3233; wherein a support simultaneously contains two Y-zeolites with different acid site densities and distributions of aluminium between the surface and the volume of the crystals; as a first zeolite, the carrier contains a Y-zeolite with a higher acid site density and a ratio of the surface-to-volume concentration of silicon to aluminium that is Si/Al=1.2-2.1; as a second zeolite, the carrier contains a Y-zeolite with a lower acid site density and a ratio of the surface-to-volume concentration of silicon to aluminium that is Si/Al=0.7-0.9. The technical result is a nickel-tungsten hydrocracking catalyst that has high activity. This is achieved by solving the problem of providing a catalyst with optimal acid characteristics for hydrocracking hydrocarbon feedstock and obtaining a high yield of kerosene and diesel oil cuts.
The invention relates to the field of oil-refining, and more particularly to catalysts for obtaining light olefins. The proposed catalyst for joint cracking of oil fractions includes zeolite ZSM-5, ultra-stable zeolite HREY and a matrix comprising amorphous aluminosilicate, aluminum oxide and bentonite clay, and is characterized in that the zeolite ZSM-5 has a Si/Al ratio of 30 to 80 and contains 2.0 to 4.0 wt% of phosphorus, the catalyst containing the following relative amounts of components, in wt%: 8-20 phosphorus-modified zeolite ZSM-5; 15-25 ultra-stable zeolite HREY; 15-30 aluminum oxide; 15-30 bentonite clay; and 16-30 amorphous aluminosilicate. Mixtures of non-hydrotreated vacuum gas oil with the following gasoline fractions are used as the oil fractions: straight-run gasoline fraction 62-85C, a fraction with a boiling point of 70C, gasoline refined oil, a mixture of the specified fractions. The technical result is that of obtaining a highly active catalyst for joint cracking of oil fractions which provides high yields of light olefin hydrocarbons.
The invention relates to the field of oil-refining, and more particularly to catalysts for obtaining light olefins. The proposed catalyst for cracking oil fractions includes phosphorus-modified zeolite ZSM-5 and a matrix, and is characterized in that the zeolite ZSM-5 has a Si/Al ratio of 40 to 150 and contains 1.0 to 4.0 wt% of phosphorus, and the matrix components used are aluminum oxide and bentonite clay, or aluminum oxide, bentonite clay and amorphous aluminosilicate, the catalyst containing the following relative amounts of components, in wt. %: 40-50 phosphorus-modified zeolite ZSM-5; 15-25 aluminum oxide; 20-35 bentonite clay; and 0-10 amorphous aluminosilicate. The following are used as oil fractions: straight-run gasoline fraction 62-85C, a fraction with a boiling point of 70C, gasoline refined oil, a mixture of the specified fractions. The technical result is that of obtaining a highly active catalyst for cracking oil fractions which provides greater yield of light olefins.
OBSCHESTVO S OGRANICHENNOI OTVETSTVENNOSTYU "NOVIE GAZOVIE TEHNOLOGII-SINTEZ" (OOO "NGT-SINTEZ") (Russia)
Inventor
Bessonov, Aleksandr Anatolevich
Ivanov, Dmitrii Valerevich
Imsheneckii, Vladimir Vladislavovich
Lobichenko, Elena Nikolaevna
Abstract
The invention relates to heterogeneous catalytic reactors. The proposed reactor comprises: a cylindrical housing; a catalyst basket mounted coaxially with the housing and comprising side walls and a bottom wall; a removable cover having an inlet element disposed therein for supplying a reaction mixture; and a bottom having an outlet element disposed therein for removing reaction products. The upper part of the catalyst basket has an upper cylindrical ledge that projects in a direction from the axis toward the reactor housing; a connection between the reactor housing and the catalyst basket is configured to be detachable by means of mounting the upper cylindrical ledge of the basket in a cylindrical recess in the reactor housing; the side walls of the catalyst basket are impermeable to reaction mixture and reaction products, and the lower wall of the basket is permeable to reaction mixture and reaction products; in the lower part of the catalyst basket there is a lower cylindrical ledge that projects in a direction from the axis toward the reactor housing; between the reactor housing and the side walls of the basket there is a gas gap that is delimited from above by the upper cylindrical ledge of the basket and is partially delimited from below by the lower cylindrical ledge of the basket.
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
B01J 19/24 - Stationary reactors without moving elements inside
5.
GUARD BED CATALYST FOR HYDROTREATMENT OF SILICON-CONTAINING HYDROCARBON FEEDSTOCK
6618436233. The catalyst has a specific surface area of 245-275 m2/g, a pore volume of 0.50-0.55 cm336233. The technical result is an increase in the rate of silicon extraction from feedstock, increased silicon dioxide capacity of the catalyst, and increased resistance of the catalyst to deactivation under conditions of hydrocarbon feedstock hydrotreatment.
B01J 31/04 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
226572411657222252336233 - the remainder. The catalyst has a specific surface area in the range of 120-190 m2/g, a pore volume in the range of 0.35-0.65 cm3/g, an average pore diameter in the range of 7-12 nm, and is in the form of particles having a circular, trefoil or quatrefoil cross-sectional shape with a diameter of a circumscribed circle in the range of 1.0-1.6 mm and a length up to 20 mm. After the sulfidation according to known methods, the catalyst comprises, wt. %: Mo - 10.0-16.0; Co - 2.7-4.5; P - 0.8-1.8; S - 6.7-10.8; the carrier -the remainder. The technical result is the production of a catalyst having activity in desired reactions which take place during hydrotreatment of diesel fuel.
C10G 45/04 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
2224116572233, is the remainder; which catalyst has a specific surface area of 265 to 285 m2/g, pore volume of 0.70 to 0.72 cm3/g, an average pore diameter of 100 to 105, and which is in the form of granules with the cross section in the form of a circle with a diameter of 3±0.1 mm and a length of up to 20 mm. After the sulfidation according to generally known methods, the catalyst comprises, wt %: Mo - 1.99-2.98; Ni - 0.61-0.91; S - 1.66-2.48; the carrier is the remainder.
B01J 31/04 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
8.
CATALYST FOR HYDROCARBON FEEDSTOCK UPGRADING PROCESS AND METHOD FOR PRODUCING SAME
2xy241165724ab256572657232xy241165724ab2565722333233 – the remainder; wherein tungsten and molybdenum are comprised in the catalyst at the molar ratio W/(Mo+W) of 0.3 to 0.7.
B01J 31/34 - Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups of chromium, molybdenum or tungsten
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
22657241165723623366 having the norbergite structure is in the form of particles having a size of 10 to 200 nm, which are characterized by interplanar spacings of 3.2 and 2.8 Å, with an angle between them of 53.8°. The boron in the form of surface compounds is characterized by IR absorption bands of 930-1040, 1230, 1385-1450 and 3695 cm-1. The catalyst comprises strong Brønsted acid sites and moderate-strength Brønsted acid sites. After sulfidation, the catalyst comprises: 10.0-14.0 wt% Мо; 3.0-4.3wt% Со; 6.7-9.4 wt% S; 0.5-2.0 wt% boron in the form of surface compounds; and the remainder a support. The dispersity of the applied metals, as determined using X-ray photoelectron spectroscopy (XPS) data, for the IMo3d/IA12p intensity ratio lies in the range of 1.45-1.55, and for the 1Co2p/1A12p intensity ratio lies in the range of 1.14-1.18.
B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium
B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
11.
CATALYST FOR HYDROTREATMENT OF HYDROCRACKING FEEDSTOCKS
22241165723623366 with the norbergite structure is in the form of particles having the size of 10 to 200 nm, which are characterized by interplanar spacings of 3.2 and 2.8 Å, with an angle between them of 53.8°. Boron in the form of surface compounds is characterized by absorption bands of 930-1040, 1230, 1385-1450, and 3695 cm-1 in the IR spectra. Post-sulfidation, the catalyst comprises (wt%): Mo – 10.0-14.0; Ni – 3.0-4.3; S – 6.7-9.4; boron in the form of surface compounds – 0.5-2.0; and the substrate – the remainder; wherein the substrate comprises (wt %): aluminium borate Al3BO6 having the norbergite structure – 5.0-25.0; sodium – no more than 0.03; and γ-Al2O3 - the remainder.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
12.
A CATALYST FOR HYDROTREATMENT OF HYDROCRACKING FEEDSTOCKS
The invention relates to catalysts for preliminary hydrotreatment of oil fractions with an onset of boiling temperature above 360°C for producing feedstocks with a low sulfur content, which feedstocks are further processed by hydrocracking. A catalyst comprising (wt%): [Ni(H2O)2]2[Mo4O11(C6H5O7)2] - 29.0-36.0%; a substrate - the remainder, is described; wherein the substrate comprises (wt%): aluminium borate Al3BO6 having the norbergite structure – 5.0-25.0; sodium – no more than 0.03; γ-Al2O3 - the remainder. The aluminium borate Al3BO6 with the norbergite structure is in the form of particles having the size of 10 to 200 nm, which are characterized by interplanar spacings of 3.2 and 2.8 Å, with an angle between them of 53.8°. The catalyst has a specific surface area in the range of 130 to 180 m2/g, a pore volume in the range of 0.35 to 0.65 cm3/g, an average pore diameter in the range of 10 to 15 nm, and is in the form of particles having a circular, trefoil or quatrefoil cross-sectional shape with a diameter of a circumscribed circle in the range of 1.0-1.6 mm and a length up to 20 mm. Post-sulfidation, the catalyst comprises (wt%): Mo – 10.0-14.0; Ni – 3.0-4.3; S – 6.7-9.4; the substrate – the remainder; wherein the substrate comprises (wt%): aluminium borate Al3BO6having the norbergite structure – 5.0-25.0; sodium – no more than 0.03; γ-Al2O3 - the remainder. The technical result is the maximized activity of desulfurization and denitrogenation in the hydrotreatment of oil fractions with an onset of boiling temperature above 360°C for producing quality feedstocks for hydrocracking.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
The invention relates to catalysts for producing petroleum cuts having a low sulfur content. A catalyst comprising (wt %): [Co(H2O)2(C6H5O7)]2[Mo4O11(C6H5O7)2] 33.0-43.0%; a substrate is the remainder, is described; wherein the substrate comprises (wt%): aluminium borate Al3BO6 having the norbergite structure – 5.0-25.0; sodium – no more than 0.03; γ-Al2O3 - the remainder. The aluminium borate Al3BO6 with the norbergite structure comprised in the catalyst is in the form of particles having the size of 10 to 200 nm, which are characterized by interplanar spacings of 3.2 and 2.8 Å, with an angle between them of 53.8. The catalyst has a specific surface area in the range of 130 to 180 m2/g, a pore volume in the range of 0.35 to 0.65 cm3/g, an average pore diameter in the range of 7 to 12 nm, and is in the form of particles having a circular, trefoil or quatrefoil cross-sectional shape. After sulfidation according to known methods, the catalyst comprises (wt%): Mo – 10.0-14.0; Co – 3.0-4.3; S – 6.7-9.4; the substrate – the remainder. The technical result is the obtention of a catalyst having maximized activity in desired reactions which take place during hydrotreatment of hydrocarbon feedstocks.
B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
14.
METHOD FOR REGENERATING A SPENT HYDROTREATING CATALYST
The invention relates to a method for regenerating spent catalysts and to a method for hydrotreating a diesel fuel. The invention solves the problem of providing an effective method for regenerating catalysts. A method is described for regenerating a spent hydrotreating catalyst, according to which a spent catalyst is calcined in an airstream, or in a bed no higher than 30 mm, or in a rotary-drum furnace, while agitating the bed at a temperature of no more than 650°С, i.e. under conditions which allow a catalyst to be produced that has a pore volume of 0.3-0.8 ml/g, a specific surface area of 150-280 m2/g and an average pore diameter of 6-15 nm and that contains, in wt.%: 2.0-5.35 Со; 10.0-16.0 Мо; 0.2-0.8 S; no more than 0.2 С; which is then saturated with a solution of citric acid with a concentration in the range of 1.3-2.5 mol/litre in a mixture of water and butyl diglycol (10-20 wt. %), and heat-treated under conditions that allow production of a catalyst that contains, in wt.%: 5.1-18.0 Со(C6H6O7); 7.5-15.0 Н4[Мо4(C6H5O7)2O11]; 4.3-19.0 H3[Со(ОН)6Mo6O18]; 0.5-2.30 SO4 2-; with the remainder being a carrier. The technical result is that the invention allows the catalyst activity to be restored to 100% and higher.
The invention relates to methods for hydrotreating diesel fuels based on the use of regenerated hydrotreating catalysts. A method is described for hydrotreating a diesel fuel at a temperature of 340-390°С, a pressure of 3-9 MPa, a feedstock volumetric flow rate of 1.0-2.5 h-1, and a hydrogen/feedstock volumetric ratio of 300-600 m3/m3, in the presence of a regenerated catalyst that has a pore volume of 0.3-0.8 ml/g, a specific surface area of 150-280 m2/g, and an average pore diameter of 6-15 nm and that contains molybdenum, cobalt, sulphur and a carrier, the molybdenum and cobalt being present in the catalyst in the form of a mixture of complex compounds Со(С6Н6O7), Н4[Мо4(С6Н5O7)2O11], Н3[Со(ОН)6Мо6O18], and the sulphur being present in the form of a sulphate anion SO4 2-, in the following concentrations in wt.%: 5.1-18.0 Со(С6Н6O7); 7.5-15.0 Н4[Мо4(С6Н5O7)2O11]; 4.3-19.0 Н3[Со(ОН)6Мо6O18]; 0.5-2.30 SO4 2-; with the remainder being the carrier. The technical result is the production of a hydrotreated diesel fuel that has a sulphur content of no more than 10 ppm.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
The invention relates to regenerated hydrotreating catalysts intended for the production of low-sulphur diesel fuel. The invention solves the problem of providing an improved regenerated hydrotreating catalyst. A regenerated hydrotreating catalyst is described which has a pore volume of 0.3-0.8 ml/g, a specific surface area of 150-280 m2/g and an average pore diameter of 6-15 nm, and which contains molybdenum, cobalt, sulphur and a carrier, the molybdenum and cobalt being present in the catalyst in the form of a mixture of complex compounds Со(C6H6O7), Н4[Мо4(C6H5O7)2O11], H3[Со(ОН)6Mo6O18], and the sulphur being present in the form of a sulphate anion SO4 2-, in the following concentrations in wt.%: 5.1-18.0 Со(C6H6O7); 7.5-15.0 Н4[Мо4(C6H5O7)2O11]; 4.3-19.0 H3[Со(ОН)6Mo6O18]; 0.5-2.30 SO4 2-; with the remainder being the carrier, wherein cobalt citrates can be coordinated to molybdenum citrate Н4[Мо4(C6H5O7)2O11] and to 6-molybdocobaltate H3[Со(ОН)6Mo6O18]. The technical result is that the invention makes it possible to produce regenerated catalysts the activity of which, in the hydrotreatment of a diesel fuel, is more than or equal to 100% of the activity of fresh catalysts.
B01J 31/02 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
C10G 45/06 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
17.
METHOD FOR MANUFACTURING A CRACKING CATALYST WITH ALKALINE-EARTH ELEMENTS
The invention relates to the field of the petroleum refining and petrochemical industry, and more particularly to methods for manufacturing catalysts of the catalytic cracking of petroleum fractions. The invention solves the problem of producing an effective cracking catalyst. A method for manufacturing a cracking catalyst includes carrying out ion exchanges for cations of rare-earth elements and ammonium in NaY zeolite, two stages of ultrastabilization of the zeolite in an environment of water vapour, mixing the zeolite with a matrix comprised of bentonite clay, aluminium hydroxide and amorphous aluminium silicate, producing a composition, spray drying said composition, and subsequently calcining and producing a catalyst, wherein prior to the first stage of ultrastabilization, additional ion exchange of sodium cations in the zeolite for magnesium cations or calcium cations is carried out without intermediate filtration to produce Y zeolite, containing: not more than 0.6 mass% sodium oxide; 0.5-5.5 mass% rare earth element oxides; 0.5-4.0 mass% magnesium oxide; 1.0-7.0 mass% calcium oxide; wherein the catalyst contains 0.1-1.1 mass% rare earth element oxides; 0.23 mass% sodium oxide; 0.1-0.8 mass% magnesium oxide from the zeolite component or 0.2-1.4 mass% calcium oxide from the zeolite component.
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