Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
  • C10G47/12—Inorganic carriers
  • C10G47/16—Crystalline alumino-silicate carriers
  • C10G47/18—Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/85—Chromium, molybdenum or tungsten
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J29/00—Catalysts comprising molecular sieves
  • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/19—Catalysts containing parts with different compositions
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/04—Oxides
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
  • C10G47/12—Inorganic carriers
  • C10G47/14—Inorganic carriers the catalyst containing platinum group metals or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
  • C10G47/12—Inorganic carriers
  • C10G47/16—Crystalline alumino-silicate carriers
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
  • C10G47/12—Inorganic carriers
  • C10G47/16—Crystalline alumino-silicate carriers
  • C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
  • B01J2229/10—After treatment, characterised by the effect to be obtained
  • B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
  • B01J2229/30—After treatment, characterised by the means used
  • B01J2229/42—Addition of matrix or binder particles
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/24—Chromium, molybdenum or tungsten
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/74—Iron group metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/20—Sulfiding

Definitions

• the present invention is framed in the area of catalysts for hydrocracking, more particularly catalysts comprising at least one metal of group VIB, and at least one metal of group VIII, a matrix, and a microporous crystalline solid.
• Hydrocracking of heavy oil fractions is a process of great importance within the current refinery schemes, since it allows to obtain a wide variety of light products such as jet-fuel, medium distillates and light diesel from heavier and low feeds. intrinsic value.
• An advantage of the hydrocracking process with respect to other conversion processes, such as catalytic cracking, is that it produces medium distillates of excellent quality, while hydrocracking gasoline usually has a lower octane rating than that obtained by catalytic cracking.
• the great flexibility of the hydrocracking process allows the production of the different fractions to be adapted to market demand.
• Conventional hydrocracking catalysts are bifunctional in nature, that is, they are formed by the combination of a hydrogenating function and an acidic function.
• the hydrogenating function is given by the presence in the catalyst of one or more metals of group VIB of the periodic table of the elements such as molybdenum and tungsten, or by a combination of one or more metals of group VIII
• the acid function is generally associated with a high specific surface porous support that has surface acidity, such as halogenated alumina, mixed oxides such as amorphous silica-alumina, and zeolites. Both the activity and the selectivity to the different products of a bifunctional hydrocracking catalyst are largely determined by the balance between the hydrogenating function and the acidic function.
• the catalyst When the acid function is weak and the hydrogenating function is strong the catalyst is characterized by having a low hydrocracking activity, which forces to work at high reaction temperatures (above 400 ° C) or at space velocities (feed volume to be treated per unit volume of catalyst and per hour) very low (generally less than 2 h " ), and a high selectivity to medium distillates.
• a good hydrocracking catalyst must have an adequate balance between the acidic function and the hydrogenating function
• the supports with low acidic function most currently used in the formulation of conventional hydrocracking catalysts highlights the amorphous silica-alumina.
• the amorphous silica-alumina hydrocracking catalysts pres They have a good selectivity to middle distillates, but as already mentioned, they are characterized by low activity.
• the supports that have a stronger acid function are zeolites.
• zeo litas and specifically the zeolite Y with a Faujasite structure, are part of the formulation of the latest generation hydrocracking catalysts.
• zeolite-based hydrocracking catalysts have a higher activity than conventional amorphous silica-alumina-based catalysts, although their selectivity to medium distillates is generally lower than the latter.
• Some hydrocracking processes using zeolite-based catalysts Y are described, for example, in patents US-3,269,934 and US-3,524,809.
• the activity and selectivity of a hydrocracking catalyst based on zeolite Y can be altered by modifying the acidity of the zeolite, which depends largely on its chemical composition, and more specifically on the relationship between silicon atoms and aluminum atoms (ratio Si / Al) that are part of its crystalline structure. It is well known that the presence of an aluminum atom in tetrahedral coordination in the crystalline network of the zeolite generates a charge deficiency that is compensated by a proton, thus leading to the formation of an acid center of the Brónsted type. Therefore, it is possible, in principle, to control the acidity of the zeolite by varying the Si / Al ratio in the network.
• Hydrocracking catalysts based on zeolite Y with high Al content in the network have a high activity because they have a high concentration of Bronsted acid centers.
• these catalysts have a low selectivity to medium distillates since the presence of a large number of acid centers favors secondary cracking reactions favoring the formation of lighter products, such as gases and ⁇ afia.
• hydrocracking catalysts containing zeolite Y with low network Al content are more selective to medium distillates although they have a lower hydrocracking activity .
• zeolite Y In order to reduce the concentration of Al in the network and achieve the appropriate range of Si / Al ratios in hydrocracking catalysts, zeolite Y must undergo post-synthesis desaluminization treatments since this zeolite cannot be synthesized with a high Si / Al ratio . Such desaluminization treatments generally require the use of severe hydrothermal conditions that lead to a partial loss of the crystallinity of the zeolite.
• hydrocracking catalyst with good activity and selectivity to medium distillates based on a microporous crystalline solid with a topology such that it has cavities of a high volume similar to that of large pore zeolites, such as zeolite Y , and that can be obtained with a high Si / Al ratio in a single synthesis stage, avoiding subsequent desaluminization processes.
• microporous crystalline solid known as ITQ-21 is described in Spanish patent application P200101145. However, its use as a component of a hydrocracking catalyst is not described, nor is it suggested in said application.
• the Spanish application P20012287 also refers to said crystalline solid material, specifically its use in cracking; but its use is not described therein as a component of a hydrocracking catalyst in conjunction with group VIB or VIII metals.
• the present invention relates to a hydrocracking catalyst characterized in that it comprises - a hydrogenating component selected from at least one metal of group VIB, at least one metal of group VIII, and combinations thereof,
• At least one matrix comprising at least one oxide selected from an amorphous oxide, a low crystallinity oxide, and mixture of both, and - at least one microporous crystalline solid material having a molar composition in its calcined and anhydrous state given by
• the hydrocracking catalyst of the present invention comprises a hydrogenating component that is at least one metal from among the metals of groups VD3 and VIII of the periodic table.
• the element of the VIB group may be chromium, molybdenum, tungsten or mixtures thereof. In a preferred embodiment of the present invention the element of group VIB is selected from molybdenum and tungsten.
• the element of group VIII may be any of iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium, platinum and mixtures thereof.
• group VIII metals non-noble metals are preferred, preferably iron, cobalt and nickel.
• the hydrogenating component of the catalyst is given by the combination of at least one non-noble metal of group VIII and at least one metal of group VIB.
• Preferred combinations are: nickel-molybdenum, cobalt-molybdenum and nickel-tungsten, although optionally combinations of three elements, such as nickel-cobalt-molybdenum, can be used.
• the metals of group VIII and of the VLB group can be totally or partially in metallic form and / or in the form of oxide and / or in the form of sulphides.
• the second essential component of the catalyst is the microporous crystalline solid material that has a molar composition in its calcined and anhydrous state:
• X 2 O 3 «I 2 : ZO 2 , wherein preferably the trivalent element, X, is Al, B, Fe, In, Ga, Cr or mixtures thereof, preferably Al.
• Y is preferably a tetravalent element such as Si, Ti, Sn or mixtures of them, although Si is preferred.
• the crystalline solid material also has, in its calcined and synthesized form without calcining, an X-ray diffraction pattern that is different from other known crystalline solid materials, and whose most important diffraction lines are given in Table 1 for calcined form and in table 2 for the uncalcined form. It should be taken into account that the exact position of the diffraction peaks will depend on factors such as the chemical composition and crystal size of the material, among others.
• the diffraction data listed for this sample as single or single lines may be formed by multiple overlaps or overlapping reflections that, under certain conditions, such as differences in crystallographic changes, may appear as resolved or partially resolved lines.
• crystallographic changes may include small variations in the parameters of the unit cell and / or changes in the symmetry of the crystal, without a change in the connectivity between the atoms of the structure. These modifications, which also include changes in relative intensities may also be due to differences in the type and amount of compensation cations, network composition, crystal size and shape thereof, preferred orientation or the type of thermal or hydrothermal treatments suffered.
• the crystalline solid material has a high pore volume and with a pore diameter measured by adsorption of Ar corresponding to that of a large pore zeolite.
• this material can be synthesized directly with the appropriate Si / Al ratio without resorting to post-synthesis desaluminization processes.
• the third component of the catalyst of the present invention is a matrix, as defined above.
• Said matrix is preferably selected from one or more of the following groups: alumina, silica-alumina, silica, clays, magnesium oxide, titanium oxide, boron oxide, zirconium oxide, aluminum phosphates, zirconium phosphates, carbon and aluminates
• the matrix is formed by an amorphous inorganic oxide containing some form of alumina, and more specifically gamma-alumina is preferred.
• the catalyst of the present invention may contain, in addition to the three essential components, at least one acidity promoting element which is preferably selected from phosphorus and boron.
• the catalyst of the present invention may comprise at least one element of the VILA group.
• the element of the VIIA group is fluorine.
• the catalyst of the present invention has in a preferred embodiment a composition expressed in% by weight with respect to the total catalyst weight, which corresponds to:
• a hydrogenating component selected from at least one metal of group VIB, at least one metal of group VIII, and combinations thereof, preferably from 0.1 to 50%, and more preferably from 0.1 at 40%, - from 0.1 to 99% crystalline acid solid material, preferably from a
• said promoter element may be present in a proportion of:
• the catalyst comprises at least one element of the VIIA group
• said element may be present in the catalyst in a proportion: from 0 to 20% by weight with respect to the total weight of the catalyst.
• the VIIA group element is fluorine, and is present in the catalyst in a proportion of 0 to 20% by weight with respect to the total weight of the catalyst.
• the present invention has as a further object a process for the preparation of a catalyst as defined above comprising at least
• the hydrogenating component directly onto the matrix before being mixed with the crystalline acid solid.
• the preparation stage of the microporous crystalline solid it can be prepared from a reaction mixture containing H 2 O, optionally an oxide or other source of the trivalent element X, such as Al and / or B, an oxide or other source of the tetravalent element or elements Y, such as Si; a source of Ge, Z, such as GeO 2 , and an organic agent structure director (R).
• the structure directing agent is N (16) -methylparteinium hydroxide.
• fluorides and more specifically HF, or OH groups "can be used as mobilizing agents for silica and germanium oxide.
• Organic molecules and fluoride ions are occluded within the structure, if fluorides are used as a mobilizing agent, which can be removed by conventional means
• the organic component can be removed, for example by extraction and / or by heat treatment by heating at a temperature above 250 ° C for a period of time between 2 minutes and 25 hours.
• the crystalline solid material is preferably synthesized in the presence of an oxide or other source of a trivalent element, such as B and / or Al, preferably Al.
• composition of the reaction mixture has the following composition in terms of molar ratios of oxides:
• the crystallization of the microporous crystalline solid material can be carried out in static or stirring, in autoclaves at a temperature between 80 and 200 ° C, at times sufficient to achieve crystallization, for example between 12 hours and 30 days. It should be taken into account that the components of the synthesis mixture can come from different sources, and depending on these, crystallization times and conditions may vary.
• crystals of the previously synthesized microporous material, as seeds, in amounts of up to 15% by weight with respect to the total oxides, can be added to the synthesis mixture. These seeds can be added before or during the crystallization of the material.
• the crystals of the solid are separated from the mother liquors, and recovered.
• the compensation cations in the crystalline solid material in uncalcined form, or after thermal treatment, can be exchanged in the case of being present, by other cations such as metal ions, H + and precursors of H + such as NH + 4 .
• cations that can be introduced by ion exchange those that can have a positive role in the activity of the material as a catalyst are preferred, and more specifically cations such as H + , rare earth cations, and group VIII metals are preferred, as well as of the HA, IIIA, IVA, Va, IB, IIB, IIIB, IVB, VB, VIIB group of the periodic table of the elements.
• the protonic (acid) form of the crystalline solid material is preferred.
• the crystalline solid material can be subjected to a calcination treatment in the presence of water vapor and / or a mixture of water and air vapor or any of its components, at temperatures between 200 and 700 ° C for a time between 10 minutes and 5 hours.
• the hydrogenation component is incorporated in various alternative ways.
• step 2a) defined above the incorporation of the hydrogenating component is carried out on a mixture of the matrix and the microporous crystalline solid.
• step 2b) defined above the incorporation of the hydrogenating component is carried out directly on the matrix before being mixed with the crystalline acid solid.
• the incorporation of the hydrogenating component can be carried out by one or more ion exchange steps in case the incorporation is carried out on the mixture of the crystalline acid solid and the matrix.
• the incorporation of the hydrogenating component can be carried out by impregnation both in the case that it is carried out directly on the matrix and in the case that it is carried out on the mixture of matrix and crystalline solid.
• the impregnation can be carried out in one or more stages from a solution containing at least one precursor of at least one oxide of at least one metal among which groups VIB and VIII of the periodic table form.
• impregnation of the precursor (or precursors) of the oxide (s) of the element (s) of group VIII is preferably performed then, or at the same time, that the impregnation of the precursor (s) of the oxide (s) of the element (s) of the group VIB.
• the impregnation of these elements can be carried out by the pore volume method, also known as "dry” impregnation, in which the volume of the pores of the solid to be impregnated is filled with a solution containing at least one precursor of at least one of the metals of groups VIB and VIII.
• the impregnation can also be carried out with an excess solution containing at least one precursor of at least one of the metals of groups VIB and VIII. In this case, the excess solvent is slowly removed by evaporation under controlled conditions.
• nitrates, sulfates and halides are typically used as sources of the elements of group VIII.
• the catalyst contains at least one promoter element such as phosphorus and / or boron, and at least one element of the VIIA group, such as fluorine, these can be incorporated into any time during the preparation of the catalyst, preferably on the support that already contains the crystalline solid material and the matrix. It is also possible to incorporate the promoter element (s) and the VIIA group on the matrix, and then mix with the crystalline solid. These elements can be incorporated by any of the known methods, although the impregnation method is preferred, either at pore volume (“dry" impregnation) or in excess of solvent.
• orthophosphoric acid H 3 PO
• H 3 PO is preferred, although some of its salts and esters, such as ammonium phosphates, can also be used.
• Any source that is well known to those skilled in the art can be used as the source of the VIIA group element.
• fluorine hydrofluoric acid or its salts can be used as a source.
• fluorine compounds that can lead to the formation of fluoride by hydrolysis in the presence of water, such as ammonium fluorosilicate, (NH 4 ) 2 SiF 6 , silicon tetrafluoride, SiF 4 , or sodium tetrafluoride, Na 2 SiF 6 .
• the fluoride can be incorporated into the catalyst, for example, by impregnation from an aqueous solution of hydrofluoric acid or ammonium fluoride.
• calcination is carried out at temperatures between 150 ° C and 800 ° C.
• the catalyst of the present invention is subjected to a sulphuration step before coming into contact with the feed in order to transform, at least partially, the metals of groups VLB and VIII into the corresponding sulphides.
• the sulfuration treatment can be carried out by any of the methods described in the literature.
• a typical method of sulfurization is to heat the catalyst in the presence of a stream of pure hydrogen sulfide or a mixture of hydrogen sulfide and hydrogen or a stream containing hydrogen and liquid hydrocarbons which in turn contain at least one sulfur-containing compound in its composition.
• the sulfurization is preferably carried out at a temperature between 150 and 800 ° C. This process is generally carried out in a continuous fixed bed reactor.
• the present invention also aims at the use of the catalyst defined above in a hydrocracking process of a feed formed by hydrocarbons
• Said hydrocarbon feed may optionally contain sulfur and nitrogen in the form of organic compounds, as well as metals and oxygenated compounds.
• the feed can be subjected to a hydrotreatment process prior to hydrocracking in order to reduce their concentration to levels not harmful to the catalyst of the invention.
• the catalyst can be used for hydrocracking heavy fractions of hydrocarbons.
• These fractions can be of different origin, such as vacuum gasoil.
• these fractions contain at least 80% by volume of compounds with boiling points greater than 350 ° C, and preferably between 350 ° C and 580 ° C.
• These fractions generally contain heteroatoms, such as sulfur and nitrogen.
• the nitrogen content is usually between 1 and 5000 ppm (by weight), and the sulfur content is usually from 0.01% to 5% by weight.
• these fractions can be subjected to a hydrotreatment process prior to hydrocracking in order to decrease the concentration of heteroatoms or to eliminate some contaminating metals they may contain.
• the hydrocracking catalyst for hydrocarbon feeds of the present invention has high activity and selectivity to medium distillates.
• the hydrocarbon feed is contacted with the hydrocracking catalyst in the presence of hydrogen, generally in a fixed bed reactor.
• the conditions of the hydrocracking process may vary according to the nature of the food, the quality of the desired products, and the particular facilities of each refinery. Generally the temperature is usually higher than 200 ° C, and is often between 250 ° C and 480 ° C. The pressure is usually greater than 0.1 MPa and often greater than 1 MPa.
• the H 2 / hydrocarbon ratio is usually higher than 50 and generally between 80 and 5000 Nm 3 of H 2 per m 3 of feed.
• the spatial velocity (LHSV) is generally between 0.01 and 20 feed volumes per catalyst volume and per hour.
• the hydrocracking process is carried out at temperatures of 300 ° C to 500 ° C, pressures of 5 to 20 MPa, H 2 / hydrocarbon ratios of 200 to 1500 Nm 3 / m 3 and LHSV of 0.05 to 5 h "1 .
• Al-SC crystalline solid material containing aluminum in the network
• ROH is N (16) -methylparteinium hydroxide.
• the gel is heated at 175 ° C for 5 days in steel autoclaves with an internal Teflon sheath. After washing with distilled water and drying at 100 ° C, the Al-SC material is obtained. Subsequently, the Al-SC material is subjected to a calcination step at 500 ° C for 5 hours.
• This example illustrates the preparation of a hydrocracking catalyst containing the Al-SC material obtained according to the procedure described in the example 1, a matrix of gamma-alumina and nickel-molybdenum as a hydrogenating component, according to the invention.
• the Al-SC material obtained according to the procedure described in Example 1 is mixed with a gamma-alumina matrix (specific surface area of 122 m / g and pore volume of 0.21 cm / g) in a 1: 1 ratio by weight.
• the mixture is homogenized by adding distilled water to form a paste containing gamma-alumina and the Al-SC material in the appropriate proportions and stirring the paste for at least 15 minutes.
• the mixture is then dried in an oven at 100 ° C for 12 hours.
• SC is impregnated by the "dry" pore volume or impregnation method with an aqueous solution of ammonium heptamolybdate.
• the solid obtained is dried in an oven at 100 ° C for 12 hours and then calcined in muffle at 500 ° C for 3 hours.
• the calcined solid formed by the support which contains a mixture of gamma-alumina and Al-SC material, and by molybdenum oxide, is impregnated by the pore volume method with a solution containing the required amount of nitrate. nickel.
• the solid is dried in an oven at 100 ° C for 12 hours and then calcined in a flask at 500 ° C for 3 hours.
• the chemical composition of the catalyst prepared under these conditions, given as% by weight, is as follows:
• Example 3 This example shows the preparation of a hydrocracking catalyst containing the Al-SC material according to the invention in which the hydrogenating component is incorporated exclusively on the gamma-alumina matrix.
• the gamma-alumina matrix is impregnated with an aqueous solution of ammonium heptamolybdate by the pore volume method, the solid is dried in an oven at 100 ° C and calcined in a flask at 500 ° C following the same procedure described in Example 2.
• the solid formed by gamma-alumina and molybdenum oxide is impregnated with an aqueous solution of nickel nitrate at pore volume, oven dried at 100 ° C and subsequent calcination at 500 ° C under the conditions described in example 2.
• the gamma-alumina matrix containing molybdenum oxide and nickel oxide is mixed with the Al-SC material in the appropriate proportions to obtain a catalyst with the following chemical composition, given as% by weight:
• the hydrocracking experiments were carried out in a continuous fixed bed reactor loaded with 4.0 grams of catalyst diluted with silicon carbide to a total volume of 14 cm 3 . Before contacting the vacuum diesel with the catalyst, it was subjected to a sulphuration stage at 400 ° C for 8 hours in the presence of a mixture of H 2 S and H 2 (10% by volume of H 2 S) using a total gas flow of 442 cm 3 / min. Once the sulphidation stage was completed, the vacuum diesel was hydrocracked in the presence of hydrogen under the following reaction conditions: total pressure of 5.3 MPa, H 2 / diesel ratio of 1291 NmV, spatial velocity (WHSV) of 2.8 h "1. The conversion was adjusted by varying the reaction temperature between 385 ° C and 415 ° C.
• the conversion results and yields were determined after a period of catalyst stabilization, which was generally observed after 8-10 hours of contacting the diesel feed with the catalyst.
• the conversion has been calculated as the% by weight of products with a boiling point below 380 ° C present in the reactor effluent.
• Kerosene 150 ° C - 250 ° C
• Diesel 250 ° C - 380 ° C
• the selectivity to middle distillates has been calculated as the sum of the selectivities to kerosene and diesel oil (boiling range between 150 ° C and 380 ° C).
• the results of conversion and selectivity to the different product fractions obtained at different reaction temperatures are shown in Table 4.
• This example illustrates the activity and selectivity of a catalyst prepared according to example 2 according to the invention, for the hydrocracking of a vacuum diesel oil whose main characteristics are shown in Table 3.
• the hydrocracking experiments were carried out in a continuous fixed bed reactor loaded with 6.0 grams of catalyst diluted with silicon carbide to a total volume of 14 cm 3 . Before contacting the catalyst with the vacuum diesel, it was subjected to a sulphuration stage at 400 ° C for 8 hours in the presence of a mixture of H 2 S and H 2 (10% by volume of H 2 S) using a total gas flow of 442 cm 3 / min. Once the sulphidation stage was completed, the vacuum diesel was hydrocracked in the presence of hydrogen under the following reaction conditions: total pressure of 5.3 MPa, H 2 / diesel ratio of 1291 Nm / m, spatial velocity (WHSV) of 1.9 h "1. The conversion was adjusted by varying the reaction temperature between 385 ° C and 415 ° C. TABLE 5

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