EP1159066A1 - Catalyseur contenant une zeolithe chargee en element du groupe vb et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarbonees - Google Patents
Catalyseur contenant une zeolithe chargee en element du groupe vb et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarboneesInfo
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- EP1159066A1 EP1159066A1 EP00945980A EP00945980A EP1159066A1 EP 1159066 A1 EP1159066 A1 EP 1159066A1 EP 00945980 A EP00945980 A EP 00945980A EP 00945980 A EP00945980 A EP 00945980A EP 1159066 A1 EP1159066 A1 EP 1159066A1
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- European Patent Office
- Prior art keywords
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- zeolite
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Classifications
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- 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
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/076—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- 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
Definitions
- the present invention relates to a catalyst which can be used for hydrorefining and hydrocracking of hydrocarbon feedstocks under hydrogen pressure, said catalyst comprising at least one zeolite (preferably zeolite Y or beta) and at least one oxide matrix, the zeolite containing in its porous network at least one metal of group VB (group 5 according to the new notation of the periodic classification of elements: Handbook of Chemistry and Physics, 76th edition, 1995-1996), (preferably niobium) and possibly at least one noble or non-noble group VIII metal (groups 8, 9 and 10) of said classification, preferably cobalt, nickel and iron.
- the oxide matrix contains at least one group VIB metal, advantageously molybdenum and tungsten, and / or at least one group VIII metal, advantageously cobalt, nickel and iron and / or at least one metal from group VB preferably niobium.
- the catalyst also contains at least one promoter element (phosphorus, boron, silicon).
- the present invention also relates to the processes for the preparation of said catalyst, as well as its use for hydrocracking hydrocarbon feedstocks such as petroleum cuts and cuts obtained from coal containing sulfur and nitrogen in the form of organic compounds, the said fillers possibly containing metals and / or oxygen
- the catalysts used in conventional hydrocracking are all of the bifunctional type combining an acid function with a hydrogenating function.
- the acid function is generally provided by supports of the crystalline aluminosilicate type called zeolites.
- the hydrogenating function is provided either by one or more metals from group VIII of the periodic table of elements, such as iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum, or by a combination of at least one metal of group VI of the periodic table such as chromium, molybdenum and tungsten and at least one metal of group VIII in general non-noble such as Co, ⁇ " ⁇ and Fe
- the zeolite-type supports for example of the Y-type or else pure or dealuminated beta, have a very high acidity.
- a hydrogenating function introduced into the zeolite can be provided by at least one element or compound comprising the element of group VB such as niobium, at least one element of group VIB and / or at least one element of group VIII.
- the element of group VB can be advantageously associated with at least one metal or compound of metal of group VIII. It is advantageously possible to use a combination of metals from group VB and optionally a combination of metals from group VIII.
- the invention relates to a catalyst containing at least one matrix, at least one zeolite, at least one element located at the level of the matrix (that is to say deposited on the catalyst or contained in the matrix) and chosen from the group formed by the elements of groups VIB, VIII and VB and at least one promoter element chosen from the group formed by phosphorus, boron, silicon, zeolite containing in its porous network at least one element of group VB
- the catalyst of the present invention generally contains in% by weight relative to the total mass of the catalyst:
- zeolite content is at least 5? ⁇ , preferably at least 15%, or even at least 20? ⁇ , - 1 to 99.7% or 1 to 97.9%, preferably 10 to 95% and even more preferably 15 to 95% of at least one amorphous oxide matrix, preferably an alumma, a silica or a silica-alumina,
- - 0 to 40% advantageously from 1 to 40%, preferably from 1.5 to 35% and even more preferably from 2 to 30% of at least one metal of group VIB (expressed by weight of oxide ), - 0 to 30? &, Advantageously from 0.1 to 30? ⁇ , preferably from 0.1 to 25% and even more preferably from 0.1 to 20% of at least one metal from group VIII (expressed by weight of oxide),
- the zeolite contains in its system porous (expressed by weight of oxide in the catalyst):
- the metal of group VB contained in the porous network of the zeolite can be the same or different from that contained in the matrix.
- the group VIII metal contained in the zeolite may be the same or different from that contained in the matrix.
- the demonstration of the presence of the hydrogenating phase in the porous network of the zeolite can be carried out by various methods known to those skilled in the art. profession such as for example the electron microprobe and the transmission electron microscopy equipped with an X energy dispersion spectrometer with detector allowing the identification and the quantification of the elements present in the crystals of the zeolite and in the oxide matrix.
- the catalyst of the present invention has a very high hydrocracking activity of hydrocarbon fractions and a higher selectivity than the catalytic formulas known in the prior art. Without wishing to be bound by any theory, it seems that this particularly high activity of the catalysts of the present invention is due to the combined presence of a hydrogenating function on the matrix and of element of group VB at se of the porous network of the zeolite, in combination with the presence of promoter element.
- the hydrogenating function on the matrix is provided by at least one element from groups VIII, VIB, VB, and preferably by at least one element from GVIB or advantageously by an element from GVIII, preferably a non-noble element (Co, Ni). .
- a combination of at least one element of the GVIII and at least one element of the GVIB will be used.
- the promoter element is mainly located on the matrix.
- the silicon introduced mainly located on the support matrix can be characterized by techniques such as the Castamg microprobe (distribution profile of the various elements), transmission electron microscopy coupled with an X-analysis of the components of the catalysts, or even by establishing a distribution map of the elements present in the catalyst by electronic microprobe.
- These local analyzes will provide the location of the various elements, in particular the location of the amorphous silica on the matrix due to the introduction of silicon.
- the location of the silicon in the framework of the zeolite is also revealed.
- a quantitative estimate of the local contents of silicon and other elements can be carried out.
- the NMR of the solid of : ° S ⁇ rotating at the magic angle is a technique which makes it possible to detect the presence of amorphous silica introduced into the catalyst according to the procedure described in the present invention.
- the catalyst of the present invention can be prepared by any method well known to those skilled in the art.
- a preparation method comprises the following stages: a) introduction into the zeolite of at least one element of group VB and optionally at least one element of group VIII and / or VIB b) mixing with the matrix and shaping to get support; c) introduction of at least one promoter element by impregnation and introduction of at least one element from groups VIB, VIII and VB into the matrix or on the support by at least one of the following methods: - addition of at least a compound of said element during shaping so as to introduce at least part of said element, - impregnation of the support with at least one compound of said element or ion exchange on the calcined support with a solution of at least one compound from the group
- VIII d drying and calcination of the final product obtained and optionally drying and / or calcination of the products obtained at the end of steps a) or b) or after impregnation.
- the catalyst of the present mvention is prepared according to the following three steps • a) mtroduction at moms a group VB metal and optionally at moms a metal of group VIII and / or VIB in the zeolite optionally followed by drying and calcination or calcination without prior drying. Drying can be carried out at a temperature between 60 and 250 ° C and calcination at a temperature between 250 and 800 ° C. b) shaping the mixture of the zeolite containing the metal of group VB and optionally the metal of group VIII obtained in step a) with the oxide matrix to obtain the support.
- One of the preferred shaping methods in the present invention consists in kneading the zeolite in a wet alumina gel for a few tens of mmutes, then in passing the dough thus obtained through a die to form extrudates of diameter preferably understood between 0.4 and 8 mm.
- the introduction of the elements of group VB and / or VIB and / or VIII not included in the zeolite may have taken place optionally at this stage by adding at least one compound of said element, so as to introduce at least part of said element.
- This introduction can be accompanied by that of phosphorus, boron, and / or silicon and possibly that of the element of the VIIA gourd (fluorine for example).
- the solid formed is then optionally dried at a temperature between 60 and 250 ° C and calcined at a temperature of 250 to 800 ° C.
- a deposition method well known to those skilled in the art is the impregnation of the support with a solution containing the elements of group VB and / or VIB and / or VIII, and promoter element (such as phosphorus).
- the deposit is then optionally followed by a drying at a temperature between 60 C and 250 C and optionally by a calcination at a temperature 250 to 800 ° C
- the oxide matrix is usually chosen from the group formed by transition aluminas, silicas and silica-aluminas and their mixtures. It is preferred to use matrices containing alumina, in all of its forms known to a person skilled in the art, for example gamma alumina.
- the preferred source of zeolite is Y zeolite or beta zeolite in all their forms.
- the zeolite can be in the hydrogen form or be at least partially exchanged with metal cations, for example using cations of alkaline earth metals and / or cations of rare earth metals with atomic number 57 to 71 mclus.
- the zeolite may be at least partially (ie more or less) quenched as it is well known to those skilled in the art.
- the sources of the VIB group element which can be used are well known to those skilled in the art.
- oxides and ammonium salts such as ammonium molybdate, ammonium heptamolybdate and ammonium metatungstate.
- the sources of element of the VB group which can be used are well known to those skilled in the art.
- oxides can be used, such as dimobium pentaoxide ⁇ ⁇ b2 ⁇ 5, mobic acid Nb2 ⁇ 5.H2 ⁇ , niobium hydroxides and polyoxomobates, niobium alkoxides of formula Nb (OR ⁇ ) 3 where Ri is an alkyl radical, niobium oxalate NbO (HC2 ⁇ ) 5, ammonium niobate.
- niobium oxalate or ammonium niobate is used.
- the sources of Group VIII elements which can be used are well known to those skilled in the art. For example, nitrates, sulfates, halides will be used.
- the preferred phosphorus source is 1 orthophospho ⁇ que acid H3PO4, but its salts and esters such as ammonium phosphates are also suitable.
- Phosphomolybdic acid and its salts, phosphotungstic acid and its salts can also be advantageously used.
- Phosphorus can for example be introduced in the form of a mixture of phospho ⁇ que acid and a basic organic compound containing nitrogen such as ammonia, primary and secondary animes, cyclic souls, compounds of the family of py ⁇ drne and quinolines and compounds of the pyrrole family.
- ethyl orthosihcate S ⁇ (OEt) 4 siloxanes, polysiloxanes, silicones, silicone emulsions, halide silicates such as ammonium fluorosilicate (NP;) SiFé or sodium fluorosilicate Na2S ⁇ F b .
- Silicomolybdic acid and its salts, silicotungstic acid and its salts can also be advantageously used.
- Silicon can be added, for example, by impregnation of ethyl silicate in solution in a water / alcohol mixture. Silicon can be added, for example, by impregnation of a silicon compound of silicone type suspended in water.
- the boron source can be boric acid, preferably orthoboric acid H3BO3, ammonium biborate or pentaborate, boron oxide, boric esters.
- Boron can 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 souls, cyclic souls, compounds of the family of py ⁇ drne and quinolines and compounds of the family of pyrrole. Boron can be introduced for example by a solution of boric acid in a water / alcohol mixture.
- 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.
- the salt is advantageously formed in the reaction mixture by reaction between the organic compound and hydrofluoric acid II is also possible to use sandable hvdrol compounds which can release fluoride anions in water, such as fluorosilicate ammonium (XFDiSiF ⁇ , silicon tetrafluoride S1F4 or sodium Na 2 S ⁇ F6 Fluorine can be introduced for example by impregnation of an aqueous solution of hydrofluoric acid or ammonium fluoride.
- fluorosilicate ammonium XFDiSiF ⁇ , silicon tetrafluoride S1F4 or sodium Na 2 S ⁇ F6 Fluorine
- the hydrogenating function relating to the matrix as previously defined can be introduced into the catalyst at various levels of the preparation and in various ways. It can be introduced only in part (case, for example, of associations of metal oxides of groups VI and VIII) or in whole at the time of the kneading of the source of alumina and of zeolite in step b) the rest of the hydrogenating element (s) then being introduced after kneading, and more generally after calcination.
- the group VIII metal is introduced simultaneously or after the group VI metal, whatever the mode of introduction.
- the hydrogenating function relating to the matrix can also be introduced by one or more ion exchange operations on the calcmated support (zeolite dispersed in the alumma matrix), using solutions containing the precursor salts of the metals chosen when these belong to group VIII.
- the hydrogenating function (element of group VIII) is then localized both in the porous network of the zeolite and on the matrix. In this case, it can be envisaged to limit the quantity of group VIII metal introduced into the zeolite before it is formed.
- the hydrogenating function relating to the matrix can also be introduced by one or more operations for impregnating the shaped and calmed support, by a solution of the precursors of the group VIII metal oxides when the precursors of the group VIB metal oxides and / or of the VB group were previously introduced at the time of the mixing of the support.
- the hydrogenating function relative to the matrix can finally be introduced by one or more operations of impregnation of the calcmated support constituted by the zeolite and the alumma matrix optionally doped with P, by solutions containing the precursors of the metal oxides of the VIB groups, VB and / or VIII, the precursors of group VIII metal oxides being preferably introduced after those of groups VB and VIB or at the same time as the latter.
- an intermediate calcination step of the catalyst must be carried out at a temperature between 250 and 600 ° C.
- the introduction of phosphorus, boron and / or silicon into the catalyst can be carried out at various stages of the preparation and in various ways.
- a preferred method according to the invention consists in preparing an aqueous solution of at least one element of group VI and / or at least one element of group VB and / or at least one element of group VIII and of a phosphorus compound, boron and / or silicon and to carry out a so-called dry impregnation, in which the pore volume of the precursor is filled with the solution.
- Phosphorus, boron and / or silicon can be introduced by one or more impregnation operations with excess solution on the calmated precursor.
- a preferred method consists in depositing, for example by impregnation, the promoter element (s) chosen, for example the boron-silicon couple, on the precursor, calmated or not, preferably calcmated.
- the promoter element (s) chosen for example the boron-silicon couple
- an aqueous solution of at least one boron salt such as ammonium biborate or ammonium pentaborate is prepared in an alkaline medium and in the presence of hydrogen peroxide and a so-called dry impregnation is carried out, in which filling the pore volume of the precursor with the boron-containing solution.
- a solution of a silicon compound of the silicone type will be used, for example.
- the deposition of boron and silicon can also be carried out simultaneously using, for example, a solution containing a boron salt and a silicon compound of the silicone type.
- Amsi for example it is possible to impregnate with an aqueous solution of ammonium biborate and silicone Rhodorsil E1P from the company Rhône Poulenc, to carry out a drying for example at 80 ° C., then optionally to impregnate with a solution ammonium fluoride, to carry out a drying for example at 80 ° C and to calcine for example preferably under air ht crossed, for example at 500 C C for 4 hours.
- a particular preparation comprises a) introduction of niobium into the zeolite. b) mixing with the matrix, shaping, calming, c) impregnating the calmed support with a solution of at least one nickel compound, at least one molybdenum compound and at least one promoter element (phosphorus by example), d) drying, calcmation
- the catalysts obtained by the present invention are shaped in the form of grams of different shapes and dimensions. They are generally used in the form of cylindrical or multi-lobed extrudates such as two-lobed, three-lobed, multi-lobed in a straight or twisted shape, but can optionally be manufactured and used in the form of crushed powder, tablets, rings, balls , wheels. They have a specific surface area measured by nitrogen adsorption according to the BET method (Brunauer, Emmett, Teller, J. Am. Chem.
- amsi catalysts obtained are generally used for hydrocracking, in particular of hydrocarbon cuts of the distillate type (kerosene, diesel), vacuum distillates, deasphalted residues or the like, the cuts possibly being possibly hydrotreated.
- hydrocarbon cuts of the distillate type kerosene, diesel
- vacuum distillates vacuum distillates
- deasphalted residues or the like the cuts possibly being possibly hydrotreated.
- the treated hydrocarbon feedstocks have initial boiling pumps of at least 150 ° C., preferably at least 350 ° C. and more advantageously it is a boiling cut between 350 and 620 ° C.
- the hydrocracked sections with the catalyst of the invention are preferably such that at least 80? 6 by volume corresponds to compounds whose boiling points are at least 320 ° C. and preferably between 350 and 620 ° C (i.e. corresponding to compounds containing at least 15 to 20 carbon atoms). They generally contain heteroatoms such as sulfur and nitrogen.
- the nitrogen content is usually between 1 and 5000 ppm by weight and the sulfur content between 0.01 and 5% by weight.
- the hydrocracking conditions such as temperature, pressure, hydrogen recycling rate, hourly volume speed, may be very variable depending on the nature of the load, the quality of the desired products and the facilities available to the refiner.
- the temperature is generally greater than 200 ° C and often between 250 ° C and 480 ° C.
- the pressure is greater than 0.1 MPa and often greater than 1 MPa.
- the recycling rate of hydrogen is at least 50 and often between 80 and 5000 normal liters of hydrogen per liter of charge.
- the hourly space velocity is generally between 0.1 and 20 volume of charge per volume of catalyst and per hour
- the catalyst of the present invention can be used in various cases of hydrocracking process associating one or more reactors in series with intermediate separation or not, with recycling of the residue or not.
- the catalyst can be used in any hydrocracking process known to a person skilled in the art, such as for example the one-step processes, with one or more catalysts with or without recycling of the gases and the liquid or in two steps with one or more several catalysts with or without separation between the two reactors with or without recycling of the gases and the liquid.
- the catalysts of the present invention are preferably subjected to a sulfurization treatment making it possible to transform, at least in part, the metallic species into sulphides before they are brought into contact with the charge to be treated.
- This activation treatment by sulfurization is well known to those skilled in the art and can be carried out by any method already described in the literature.
- a conventional sulphurization method well known to those skilled in the art consists of heating in the presence of hydrogen sulphide at a temperature between 150 and 800 ° C, preferably between 250 and 600 ° C, generally in a reaction zone with high ht .
- the catalyst of the present invention can be used for the hydrocracking of cuts (such as those of vacuum distillates) highly charged with sulfur and nitrogen which have been hydrotreated beforehand
- cuts such as those of vacuum distillates
- the petroleum cut conversion process takes place in two stages, the catalyst according to the invention being used in the second stage.
- the catalyst 1 of the first stage has a hydrotreatment function and comprises a matrix preferably based on alumina, and preferably not containing a zeolite, and at least one metal before a hydrogenating function.
- Said matrix can also consist of, or contain, ⁇ e silica, silica-alumina, oxide boron, magnesia, zirconia, titanium oxide or a combination of these oxides.
- the hydro-dehydrogenating function is ensured by at least one metal or compound of group VIII metal such as nickel and cobalt in particular.
- this catalyst may contain phosphorus.
- the first step generally takes place at a temperature of 350-460 ° C, preferably 360-450 ° C, a pressure greater than 2 Mpa, preferably greater than 5MPa, an hourly volume speed of 0.1-5h ⁇ l and preferably 0.2-2h " l and with a quantity of hydrogen at least 100N1 / X1 charge, and preferably 260-3000N1 / 1 charge.
- the temperatures are generally greater than or equal to 230 ° C and often between 300 ° C and 430 ° C.
- the pressure is generally greater than 2 MPa and preferably greater than 5 MPa.
- the quantity of hydrogen is at least 1001/1 of charge and often between 200 and 30001/1 of hydrogen per liter of charge.
- the hourly volume speed is generally between 0.15 and 10h ⁇ -L
- hydrocracking modes can be used.
- a first hydrocracking mode the pressure is moderate.
- the catalyst according to the invention is then used at a temperature generally greater than or equal to 230 ° C or at 300 ° C, generally at most 480 ° C, and often between 350 ° C and 450 ° C.
- the pressure is generally greater than 2 MPa and less than or equal to 12 MPa.
- a moderate pressure range is particularly interesting, which is 7.5-11 MPa, preferably 7.5-10 MPa or even 8-11 MPa and advantageously 8.5-10 MPa.
- the quantity of hydrogen is at least 100 normal liters of hydrogen per liter of charge and often between 200 and 3000 normal liters of hydrogen per liter of charge.
- the hourly volume speed is generally between 0.1 and 10h ⁇ -L
- the catalyst of the present invention can be used for hydrocracking under conditions of high hydrogen pressure of at least 8.5 MPa, preferably at least 9 MPa or at least 10 MPa.
- the treated sections are for example of vacuum distillates type highly charged with sulfur and nitrogen which have been hydrotreated beforehand.
- the petroleum cut conversion process takes place in two stages, the catalyst according to the invention being used in the second stage.
- the temperatures are generally greater than or equal to 230 ° C and often between 300 ° C and 430 ° C.
- the pressure is generally greater than 8.5 MPa and preferably greater than 10 MPa.
- the quantity of hydrogen is at least 1001/1 of charge and often between 200 and 30001/1 of hydrogen per liter of charge.
- the hourly volume speed is generally between 0.15 and 10 h ⁇ l.
- the catalysts of the present invention exhibit better conversion activity and better selectivity for middle distillates than commercial catalysts.
- the catalyst according to the invention can also be used for hydrorefining (HDS, HDN and hydrogenation in particular " ).
- the temperature is generally higher than 200 ° C. and often between 280 ° C. and 480 ° C.
- the pressure is generally greater than 0, lMPa and often greater than IMPa.
- the presence of hydrogen is generally necessary with a hydrogen recycling rate generally of at least 80 and often between 100 and 4000 liters of hydrogen per liter of charge.
- the hourly volume speed is generally between 0.1 and 20h-l
- Example 1 Manufacturing of a non-conforming catalyst A
- Catalyst A is produced as follows: 20% by weight of a zeolite is used
- Y of crystalline parameter equal to 2.429 nm and overall Si / Al atomic ratio of 13.6 and with an atomic Si / Al ratio of 19, which is mixed with 80% by weight of SB3 type alumma supplied by the company Condisputeda.
- the kneaded dough is then extruded through a die with a diameter of 1.4 mm.
- the extrudates are then dried overnight at 120 ° C in air and then calcined at 550 ° C in air.
- the extrudates are impregnated to dryness, that is to say by filling the pore volume with an aqueous solution of a mixture of ammonium heptamolybdate, nickel nitrate and orthophospho ⁇ que acid, so as to deposit 2.2% by weight nickel oxide NiO, 12.3% by weight of molybdenum oxide M0O3, 4.4% by weight of phosphorus oxide P2O5 dried overnight at 120 ° C in air and finally calm in air at 550 ° C .
- the final catalyst contains amsi 16.2% by weight of zeolite Y.
- Example 2 Manufacturing of a non-conforming catalyst B
- Catalyst B is produced in the following manner: 70% by weight of a Y zeolite with a crystalline parameter equal to 2.429 nm and an overall Si / Al atomic ratio of 13.6 and an Si / Al atomic framework ratio of 19 is used, that is mixed with 30% by weight of SB3 type alum supplied by the company Condisputeda.
- the kneaded dough is then extruded through a die with a diameter of 1.4 mm.
- the extrudates are then dried overnight at 120 ° C in air and then calcmated at 550 ° C in air.
- the extrudates are impregnated to dryness, that is to say by filling the pore volume with an aqueous solution of a mixture of ammonium heptamolybdate, nickel nitrate and orthophospho ⁇ que acid, so as to deposit 1.5? ⁇ by weight of nickel oxide NiO, 7.3% by weight of molybdenum oxide M0O3 and 2.5% by weight of phosphorus oxide P205.
- the wet extrudates were dried overnight at 120 ° C under air and lastly calcmés in air at 550 C C.
- the fmal catalyst contains 62.1% by weight of zeolite Y.
- Example 3 Manufacture of Compliant Catalysts C and D
- Catalysts C and D are produced in the following manner: firstly a Y zeolite powder with a crystalline parameter equal to 2.429 nm and an overall Si / Ai atomic ratio of 13 is prepared, 6 and a Si / Ai atomic framework ratio of 19, which is impregnated with an aqueous solution of niobium oxalate so as to deposit 1.4% by weight of Nb Os relative to the zeolite. Without prior drying, it is calcined at 500 ° C. for 2 hours under dry air.
- catalyst C 20% by weight of the niobium-impregnated zeolite prepared above is used, which is mixed with 80% by weight of SB3-type alumma supplied by the company Condisputeda.
- the kneaded paste is then extruded through a 1.4 mm diameter die.
- the extrudates are then dried overnight at 120 ° C in air and then calcmated at 550 ° C in air.
- the extrudates are impregnated to dryness, that is to say by filling the pore volume with an aqueous solution of a mixture of ammonium heptamolybdate, nickel nitrate and orthophospho ⁇ que acid, dried overnight at 120 ° C.
- the composition of the impregnation solution is calculated so as to obtain on the final catalyst 2.37% by weight of nickel oxide NiO, 12.03% by weight of molybdenum oxide Mo ⁇ 3, 4.8% by weight of phosphorus oxide P2O5.
- the catalyst therefore also contains 0.3% by weight of niobium oxide Nb2 ⁇ 5 and 15.6% by weight of zeolite Y.
- catalyst D an amount of 70% by weight of the niobium-impregnated zeolite prepared above is used, with 30% by weight of SB3 type alumina supplied by the company Condisputeda.
- the kneaded dough is then extruded through a die with a diameter of 1.4 mm.
- the extrudates are then dried overnight at 120 ° C in air and then calcmated at 550 ° C in air.
- the extrudates are then impregnated to dryness, that is to say by filling with an aqueous solution of a mixture of heptamolybdate -ammonium, nickel nitrate and orthophosphonic acid, so as to deposit 1.5% by weight.
- the catalyst contains by weight of oxide: 1.5% by weight of nickel oxide NiO, 7.3% by weight of molybdenum oxide Mo ⁇ 3 / 0.8% by weight of niobium oxide Nb2 ⁇ 5, 2.5% by weight of phosphorus oxide P2O5
- the final catalyst contains 60% by weight of zeolite Y.
- Example 4 Analyzes of the Catalysts The two catalysts A and C containing only about 16% of zeolite were analyzed so as to demonstrate the presence or absence of niobium in the zeolite.
- the first method used is transmission electron microscopy equipped with an X energy dispersion spectrometer allowing the identification and quantification of the elements present in the crystals of the zeolite.
- JEOL 2010R URP equipped with an X TRACOR energy dispersion spectrometer itself equipped with a Z-MAX30 detector.
- the catalyst extrudates are finely ground in a mortar.
- the powder is mixed in resin to make ultra-thin cuts of thickness 700 A for the two catalysts.
- the cuts produced are collected on a Cu grid covered with a membrane C with holes serving as a support for the preparation. These preparations are dried under an IR lamp before being introduced into the transmission electron microscope where they will be subjected to a primary vacuum for a few minutes and then to a secondary vacuum during the entire observation.
- the electron microscope makes it possible to perfectly identify the crystals of zeolite with a size of about 0.4 micron dispersed in the alumina matrix. We then proceed to a certain number of local analyzes (from 15 to 20) carried out on various zones of matrix and on various crystals of zeolites with a probe beam of 0.1 micron in diameter. Quantitative signal processing provides the relative concentration in atomic% of the elements (excluding oxygen).
- Table 1 summarizes the results obtained for samples A and C described in the examples above.
- the catalyst A contains crystals of zeolite Y without molybdenum and without niobium.
- the amount of Ni detected is due to the imprecision of the measurement.
- this analysis technique makes it possible to detect without ambiguity the presence of niobium and the absence of molybdenum in the crystals of zeolite Y.
- the second technique used is the electronic microprobe. Some extrudates are coated with resin and then polished to their diameter and metallized with carbon. The sample is introduced into a JXM 880 apparatus in order to analyze the local composition of Al, Si, Mo, Nb and Ni in different pumps.
- niobium in the zeolite Y in the case of sample C, the following calculations are carried out. For each analysis point the concentration of oxide of Al, Si, Mo, Nb and Ni is measured From the concentration in Al and Si oxide and the atomic ratio of the zeolite, the mass ratio AI 2 O 3 / (Zeolite Y + AI2O3) is deduced at each point. We can then draw up a diagram linking the niobium concentration measured as a function of the mass ratio AI 2 O 3 / (Zeolite Y + AI2O3) For catalyst C, the measuring heads containing no zeolite and therefore for which AI2O3 / (Zeolite Y + must not contain niobium.
- the catalysts are used under the conditions of hydrocracking at moderate pressure on an oil charge, the main characteristics of which are as follows:
- the catalytic test unit includes two reactors in a fixed bed, with upward flow of charge ("up-flow"). 40 ml of catalyst are introduced into each of the reactors.
- the catalyst for the first hydrotreatment stage HTH548 sold by the company is introduced. Procatalvse comprising an element of group VI and an element of group VIII deposited on an alum.
- the hydrocracking catalyst (A, B, C or D) is introduced.
- the two catalysts undergo an rn-situ sulfurization step before reaction. Note that any rn-situ or ex-situ sulfurization method is suitable.
- the charge described above can be transformed.
- the total pressure is 8.5 MPa
- the hydrogen flow rate is 500 liters of gaseous hydrogen per liter of charge injected
- the hourly volume speed is 0.8 h " l.
- the two reactors operate at the same temperature .
- the catalytic performances are expressed by the gross conversion at 400 ° C (CB), by the gross selectivity (SB) and by the conversions in hydrodesulfurization (HDS) and in hydrodenitrogenation (HDN) These catalytic performances are measured on the catalyst after a stabilization period, generally at least 48 hours, has been observed.
- catalyst C Comparison of catalyst C with catalyst A containing the same amount of zeolite Y, oxide matrix, hydrogenating element and phosphorus, shows that the presence of a metal of group VB contained in the porous network of the zeolite gives more a better level of conversion of the 380 ° C fraction than catalyst A which does not contain any.
- the selectivity is of the same level while the activity in HDS and HDN is slightly increased.
- catalysts B and D containing a large amount of zeolite there is a very marked improvement in the conversion, the selectivity and the HDS and HDN activities when the metal of group VB is present in the porous network of the zeolite.
- catalysts C and D containing niobium in the porous network have the advantage of giving better performance in hydrotreatment (hydrodesulfurization and hydrodenitrogenation).
- Example 4 Comparison of the hydrocracking catalysts of a distill t under vacuum at higher pressure.
- the catalysts are used under the conditions of hydrocracking at high pressure (12 MPa) on an oil charge, the main characteristics of which are as follows: initial pump 277 ° C. pump 10% 381 ° C. pump 50% 482 ° C pump 90% 531 ° C pump final 545 ° C flow pump + 36 ° C density (20/4) 0.919
- the catalytic test unit comprises two reactors in fixed ht, with upward flow of the charge ("up-flow"). 40 ml of catalyst are introduced into each of the reactors.
- the catalyst "1" of the first hydrotreatment stage HR360 sold by the company Procatalyse is introduced, comprising an element from group VI and an element from group VIII deposited on alumina.
- the second reactor the one in which the charge passes last, the second stage catalyst “2” is introduced, that is to say the hydroconversion catalyst.
- the two catalysts undergo an rn-situ sulfurization step before reaction. Note that any m-situ or ex-situ sulfurization method is suitable.
- the total pressure is 12 MPa
- the hydrogen flow rate is 1000 liters of gaseous hydrogen per liter of charge injected
- the overall hourly volume speed is 0.9 h ⁇
- the temperature of the first reactor is 390 ° C.
- the catalytic performances are expressed by the temperature which makes it possible to reach a gross conversion level of 70% and by the gross selectivity. These catalytic performances are measured on the catalyst after a stabilization period, generally at least 48 hours, has been observed.
- the gross selectivity SB is taken equal to: minus
- reaction temperature of the second reactor containing the hydroconversion catalyst (A, B, C or D) is fixed so as to reach a gross conversion CB equal to 70% by weight.
- catalyst B containing a large amount of zeolite Y relative to catalyst A shows that by increasing the amount of zeolite the activity of the catalyst greatly increased by the temperature level required to obtain 70% conversion of the charge but leads to a very significant loss of selectivity.
- the presence of an element of group VB inside the porous network of the zeolite obtained with sample C and D shows that the very good level of selectivity of catalyst A is maintained.
- Sample D has on the other hand much better activity like sample B due to the presence of a high zeolite content. Adding a VB group metal at the sem of the porous network of the zeolite is therefore particularly advantageous for obtaining hydrocracking catalysts which are very active and very selective in middle distillates.
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- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9908177 | 1999-06-25 | ||
FR9908177A FR2795342B1 (fr) | 1999-06-25 | 1999-06-25 | Catalyseur contenant une zeolithe chargee en element du groupe vb et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarbonees |
PCT/FR2000/001732 WO2001000321A1 (fr) | 1999-06-25 | 2000-06-22 | Catalyseur contenant une zeolithe chargee en element du groupe vb et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarbonees |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1159066A1 true EP1159066A1 (fr) | 2001-12-05 |
Family
ID=9547327
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00945980A Ceased EP1159066A1 (fr) | 1999-06-25 | 2000-06-22 | Catalyseur contenant une zeolithe chargee en element du groupe vb et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarbonees |
Country Status (4)
Country | Link |
---|---|
US (1) | US6531051B1 (fr) |
EP (1) | EP1159066A1 (fr) |
FR (1) | FR2795342B1 (fr) |
WO (1) | WO2001000321A1 (fr) |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2795341B1 (fr) * | 1999-06-25 | 2001-08-17 | Inst Francais Du Petrole | Catalyseur contenant une zeolithe chargee en element des groupes vib et/ou viii et son utilisation en hydroraffinage et hydrocraquage de coupes hydrocarbonees |
ITMI20031360A1 (it) * | 2003-07-03 | 2005-01-04 | Enitecnologie Spa | Solido poroso amorfo cataliticamente attivo e processo per la sua preparazione. |
CN100360235C (zh) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | 含复合沸石的氧化铝载体及其制备方法 |
CN100360221C (zh) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | 一种含改性y沸石的氧化铝载体及其制备方法 |
WO2007031560A2 (fr) * | 2005-09-14 | 2007-03-22 | Shell Internationale Research Maatschappij B.V. | Catalyseur et procede d'hydrocraquage |
KR101767375B1 (ko) | 2009-04-21 | 2017-08-11 | 알베마를 유럽 에스피알엘 | 인 및 붕소를 함유하는 수소처리 촉매 |
CN104226297B (zh) * | 2013-06-13 | 2016-12-28 | 中国石油化工股份有限公司 | 一种重油加氢处理催化剂及其制备与应用 |
AU2016202495B2 (en) * | 2015-04-23 | 2020-05-21 | Reliance Industries Limited | Multi-metallic catalyst system and use of the same in preparing upgraded fuel from biomass |
KR101736197B1 (ko) * | 2015-10-07 | 2017-05-17 | 한국화학연구원 | 다환 방향족 탄화수소로부터 BTEX(벤젠(Benzene), 톨루엔(Toluene), 에틸벤젠(Ethylbenzene), 자일렌(Xylene)) 제조용 Beta 제올라이트 촉매 및 이의 제조방법 |
US10953396B2 (en) | 2019-07-03 | 2021-03-23 | Saudi Arabian Oil Company | Methods for producing mesoporous zeolite multifunctional catalysts for upgrading pyrolysis oil |
US11130119B2 (en) | 2019-07-03 | 2021-09-28 | Saudi Arabian Oil Company | Methods for producing multifunctional catalysts for upgrading pyrolysis oil |
US11384297B1 (en) | 2021-02-04 | 2022-07-12 | Saudi Arabian Oil Company | Systems and methods for upgrading pyrolysis oil to light aromatics over mixed metal oxide catalysts |
US11746299B1 (en) | 2022-07-11 | 2023-09-05 | Saudi Arabian Oil Company | Methods and systems for upgrading mixed pyrolysis oil to light aromatics over mixed metal oxide catalysts |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3853747A (en) * | 1967-09-20 | 1974-12-10 | Union Oil Co | Hydrocracking process |
US3875081A (en) * | 1969-10-24 | 1975-04-01 | Union Oil Co | Hydrocarbon conversion catalyst |
US3730878A (en) * | 1971-03-04 | 1973-05-01 | Universal Oil Prod Co | Hydrocarbon conversion catalyst |
US4297243A (en) * | 1979-10-02 | 1981-10-27 | Union Oil Company Of California | Molybdenum-exchanged crystalline aluminosilicate zeolite |
US4777157A (en) * | 1986-06-30 | 1988-10-11 | Union Oil Company Of California | Hydrocracking catalyst |
GB8814601D0 (en) * | 1988-06-20 | 1988-07-27 | Shell Int Research | Process for preparation of zeolitic catalysts |
US5393409A (en) * | 1993-03-08 | 1995-02-28 | Uop | Hydrocracking process using a controlled porosity catalyst |
JP2992971B2 (ja) * | 1994-09-01 | 1999-12-20 | 株式会社ジャパンエナジー | 水素化処理用触媒 |
DK0913195T3 (da) * | 1996-06-28 | 2003-11-24 | China Petrochemical Corp | Katalysator til hydrogenkrakning af en destillatolie og en produktionsmetode dertil |
FR2775200B1 (fr) * | 1998-02-20 | 2000-04-28 | Inst Francais Du Petrole | Catalyseur comprenant une zeolithe nu-88, un element du groupe vb et son utilisation en hydroconversion de charges petrolieres hydrocarbonees |
FR2779072B1 (fr) * | 1998-05-28 | 2000-07-13 | Inst Francais Du Petrole | Catalyseur comprenant une zeolithe choisie dans le groupe forme par les zeolithes nu-85, nu-86 et nu-87, un element du groupe vb et son utilisation en hydroconversion de charges petrolieres hydrocarbonees |
FR2780311B1 (fr) * | 1998-06-25 | 2000-08-11 | Inst Francais Du Petrole | Catalyseur d'hydrocraquage comprenant une zeolithe y non globalement desaluminee, un element du groupe vb, et un element promoteur choisi dans le groupe forme par le bore, le phosphore et le silicium |
-
1999
- 1999-06-25 FR FR9908177A patent/FR2795342B1/fr not_active Expired - Lifetime
-
2000
- 2000-06-22 WO PCT/FR2000/001732 patent/WO2001000321A1/fr active Application Filing
- 2000-06-22 EP EP00945980A patent/EP1159066A1/fr not_active Ceased
- 2000-06-26 US US09/603,837 patent/US6531051B1/en not_active Expired - Lifetime
Non-Patent Citations (1)
Title |
---|
See references of WO0100321A1 * |
Also Published As
Publication number | Publication date |
---|---|
FR2795342A1 (fr) | 2000-12-29 |
WO2001000321A1 (fr) | 2001-01-04 |
US6531051B1 (en) | 2003-03-11 |
FR2795342B1 (fr) | 2001-08-17 |
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