, that is to say in the reactor, or ex-situ. A conventional sulphurization method well known to those skilled in the art consists of heating the catalyst in the presence of hydrogen sulphide (pure or for example under a stream of a hydrogen / hydrogen sulphide mixture) at a temperature of between 150 and 800 ^° C. preferably between 250 and 600 ° C, usually in a crossed-bed reaction zone.

Reduction of noble metal catalysts

Prior to the injection of the feedstock, the noble metal hydrσcraking catalyst can be preliminarily subjected to a reduction treatment making it possible to transform, at least in part, the noble metal oxides into reduced noble metals. One of the preferred methods for carrying out the reduction of the catalyst is a treatment in hydrogen at a temperature of between 150 and 650 ^° C. and at a total pressure of between 0.1 and 20 MPa. It should also be noted that any ex-situ reduction method may be suitable. For example, reduction may comprise a holding at a temperature of 15O ⁰ C for 2 hours, followed by raising the temperature to 35O ⁰ C at 1 ° C per minute and then holding at 350 ⁰ C for 2 hours. During this reduction treatment, the hydrogen flow rate may be 1000 liters of hydrogen per liter of catalyst.

loads

A wide variety of fillers can be processed by the processes according to the invention described above. Generally they contain at least 20% volume and often at least 80% volume of compounds boiling above 340 ° C.

The feedstock may be, for example, LCOs (light cycle OII (light gas oils from a catalytic cracking unit)), atmospheric distillates, vacuum distillates, for example gas oils resulting from the direct distillation of the crude or from conversion units. such as FCC, coker or visbreaking, as well as feeds from aromatics extraction units of lubricating oil bases or from solvent dewaxing of lubricating oil bases, or distillates from processes for desulphurization or hydroconversion in fixed bed or bubbling bed of RAT (atmospheric residues) and / or RSV (vacuum residues) and / or deasphalted oils, or the charge can be a deasphalted oil, or any mixture of the aforementioned charges. The above list is not exhaustive. Paraffins from the Fischer-Tropsch process are excluded. In general, the feeds have a T5 boiling point greater than 340 ⁰ C, and more preferably greater than 37o C ⁰ ₁ i.e. 95% of the compounds present in the feed have a boiling point at 340 ⁰ C, and more preferably greater than 370 ⁰ C.

The nitrogen content of the feedstocks treated in the processes according to the invention is usually greater than 500 ppm by weight, preferably between 500 and 10000 ppm by weight, more preferably between 700 and 4000 ppm by weight and even more preferably between 1000 and 1000 ppm by weight. and 4000 ppm weight. The sulfur content of the fillers treated in the processes according to the invention is usually between 0.01 and 5% by weight, preferably between 0.2 and 4% by weight and even more preferably between 0.5 and 2%. % weight

The charge may optionally contain metals. The cumulative nickel and vanadium content of the feeds treated in the processes according to the invention is preferably less than 1 ppm by weight.

The asphaltene content is generally less than 3000 ppm by weight, preferably less than 1000 ppm by weight, more preferably less than 200 ppm by weight.

Cribs

In the case where the feedstock contains resins and / or asphaltenes-type compounds, it is advantageous to first pass the feedstock over a bed of catalyst or adsorbent other than the hydrocracking and / or hydroconversion catalyst or catalyst. hydrotreating. The catalysts or guard beds used according to the invention are in the form of spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm. The shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings. The cylindrical shape is preferably used, but any other shape may be used.

In order to remedy the presence of contaminants and / or poisons in the feed, the guard catalysts may, in another preferred embodiment, have more particular geometric shapes in order to increase their void fraction. The void fraction of these catalysts is between 0.2 and 0.75. Their outer diameter can vary between 1 and 35 mm. Among the particular forms possible without this list being limiting: hollow cylinders, hollow rings, Raschig rings, serrated hollow cylinders, crenellated hollow cylinders, pentaring carts, multi-hole cylinders, etc.

These catalysts or guard beds may have been impregnated with an active phase or not. Preferably, the catalysts are impregnated with a hydro-dehydrogenation phase. Very preferably, the CoMo or NiMo phase is used.

These catalysts or guard beds may have macroporosity. Guard beds can be marketed by Norton-Saint-Gobain, for example, guard beds

MacroTrap®. Guard beds can be marketed by Axens in the ACT family:

ACT077, ACT935, ACT961 or HMC841, HMC845, HMC941 or HMC945. It may be particularly advantageous to superpose these catalysts in at least two different beds of varying heights. The catalysts having the highest void content are preferably used in the first catalytic bed or first catalytic reactor inlet.

It may also be advantageous to use at least two different reactors for these catalysts.

The preferred guard beds according to the invention are HMC and IΑCT961.

Operating conditions

Operating conditions such as temperature, pressure, hydrogen recycling rate, hourly space velocity, may be very variable depending on the nature of the load, the quality of desired products and facilities available to the refiner. The hydrocracking / hydroconversion or hydrotreatment catalyst is generally brought into contact, in the presence of hydrogen, with the charges described above, at a temperature greater than 200 ^° C., often between 250 and 480 ^° C., advantageously between 320 and 450 ⁰ C, preferably between 330 and 435 ° C, under a pressure greater than 1 MPa, usually between 2 and 25 MPa, preferably between 3 and 20 MPa ₁ space velocity is between 0.1 and 2Oh ^"1 and preferably ^{0,1-6h" 1,} preferably 0,2-3h ^"1, Ia and quantity of hydrogen introduced being such that the volume ratio of liter of hydrogen / liter of hydrocarbon is between 80 and 5000I / I and most often between 100 and 2000 l / l.

These operating conditions used in the processes according to the invention generally make it possible to achieve pass conversions, in products having points. boiling below 340 ° C, and better still below 370 ^c C, greater than 15% and even more preferably between 20 and 95%.

Modes of realization

The hydrocracking and / or hydroconversion processes using the catalysts according to the invention cover the pressure and conversion ranges from mild hydrocracking to high pressure hydrocracking. Mild hydrocracking is understood to mean hydrocracking leading to moderate conversions, generally less than 40%, and operating at low pressure, generally between 2 MPa and 6 MPa.

The catalyst of the present 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, optionally in combination with a hydrorefining catalyst located upstream of the catalyst of the present invention.

The catalyst of the present invention can be used alone, in one or more bubbling bed reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the unconverted fraction, optionally in combination with a catalyst. hydrorefining in a fixed bed or bubbling bed reactor upstream of the catalyst of the present invention.

The bubbling bed operates with removal of spent catalyst and daily addition of new catalyst to maintain stable catalyst activity.

One-step process

The so-called hydrocracking in one step, comprises first and generally a thorough hydrorefining which aims to achieve a hydrodenitrogenation and desulphurization of the load before it is sent to the hydrocracking catalyst itself , especially in the case where it comprises a zeolite. This extensive hydrorefining of the feed results in only a limited conversion of the feedstock into lighter fractions, which remains insufficient and must therefore be completed on the more active hydrocracking catalyst. However, it should be noted that no separation occurs between the two types of catalysts. All the effluent at the outlet of the reactor is injected onto the hydrocracking catalyst itself and only after that a separation of the formed products is achieved. This version of the hydrocracking, also called "Once Through", has a variant which has a recycling of the unconverted fraction to the reactor for further conversion of the charge.

One-step process in a fixed bed

For catalysts with a low silica content, the silica content by weight of the support used in the composition of the catalyst is between 5 and 30% and preferably between 5 and 20%.

For catalysts with a high silica content, the silica content by weight of the support used in the composition of the catalyst is between 20 and 80% and preferably between 30 and 60%.

In the case where the catalyst according to the present invention is used upstream of a zeolitic hydrocracking catalyst, for example based on zeolite Y, a catalyst having a low silica content as defined above will advantageously be used. It can also be advantageously used in combination with a hydrorefining catalyst, the latter being located upstream of the catalyst of the present invention.

When the catalyst according to the present invention is used upstream of an alumina-silica or zeolite-based hydrocracking catalyst, in the same reactor in separate catalytic beds or in separate reactors, the conversion is generally (or preferably) less than 50% by weight and preferably less than 40%.

The catalyst according to the invention can be used upstream or downstream of the zeolite catalyst. Downstream of the zeolite catalyst, it makes it possible to crack the HPA. By HPA is meant polyaromatic hydrocarbons as described in particular in the book "Hydrocracking, Science and Technology" J.Scherzer, Editions M.Dekker Incorporated, 1996.

One-step process in bubbling bed

The catalyst according to the invention can be used alone in one or more reactor (s). In the context of such a process, it will advantageously be possible to use several reactor (s) in series, the reactor (s) in bubbling bed containing the catalyst according to the invention being preceded by one or more reactor (s) containing at least one hydrorefining catalyst fixed bed or bubbling bed.

When the catalyst according to the present invention is used downstream of a hydrorefining catalyst, the conversion of the fraction of the charge caused by this hydrorefining catalyst is generally (or preferably) less than 30% by weight and preferably less than 25%.

One-step process in fixed bed with intermediate separation

The catalyst according to the present invention may also be used in a one-step hydrocracking process comprising a hydrorefining zone, an area allowing the partial elimination of ammonia, for example by a hot flash, and an area comprising a hydrocracking catalyst. This process for the hydrocracking of hydrocarbon feeds in one step for the production of middle distillates and optionally of oil bases comprises at least a first hydrorefining reaction zone, and at least a second reaction zone, in which hydrocracking is carried out. at least a part of the effluent of the first reaction zone. This process also comprises an incomplete separation of the ammonia from the effluent leaving the first zone. This separation is advantageously carried out by means of an intermediate hot flash. The hydrocracking performed in the second reaction zone is carried out in the presence of ammonia in an amount less than the amount present in the feed, preferably less than 1500 ppm by weight, more preferably less than 1000 ppm by weight and even more preferably lower. at 800 ppm weight of nitrogen. The catalyst of the present invention is preferably used in the hydrocracking reaction zone in association or not with a hydrorefining catalyst located upstream of the catalyst of the present invention.

The catalyst according to the invention can also be used in the first reaction zone in pretreatment converting, alone or in combination with a conventional hydrorefining catalyst, upstream of the catalyst according to the invention, in one or more catalytic bed (s). (s), in one or more reactor (s). One-step hydrocracking process with preliminary hydrorefining on low acid catalyst.

The catalyst according to the invention can be used in a hydrocracking process comprising: a first hydrorefining reaction zone in which the feedstock is brought into contact with at least one hydrorefining catalyst having, in the standard activity test, defined in French Patent No. 2,840,621 as well as in US patent application US 04 / 0,04,888, a cyclohexane conversion rate of less than 10% by weight,

a second hydrocracking reaction zone in which at least a portion of the effluent resulting from the hydrorefining stage is brought into contact with at least one hydrocracking catalyst having a conversion rate in the standard activity test; cyclohexane greater than 10% by weight, the catalyst according to the invention being present in at least one of the two reaction zones.

The proportion of the catalytic volume of hydrorefining catalyst generally represents 20 to 45% of the total catalytic volume.

The effluent from the first reaction zone is at least partly, preferably completely, introduced into the second reaction zone of said process. An intermediate separation of the gases can be carried out as previously described

The effluent leaving the second reaction zone is subjected to a so-called final separation (for example by atmospheric distillation optionally followed by vacuum distillation), so as to separate the gases. There is obtained at least one residual liquid fraction, essentially containing products whose boiling point is generally greater than 340 ° C., which may be at least partly recycled upstream of the second reaction zone of the process according to the invention, and preferably upstream of the hydrocracking catalyst based on alumina-silica, with a view to producing middle distillates.

The conversion to products having boiling points below 340 ° C. or even below 37 ^° C. is at least 50% by weight.

Two-step process In a so-called two-stage hydrocracking scheme with intermediate separation between the two reaction zones, in a given step, the catalyst of the present invention can be used in one or both reactors in association or not with a catalyst hydrorefining process upstream of the catalyst of the present invention.

The two-stage hydrocracking comprises a first step whose objective, as in the "one-step" process, is to perform the hydrorefining of the feedstock, but also to achieve a conversion of the latter of the order in general. from 40 to 60%. The effluent from the first step then undergoes separation (distillation), which is often called intermediate separation, which aims to separate the conversion products from the unconverted fraction. In the second step of a two-stage hydrocracking process, only the fraction of the unconverted feedstock in the first step is processed. This separation allows a two-stage hydrocracking process to be more selective in middle distillate (kerosene + diesel) than a one-step process. Indeed, the intermediate separation of the conversion products avoids their "over-cracking" in naphtha and gas in the second step on the hydrocracking catalyst. Furthermore, it should be noted that the unconverted fraction of the feedstock treated in the second stage generally contains very low levels of NH ₃ as well as organic nitrogen compounds, generally less than 20 ppm by weight or less than 10 ppm. weight.

The configurations of fixed-bed or ebullated-bed catalytic beds described in the case of a so-called one-step process can be used in the first step of a so-called two-step scheme, that the catalyst according to the invention is used alone. or in combination with a conventional hydrorefining catalyst.

For the so-called one-step processes and for the first step two-stage hydrocracking processes, the preferred catalysts according to the invention are doped catalysts based on non-noble group VIII elements, even more preferably catalysts. based on nickel and tungsten and the preferred doping element being phosphorus.

The catalysts used in the second stage of the two-stage hydrocracking processes are preferably the noble element-based doping catalysts of group VIII _1, still more preferably the platinum and / or palladium catalysts and the preferred doping element being phosphorus. Hydrotreating / hydroforming hydrocarbon feeds according to the invention

The catalysts according to the invention are used for the hydrotreatment and hydrorefining of hydrocarbon feeds such as petroleum cuts, coal cuts or hydrocarbons produced from natural gas and more particularly for hydrogenation, hydrodesulfurization , hydrodenitrogenation, hydrodeoxygenation, hydrodearomatization and hydrodemetallation of hydrocarbon feeds containing aromatic and / or olefinic and / or naphthenic and / or paraffinic compounds, said feeds optionally containing metals and / or nitrogen and / or oxygen and / or sulfur.

More particularly, the feedstocks employed in the hydrotreatment processes are gasolines, gas oils, vacuum gas oils, atmospheric residues, vacuum residues, atmospheric distillates, vacuum distillates, heavy fuels, oils, waxes and paraffins, used oils, residues or deasphalted crudes, fillers derived from thermal or catalytic conversion processes and mixtures thereof. They generally contain heteroatoms such as sulfur, oxygen and nitrogen and / or at least one metal.

As mentioned above, the catalysts of the invention can be used in a large number of hydrorefining or hydrotreatment applications. The operating conditions that can be applied in these processes are usually: a temperature of 200 to 450 ° C, preferably between 250 and 440 ⁰ C, a pressure of 1 to 25 MPa, preferably between 1 and 18 MPa, a hourly volume velocity of 0.1 to 20 h ^-1 , preferably between 0.2 and 5 h ^-1 , a hydrogen / feed ratio expressed as a volume of hydrogen, measured under normal conditions of temperature and pressure, by volume generally from 80 l / l to 5000 l / l and most often from 100 l / l to 2000 l / l.

The following examples illustrate the present invention without, however, limiting its scope.

EXAMPLES

In the examples which follow, the aerosol technique used is that described above in the description of the invention. Example 1: Preparation of a catalyst C1 (invention

S1 support formatting

Preparation of a hierarchically porous material S1 consisting of zeolite nanocrystals of ZSM-5 type (MFI) (Si / Al = 50) at 3.7% by weight of the final material and a purely silicic mesostructured matrix.

0.14 g of dry-butoxide aluminum are added to a solution containing 7 g of tetrapropylammonium solution (20% TPAOH), 4.3 ml of water and 0.0092 g of sodium hydroxide. 6 g of TEOS (tetraethylorthosilicate) are then added to this solution, which is then stirred at room temperature so as to obtain a clear solution. The solution is steamed for 18 hours at T = 95 ° C. A white milky colloidal suspension containing nanocrystals of ZSM-5 with a mean size of 130 nm is then obtained. 400 μl of this solution are then added to a solution containing 30 g of ethanol, 15 ml of water, 4.5 g of TEOS, 0.036 ml of HCl and 1.4 g of surfactant F127. The pH of the solution is adjusted to 2 with HCl. The assembly is sent into the atomization chamber of the aerosol generator and the solution is sprayed in the form of fine droplets under the action of the carrier gas (dry air) introduced under pressure (P = 1.5 bar) as it is described above in the disclosure of the invention. The droplets are dried according to the protocol described in the disclosure of the invention above. The temperature of the drying oven is set at 350 ^° C. The harvested powder is then calcined under air for 5 hours at T = 55 ^° C. The solid is characterized by XRD at low angles and at large angles, by adsorption isotherm. The TEM analysis shows that the final material consists of nanocrystals of zeolite ZSM-5 entrapped in a purely silicic matrix with organized mesoporosity characterized by a vermicular structure. Isothermal analysis of nitrogen adsorption leads to a specific surface area of the final material of S _BET = 480 m ² / g and to a pore size in the mesopore domain characteristic of the purely silicic mesostructured matrix of φ = 6. 2 nm. The wide-angle XRD analysis leads to obtaining the diffractogram characteristic of zeolite ZSM-5 (size of the micropores, measured by XRD, of the order of 0.55 nm). The small-angle XRD analysis leads to the visualization of a correlation peak associated with the vermicular organization of the mesostructured matrix. The Bragg relation gives 2 d ^* sin (0.3) = 1.5406, ie d = 15 nm. The thickness of the amorphous walls of the purely silicic mesostructured matrix defined by e = d - φ is therefore e = 9 nm. A SEM photograph spherical elementary particles thus obtained indicate that these particles have a size characterized by a diameter ranging from 50 to 700 nm, the size distribution of these particles being centered around 300 nm. The material thus synthesized is used in the form of sieved crushed compacted powder.

The support S1 is thus obtained.

Preparation of Hydrocracking Catalyst According to the Invention C1

Catalyst C1 is obtained by dry impregnation of support S1 in the form of crushed compacted powder sieved with an aqueous solution containing tungsten and nickel salts. Tungsten salt is ammonium metatungstate and that of nickel is nickel nitrate Ni (N0 ₃ ) ₂ * 6H ₂ O. After maturation at room temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and then calcined at 500 ^° C. ⁰ C under dry air. The mass contents in WO ₃ , NiO of catalyst C1 are respectively 24.7% and 3.6%.

The characteristics of the catalyst C1 are as follows: The BET surface area is 280 m ² / g. The average mesoporous diameter, measured by mercury porosimetry, is 5.5 nm.

Example 2 Preparation of a catalyst C2 (invention

S2 support formatting

Preparation of an aluminosilicate material S2 having a hierarchical porosity consisting of zeolite nanocrystals of the ZSM-5 (MFI) type (Si / Al = 50) at 10% by weight of the final material and of a mesostructured aluminosilicate matrix (Si / Al = 4 ).

0.14 g of tri-sec-butoxide of aluminum are added to a solution containing 3.5 ml of TPAOH hydroxide, 0.01 g of sodium hydroxide and 4.3 ml of water. After dissolution of the aluminum alkoxide, 6 g of tetraethylorthosilicate (TEOS) are added. The solution is stirred at room temperature for 5 h and then autoclaved at T = 95 ° C for 12 h. The white solution obtained contains nanocrystals of ZSM-5 of 135 nm. This solution is centrifuged at 20,000 rpm for 30 minutes. The solid is redispersed in water then centrifuged again at 20000 rpm for 30 minutes. This washing is done twice. The nanocrystals form a gel dried in an oven overnight at 60 ^° C. 0.461 mg of these crystals are redispersed in a solution containing 30 g of ethanol, 15 ml of water, 3.59 g of TEOS, 1.03 g. g of AlCl ₃ , 6H ₂ O, 0.036 ml of HCl and 1.4 g of P123 surfactant by stirring with ultrasound for 24 hours. The assembly is sent into the atomization chamber of the aerosol generator and the solution is sprayed in the form of fine droplets under the action of the carrier gas (dry air) introduced under pressure (P = 1.5 bar) according to the method described in the disclosure of the invention above. The droplets are dried according to the protocol described in the disclosure of the invention above. The temperature of the drying oven is set at 350 ^° C. The harvested powder is then calcined under air for 5 hours at T = 550 ^° C. The solid is characterized by XRD at low angles and at large angles, by adsorption isotherm. The TEM analysis shows that the final material consists of nanocrystals of zeolite ZSM-5 entrapped in an aluminosilicate matrix with organized mesoporosity characterized by a vermicular structure. Isothermal analysis of nitrogen adsorption leads to a specific surface of the final material of S _BET ⁼ 478 m ² / g and to a pore size in the mesopore domain characteristic of the aluminosilicate mesostructured matrix of φ = 4 nm. The wide-angle XRD analysis leads to obtaining the diffractogram characteristic of zeolite ZSM-5 (size of the micropores of the order of 0.55 nm). The small-angle XRD analysis leads to the visualization of a correlation peak associated with the vermicular symmetry of the mesostructured matrix. The Bragg relation gives 2 d * sin (0.4) = 1, 5406, ie d = 11 nm. The thickness of the amorphous walls of the aluminosilicate mesostructured matrix defined by e = d - φ is therefore e = 7 nm. An SEM image of the spherical elementary particles thus obtained indicates that these particles have a size characterized by a diameter ranging from 50 to 700 nm, the size distribution of these particles being centered around 300 nm. The material thus synthesized is used in the form of sieved crushed compacted powder.

The support S2 is thus obtained.

Preparation of the hydrocracking catalyst according to the invention C2

The catalyst C2 is obtained by dry impregnation of the support S2 in the form of crushed compacted powder sieved with an aqueous solution containing tungsten and nickel salts. The tungsten salt is ammonium metatungstate (NH _{4) 2} Wi BH ₂ O ₄ and O ₂ OMH that of nickel is nickel nitrate Ni (NO ₃ ) ₂ * 6H ₂ O. After maturation at ambient temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and then calcined at 500 ^° C. C under dry air. The WO ₃ , NiO mass contents of the catalyst C2 are respectively 24.5% and 3.5%.

The characteristics of the catalyst C2 are as follows:

The BET surface is 301 m ² / g.

The average mesoporous diameter, measured by mercury porosimetry, is 3.8 nm.

Example 3 Preparation of a C3 Catalyst (Invention)

S3 support formatting

Preparation of an aluminosilicate material S3 having a hierarchical porosity consisting of nanocrystals of Y-type zeolites (FAU) (Si / Al = 1.7) at 3.7% by weight of the final material and a mesostructured aluminosilicate matrix (Si / Al) = 4).

3.52 g of aluminum isopropoxide are added to 19.46 g of a solution of tetramethylammonium hydroxide (TIvIAOH ₁ 40% by weight). The whole is stirred until complete dissolution. In parallel, 6.00 g of tetraethylorthosilicate (TEOS) are dissolved in 40 ml of water. The two solutions are then mixed with vigorous stirring for 30 minutes. The whole is kept in a closed environment at room temperature for 18 hours without stirring and then autoclaved at T = 90 ° C for 6 days. The colloidal suspension obtained contains zeolite Y nanocrystals of 30 to 120 nm. Once the synthesis is complete, the crystals are recovered by centrifugation (20000 rpm for one hour), redispersed in water (ultrasonic) and then recentrifuged until the solution after redispersion has a pH of about 7. The pH of the colloidal suspension of nanocrystals of zeolite Y is then adjusted to 9.5 by addition of a 0.1% solution of ammonia. 400 μl of this solution are then added to a solution containing 30 g of ethanol, 15 ml of water, 3.59 g of TEOS, 1.03 g of AlCl ₃ , 6H ₂ O, 0.036 ml of HCl and 4 g of surfactant P123 by ultrasonic stirring for 24 hours. The assembly is sent into the atomization chamber of the aerosol generator and the solution is sprayed in the form of fine droplets under the action of the carrier gas (dry air) introduced under pressure (P = 1.5 bars) according to the method described in the disclosure of the invention above. The droplets are dried according to the protocol described in the disclosure of the invention above. The temperature of the drying oven is set at 350 ^° C. The harvested powder is then calcined under air for 5 hours at T = 550 ^° C. The solid is characterized by X-ray at low angles and at large angles, by nitrogen adsorption isotherm, by TEM and by X-ray fluorescence. The TEM analysis shows that the final material consists of nanocrystals of zeolite Y trapped in a matrix. aluminosilicate with organized mesoporosity characterized by a vermicular structure. Isothermal analysis of nitrogen adsorption leads to a specific surface area of the final material of S _BET = 478 m ² / g and to a pore size in the mesopore domain characteristic of the mesostructured aluminosilcate matrix of φ = 4 nm. The large-angle XRD analysis leads to obtaining the characteristic diffractogram of zeolite Y (micropore size of about 0.74 nm). The small-angle XRD analysis leads to the visualization of a correlation peak associated with the vermicular symmetry of the mesostructured matrix. The Bragg relation gives 2 d ^* sin (0.4) = 1.5406, ie d = 11 nm. The thickness of the amorphous walls of the aluminosilicate mesostructured matrix defined by e = d - φ is therefore e = 7 nm. An SEM image of the spherical elementary particles thus obtained indicates that these particles have a size characterized by a diameter ranging from 50 to 700 nm, the size distribution of these particles being centered around 300 nm. The material thus synthesized is used in the form of sieved crushed compacted powder.

The support S3 is thus obtained.

Preparation of Hydrocracking Catalyst According to the Invention C3

The catalyst C3 is obtained by dry impregnation of the support S3 in the form of crushed compacted powder sieved with an aqueous solution containing tungsten and nickel salts. Tungsten salt is ammonium metatungstate and that of nickel is nickel nitrate Ni (NO ₃ ) ₂ * 6H ₂ O. After maturation at room temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and calcined at 500 ^° C. ° C under dry air. The mass contents of WO ₃ and NiO of catalyst C 3 are respectively 24.7% and 3.6%.

The characteristics of the catalyst C3 are the following: The BET surface area is 295 m ^z / g. The average mesoporous diameter, measured by mercury porosimetry, is 3.8 nm. Example 4 Preparation of a C4 Catalyst (Invention)

The catalyst C4 is obtained by dry impregnation of the support S3 in the form of crushed compacted powder sieved with an aqueous solution containing tungsten and nickel salts and phosphoric acid H ₃ PO ₄ . The tungsten salt is ammonium metatungstate (NH ₄ ) ₆ H ₂ W ₁₂ O ₄₀ * 4H ₂ O and that of nickel is nickel nitrate Ni (NO ₃ ) ₂ * 6H ₂ O. After maturation at room temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and then calcined at 500 ^° C. in dry air. The mass contents of WO ₃ , NiO and P ₂ O ₅ of catalyst C 4 are respectively 24.7%, 3.6% and 2%.

The characteristics of catalyst C4 are as follows: The BET surface area is 270 m ² / g.

The average mesoporous diameter, measured by mercury porosimetry, is 3.7 nm.

Example 5 Preparation of a C5 Catalyst (Invention)

The catalyst C5 is obtained by dry impregnation of the support S3 with an aqueous solution containing platinum and palladium salts. The platinum salt is hexachloroplatinic acid H ₂ PtCl _B * 6H ₂ θ and the palladium salt is palladium nitrate Pd (NO ₃ ) ₂ . After maturation at room temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and then calcined at 500 ^° C. under dry air. The final Pt content is 0.5% by weight. The final Pd content is 1.0% by weight.

The characteristics of catalyst C5 are as follows:

The BET surface is 460 m ² / g.

The average mesoporous diameter, measured by mercury porosimetry, is 4.0 nm.

Example 6 Preparation of a C6 Catalyst (Invention)

Formatting the S4 medium

Preparation of a hierosized porosity aluminosilicate material S4 consisting of Y-type zeolite nanocrystals (FAU) (Si / Al = 1.7) at 15% by weight of the final material and of a mesostructured aluminosilicate matrix (Si / Al = 4 ). 14.25 g of aluminum isopropoxide are added to 78.81 g of a solution of tetramethylammonium hydroxide (TMAOH, 40% by weight). The whole is stirred until complete dissolution. In parallel, 24.30 g of tetraethylorthosilicate (TEOS) are dissolved in 162 ml of water. The two solutions are then mixed with vigorous stirring for 30 minutes. The whole is kept in a closed environment at room temperature for 18 h without agitation and then autoclaved at T = 9O ⁰ C for 6 days. The colloidal suspension obtained contains naecrystals of zeolite Y from 30 to 120 nm. Once the synthesis is complete, the crystals are recovered by centrifugation (20000 rpm for one hour), redispersed in water (ultrasonic) and then recentrifuged until the solution after redispersion has a pH of about 7. The pH of the colloidal suspension of nanocrystals of zeolite Y is then adjusted to 9.5 by addition of a 0.1% solution of ammonia. 1600 μl of this solution are then added to a solution containing 30 g of ethanol, 15 ml of water, 3.59 g of TEOS, 1.03 g of AlCl ₃ , 6H ₂ O, 0.036 ml of HCl and 4 g of surfactant P123 by ultrasonic stirring for 24 hours. The assembly is sent into the atomization chamber of the aerosol generator and the solution is sprayed in the form of fine droplets under the action of the carrier gas (dry air) introduced under pressure (P = 1.5 bar) according to the method described in the disclosure of the invention above. The droplets are dried according to the protocol described in the disclosure of the invention above. The temperature of the drying oven is set at 350 ^° C. The harvested powder is then calcined under air for 5 hours at T = 55 ^° C. The solid is characterized by XRD at low angles and at large angles, by adsorption isotherm. The TEM analysis shows that the final material consists of nanocrystals of zeolite Y trapped in an aluminosilcate matrix with organized mesoporosity characterized by a vermicular structure. The nitrogen adsorption isothermal analysis leads to a specific surface area of the final material of S _BET = 530 m ² / g and to a pore size in the mesopore domain characteristic of the mesostructured aluminosilcate matrix of φ = 4 nm. The large-angle XRD analysis leads to obtaining the characteristic diffractogram of zeolite Y (micropore size of about 0.74 nm). The small-angle XRD analysis leads to the visualization of a correlation peak associated with the vermicular symmetry of the mesostructured matrix. The Bragg relation gives 2 d ^* sin (0.4) = 1.5406, ie d = 11 nm. The thickness of the amorphous walls of the aluminosilicate mesostructured matrix defined by e = d - φ is therefore e = 7 nm. An SEM image of the spherical elementary particles thus obtained indicates that these particles have a size characterized by a diameter ranging from 50 to 700 nm, the size distribution of these particles being particles being centered around 300 nm. The material thus synthesized is used in the form of sieved crushed compacted powder.

The support S4 is thus obtained.

Preparation of the Hydrocracking Catalyst According to the Invention C6

The catalyst C6 is obtained by dry impregnation of the support S4 in the form of crushed compacted powder sieved with an aqueous solution containing tungsten and nickel salts. The tungsten salt is ammonium metatungstate (NH ₄ J ₆ HaW ₁₂ O ₄₀ MH ₂ O and that of nickel is nickel nitrate Ni (NO ₃ ) ₂ * 6H ₂ O. After maturation at room temperature in an atmosphere saturated with water, the sieved crushed compacted powder is dried at 120 ^° C. overnight and then calcined at 500 ^° C. in dry air, The mass contents of WO ₃ and NiO of the catalyst C 6 are respectively 24.4% and 3.4 %.

The characteristics of catalyst C6 are as follows: The BET surface area is 325 m ² / g. The average mesoporous diameter, measured by mercury porosimetry, is 3.8 nm.

Example 7 Evaluation of Catalysts C1 C2, C3, C4 and C6 in hydrocracking of a vacuum distillate in a high pressure step

Catalysts C1, C2, C3, C4 and C6, the preparation of which is described in Examples 1, 2, 3, 4 and 6, are used to carry out the hydrocracking of a vacuum distillate, the main characteristics of which are given in the table. 1.

Table 1: Characteristics of the vacuum distillates

The catalysts C1, C2, C3, C4 and C6 were implemented according to the method of the invention using a pilot unit comprising 1 fixed bed reactor traversed, the fluids flow from bottom to top (up-flow).

Prior to the hydrocracking test, the catalysts are sulphurized at 14 MPa at 350 ^° C. using a straight-run gas oil supplemented with 2% by weight of DMDS.

After sulphurization, the catalytic tests were carried out under the following conditions: Total pressure: 14 MPa Hydrogen flow rate: 1000 liters of hydrogen gas per liter of injected charge The space velocity (WH) is equal to 0.7 h -1 . Temperature: temperature required to reach 70% net conversion.

The catalytic performances are expressed by the temperature required to reach 70% net conversion to products having a boiling point below 370 ^° C., by the gross selectivity of the middle distillate cut at 150 ° -370 °. Conversion and selectivity are expressed from simulated distillation results.

The net conversion to products having a boiling point of less than 370 ° C, denoted CN 370 ⁰ C, is taken as:

CN 370 ⁰ C = [(% of 37O ⁰ C ^" _effluents ) - (% of 370 ⁰ C ^" _load )] / [100 - (% of 370 ⁰ C ^" _load )] with

% 370 ° C _^"eff iu _e n _ts = weight content of compounds having lower boiling points

370 ° C in effiuents, and

% 370 ⁰ C _^"c h _a r _ge = weight content of compounds having lower boiling points

370 ° C in the load.

Gross selectivity for middle distillate cut 150-370 ⁰ C, denoted by SB DM is taken as: SB DM = [(fraction 150-370 iuents _eff)] / [(% of 370 ° C _{^{"effluent3)].}}

The catalytic performances obtained are given in Table 2 below. Table 2: Catalytic results in one-stage hydrocracking and high pressure

The preceding examples thus show the whole point of using a catalyst according to the invention to carry out hydrocracking of hydrocarbon feedstocks. In fact, the catalysts according to the invention make it possible to obtain high conversions of the feedstock and selectivities to interesting middle distillates.

Example 8 Evaluation of Catalysts C1, C2, C3 C4 and C6 in hydrocracking of a vacuum distillate in a high pressure stage in combination with a hydrorefining catalyst

Catalysts C1, C2, C3, C4 and C6 whose preparations are described in Examples 1, 2, 3, 4 and 6 are used under the conditions of the hydrocracking of vacuum distillates at high pressure (12 MPa). The catalysts C1, C2, C3, C4 and C6 are used in hydrocracking in combination with a hydrorefining catalyst, the latter being located upstream of the catalyst according to the invention. The main characteristics of the oil charge are given in Table 3.

Table 3: Characteristics of Vacuum Distillates

The catalytic test unit comprises two reactors in a fixed bed, with upward flow of the charge ("up-flow"). In each of the reactors, 40 ml of catalyst are introduced. In the first reactor, the one in which the feedstock passes first, is introduced the hydrotreatment first stage catalyst HR448 sold by Axens comprising a Group VI element and a group VIlI element deposited on alumina. In the second reactor, the one in which the feedstock passes last, the catalyst according to the invention (C1, C2, C3, C4 and C6) is introduced. Both catalysts undergo an in situ sulphurization step prior to reaction. The catalysts are sulphurized at 12 MPa at 350 ^° C. using a straight-run gas oil supplemented with 2% by weight of DMDS. Once the sulfurization is complete, the charge described above can be transformed.

The catalytic tests were carried out under the following conditions: Total pressure: 12 MPa

Hydrogen flow rate: 1000 liters of hydrogen gas per liter of injected charge The space velocity (WH) is equal to 0.9 h -1.

Temperature required to reach 70% net conversion.

The catalytic performances are expressed by the required temperature to reach 70% net conversion to products having a boiling point lower than 370 ° C, by the gross selectivity of middle distillate cuts 150-370 ° C. The conversion and selectivity are expressed from the simulated distillation results and the definitions are identical to those given in Example 7.

In the following Table 4, we have reported the required reaction temperature to obtain 70% net conversion and the crude selectivity for the catalysts according to the invention.

Table 4

The preceding examples thus show the whole point of using a catalyst according to the invention to carry out hydrocracking of hydrocarbon feedstocks. In fact, the catalysts according to the invention make it possible to obtain high conversions of the feed and selectivities in distillates of interest.

Example 9 Evaluation of Catalyst C5 under Conditions Simulating the Operation of the Second Reactor of a Hydrocracking Process in Two Steps

The feedstock of the second step is produced by hydrotreating a vacuum distillate on the hydrorefining catalyst HR448 marketed by Axens in the presence of hydrogen, at a temperature of 395 ^° C. and at a space velocity of 0.55 hours. 1. The product conversion to 380 ^° C. is approximately 50% by weight. After a separation step, the 380 ° C + fraction is collected and will serve as a charge for the second step. The physicochemical characteristics of this charge are given in Table 5:

Table 5: characteristics of the second stage load

This charge is injected into the hydrocracking test unit 2 ^EMS step which comprises a fixed bed reactor with upward circulation of the charge ( "up-flow"), into which is introduced the catalyst C5 prepared in Example 5. Before injection of the charge, the catalyst is reduced under pure hydrogen at 45 ^° C. for 2 hours. The operating conditions of the test unit are as follows: Total pressure: 14 MPa

Hydrogen flow rate: 1000 liters of hydrogen gas per liter of injected charge The space velocity (WH) is 1.1 h -1. Temperature: 39O ⁰ C.

The catalytic performances are expressed by the net conversion to products having a boiling point of less than 37 ^° C., by the crude selectivity of the middle distillate cut at 150-400 ^° C. and the Gasoil yield / kerosene yield ratio in the middle distillate fraction. They are expressed from the results of simulated distillation and the definitions are identical to those given in Example 7.

The catalytic performances obtained under these conditions are described in Table 6 of this example.

Table 6: Catalan results

The preceding example thus shows all the advantages of using a catalyst according to the invention to carry out hydrocracking of hydrocarbon feedstocks. In fact, the catalyst according to the invention makes it possible to obtain high conversions of the feedstock and selectivities in terms of interesting middle distillates.

EXAMPLE 10 Evaluation of Catalysts C1, C2, C3, C4 and C6 by Hydrocracking a Vacuum Distillate in a Step at Moderate Pressure (Gentle Hydrocyclic)

Catalysts C1, C2, C3, C4 and C6, the preparation of which is described in Examples 1, 2, 3, 4 and 6, are used to carry out the hydrocracking of a vacuum distillate, the main characteristics of which are given in the table. 7. Table 7: Characteristics of Vacuum Distillate

The catalysts C1, C2, C3, C4 and C6 were implemented according to the method of the invention using a pilot unit comprising 1 fixed bed reactor traversed, the fluids flow from bottom to top (up-flow).

Prior to the hydrocracking test, the catalysts are sulphurized at 5.5 MPa, at 350 ^° C. using a straight-run gas oil supplemented with 2% by weight of DMDS.

After sulphurisation, the catalytic tests were carried out under the following conditions:

Total pressure: 5.5 MPa

Hydrogen flow rate: 450 liters of hydrogen gas per liter of injected charge

The space velocity (WH) is equal to 0.8 h-1. Temperature: 405 ^° C.

The catalytic performances are expressed as the net conversion of products with a boiling point below 370 ⁰ C ₁ as the net selectivity for middle distillate cut 150- 370 ⁰ C and the yield ratio of gas oil / kerosene yield in the middle distillate fraction. They are expressed from the results of simulated distillation and the definitions are identical to those given in Example 7.

The catalytic performances obtained are given in Table 8 below. Table 8: Catalytic Results in Moderate Hydrothermal Hybridization

The preceding example thus shows all the advantages of using a catalyst according to the invention to carry out hydrocracking of hydrocarbon feedstocks. In fact, the catalyst according to the invention makes it possible to obtain high conversions of the feedstock and selectivities in terms of interesting middle distillates.

Claims

1. Catalyst comprising: at least one support formed of at least one material with hierarchical porosity comprising silicon and consisting of at least two elementary spherical particles, each of said spherical particles comprising zeolitic nanocrystals having a pore size of between 0.2 and 2 nm and a mesostructured silicon oxide matrix having a pore size of between 1, 5 and 30 nm and having amorphous walls with a thickness of between 1 and 30 nm, said elementary spherical particles having a maximum diameter of 100 μm, at least one active phase containing at least one group VIB hydro-dehydrogenating element and or group VIII of the Periodic Table. The catalyst of claim 1 wherein said hydro-dehydrogenating element of said active phase is selected from the group consisting of Group VIB elements. 3. Catalyst according to claim 2 wherein said hydro-dehydrogenating element of said active phase selected from the group formed by the elements of group VIB of the periodic table is molybdenum. 4. Catalyst according to claim 2 wherein said hydro-dehydrogenating element of said active phase selected from the group consisting of elements of Group VIB of the Periodic Table is tungsten. The catalyst of claim 1 wherein said hydro-dehydrogenating element of said active phase is selected from the group consisting of Group VII elements. 6. Catalyst according to claim 5 wherein said hydro-dehydrogenating element selected from the group formed by the elements of Group VIII of the Periodic Table, is selected from cobalt, nickel and platinum. The catalyst of claim 1 wherein said active phase is formed of at least one Group VIB element and at least one Group VIII element. The catalyst of claim 7 wherein said group VIlI element is nickel and said group VIB element is tungsten. 9. Catalyst according to one of claims 1 to 8 wherein said zeolite nanocrystals have a pore size of between 0.2 and 0.8 nm. 10. Catalyst according to one of claims 1 to 9 wherein said zeolitic nanocrystals comprise at least one zeolite selected from aluminosilicates ZSM-5, ZSM-48, ZSM-22, ZSM-23, ZBM-30, EU-1, EU-2, EU-11, Beta, zeolite A, Y, USY, VUSY, SDUSY, mordenite, NU-87, NU-88, NU-86, NU-85, IM-5, IM-12 and Ferrierite and / or at least one related solid selected from SAPO-11 and SAPO-34 silicoaluminophosphates. 11. Catalyst according to claim 10, in which said zeolitic nanocrystals comprise at least one zeolite chosen from aluminosilicates of structural type MFI ₁ BEA, FAU ₁ LTA and / or at least one related solid chosen from silicoaluminophosphates of structural type AEL, CHA. 12. Catalyst according to one of claims 1 to 11 wherein the spherical elementary particles have a diameter of between 50 nm to 10 microns. 13. Catalyst according to one of claims 1 to 11 wherein the mesostructured silicon oxide-based matrix of said hierarchically porous material, is entirely silicic. 14. Catalyst according to one of claims 1 to 11 wherein the mesostructured silicon oxide-based matrix of the hierarchically porous material comprises at least one element X selected from the group consisting of aluminum, titanium, aluminum, tungsten, zirconium, gallium, germanium, phosphorus, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum and yttrium. The catalyst of claim 14 wherein the X element is aluminum. 16. Process for hydrocracking and / or hydroconversion of hydrocarbon feedstocks using the catalyst according to one of claims 1 to 15 17. hydrocracking process and / or hydroconversion according to claim 16 as performed by the so-called one-step process. 18. hydrocracking process and / or hydroconversion according to claim 17 comprising at least a first hydrorefining reaction zone and at least a second reaction zone in which is carried out the hydrocracking of at least a portion of the effluent the first zone and having an incomplete separation of the ammonia effluent leaving the first zone. 19. Process for hydrocracking and / or hydroconversioπ according to Claim 17, comprising: a first hydrorefining reaction zone in which the feedstock is brought into contact with at least one hydrotreatment catalyst having in the standard activity test a cyclohexane conversion rate of less than 10% by weight. a second hydrocracking reaction zone in which at least a portion of the effluent originating from the hydrorefining stage is brought into contact with at least one hydrocracking catalyst having a cyclohexane conversion level in the standard activity test; greater than 10% by mass. 20. hydrocracking process and / or hydroconversion according to claim 16 as performed by the so-called two-step process. 21. Method according to one of claims 16 to 20 as it operates in a fixed bed. 22. Method according to one of claims 16 to 20 as it operates in a bubbling bed. 23. Process for hydrotreatment of hydrocarbon feedstocks using the catalyst according to one of claims 1 to 15. 24. The method of claim 23 as placed upstream of a hydrocracking process and / or hydroconversion. 25. Method according to one of claims 16 to 24 as it operates in the presence of hydrogen, at a temperature above 200 ⁰ C under a pressure greater than 1 MPa, the space velocity being between 0.1 and 20h-1 and the amount of hydrogen introduced is such that the volume ratio by liter of hydrogen / liter of hydrocarbon is between 80 and 5000 l / l. 26. Method according to one of claims 16 to 25 wherein the hydrocarbon feeds are selected from the group consisting of LCO (light cycle oil: light gas oils from a catalytic cracking unit), atmospheric distillates, distillates under vacuum, charges from aromatics extraction units of lubricating oil bases or from solvent dewaxing of lubricating oil bases, distillates from fixed bed or bed desulfurization or hydroconversion processes bubbling of RAT (atmospheric residues) and / or RSV (vacuum residues) and / or deasphalted oils, deasphalted oils, alone or in mixture. 27. Method according to one of claims 16 to 26 wherein said hydrocarbon feeds pass beforehand on a bed of catalyst or adsorbent other than the hydrocracking catalyst and / or hydroconversion or hydrotreating