Methods of producing crude product

FIELD: physics.

SUBSTANCE: invention relates to a method of producing crude material. When crude material is brought into contact with one or more catalyst, a total product is obtained, which contains a crude product. Crude material has residue content of at least 0.2 grams per 1 gram of crude material. The crude product is a liquid mixture at 25C and 0.101 MPa. One or more properties of this crude product can be altered at least 10% from corresponding properties of the crude material. In some versions of the invention, gas is obtained after bringing crude material with one or more catalysts. These methods allow for obtaining crude material with improved characteristics.

EFFECT: invention also relates to a crude product or a mixture or a method of producing transport fuel.

22 cl, 27 ex, 4 tbl, 12 dwg

 

The text descriptions are given in facsimile form.

1. The way to obtain the crude product formed in the process of refining, which is bringing into contact of the crude feedstock with a hydrogen source in the presence of an inorganic salt catalyst to obtain the total product that includes the crude product that is a liquid mixture at 25C and 0,101 MPa, and the crude raw material has a content of rest of at least 0.2 grams of residue per 1 g of the crude raw materials; inorganic salt catalyst includes alkali metal salts, in which at least one of alkali metal salts is a carbonate of an alkali metal, and alkaline the metal has an atomic number of at least 11 and atomic ratio of at least one of the alkali metals having an atomic number of at least 11, alkali metal having an atomic number greater than 11 is in a range from 0.1 to 10; and regulate the contact conditions such that the crude product has a content of the residue, expressed in grams of residue per 1 g of the crude product, less than 30% of the residue content in the crude raw material, where the concentration of the residue is determined by the ASTM D5307.

2. The method according to claim 1, in which at least part of the total product formed as a vapor, moreover, at least part of the vapor condenses at 25C and 0,101 MPa with the formation of the crude product.

3. The way to obtain the crude product, which is bringing into contact of the crude feedstock with a hydrogen source in the presence of an inorganic salt catalyst to obtain the total product, and the crude raw material has a content of rest of at least 0.2 grams of residue per 1 g of the crude raw materials; inorganic salt catalyst includes alkali metal salts, in which at least one of alkali metal salts is an alkali metal hydride, and alkali metal has an atomic number of at least 11 and atomic ratio of at least one of the alkali metals having atomic number of at least 11, alkali metal having an atomic number greater than 11 is in a range from 0.1 to 10; receive at least a portion of the total product in the form of vapor; condense at least part of the vapor at 25C and 0,101 MPa; and formed a crude product, which has a content of the residue is less than 30% of the residue content for raw materials.

4. The method according to claim 1 or 3, wherein the atomic ratio of an alkali metal having an atomic number of at least 11, alkali metal having an atomic number greater than 11 is in the range of the t is 0.1 to 4.

5. The method according to claim 1 or 3, wherein at least one alkali metal is potassium.

6. The method according to claim 1 or 3, wherein the alkali metals are potassium, cesium, rubidium or mixtures thereof.

7. The method according to claim 1 or 3, wherein at least two alkali metal are potassium and rubidium, and the atomic ratio of potassium to rubidium is in the range from 0.1 to 5; at least two alkali metal are potassium and cesium, and the atomic ratio of potassium to cesium is in the range from 0.1 to 5; at least three of the alkali metal are potassium, cesium, rubidium, and each of the atomic relations of potassium to cesium, potassium to rubidium, and cesium to the rubidium is in the range from 0.1 to 5.

8. The way to obtain the crude product, which is bringing into contact of the crude feedstock with a hydrogen source in the presence of an inorganic salt catalyst to obtain the total product that includes the crude product, which is a liquid mixture at 25C and 0,101 MPa, and the crude raw material has a content of rest of at least 0.2 grams of residue per 1 g of the crude raw materials; inorganic salt catalyst contains salts of alkali metals, salts of alkaline earth metals, or mixtures thereof;
regulate contact conditions such that the crude is, the product has a content of the residue is less than 30% of the residue content in the raw raw where the content of the residue is determined by the ASTM D5307; and
heat the mixture of residual raw materials and waste inorganic salt catalyst to a temperature of at least 800C in the presence of a reactive gas, to receive a gas flow and/or liquid flow, which is more of the crude product from a mixture of residual raw materials and waste inorganic salt catalyst.

9. The method according to claim 8, in which the reactive gas contains hydrogen, water vapor, nitrogen, carbon dioxide, light hydrocarbons, or mixtures thereof.

10. The method according to claim 8 or 9, in which the gas flow is from 0.2 to 0.99 mol of hydrogen and/or carbon dioxide on 1 mol of the reactive gas and liquid flow has more than 0.9 grams, or more than 0,99 g water per 1 g of liquid.

11. The method according to any one of claims 1 to 3 and 8-9, in which the inorganic salt catalyst additionally contains an alkaline earth metal.

12. The method according to any one of claims 1 to 3 and 8-9, in which the hydrogen source is a hydrogen, light hydrocarbons, water, or mixtures thereof.

13. The method according to any one of claims 1 to 3 and 8-9, in which the contact conditions govern in such a way that during the contacting 1 g of the crude feedstock is formed less than 0.2 g, at most 0.15 grams less than 0.1 g, or less than 0.05 grams of hydrocarbons that condensateurs at 25C and 0,101 MPa, that is determined by material balance.

14. The method according to any one of claims 1 to 3 and 8-9, in which the crude product is from 0.00001 to 0.03 g or from 0.0001 to 0.01 grams of coke per 1 g of the crude product.

15. The method according to any one of claims 1 to 3 and 8-9, in which the crude feedstock has a total acid number (SCC), the total content of Ni/V/Fe, the total content of heteroatoms, expressed in grams of Ni/V/Fe, or grams of heteroatoms per 1 g of the raw material, and the contact conditions are adjusted in such a way that the crude product has SCC, the total content of Ni/V/Fe, and/or the total content of heteroatoms at most 90% of the values SKC, a total Ni/V/Fe, and/or the total content heteroatoms in the untreated raw material.

16. The method according to any one of claims 1 to 3 and 8-9, in which the crude product also has 1 g of the crude product from 0.00001 to 0.2 g of naphtha from 0.0001 to 0.9 g of distillate, from 0.0001 to 0.99 grams of vacuum gas oil or mixtures thereof.

17. The method according to any one of claims 1 to 3 and 8-9, in which the crude raw material is from 0.2 to 0.99 g, or from 0.3 to 0.8 g of residue per 1 g of the crude raw materials.

18. The method according to any one of claims 1 to 3 and 8-9, in which mix the crude product with raw materials, which are the same or different from the crude raw materials to produce a mixture.

19. The crude product or the mixture, which receive the method according to any one of claims 1 to 18.

20. The method of obtaining transport is private fuel boiler fuel, lubricants or chemicals, which includes processing of the crude product or the mixture according to claim 19.

21. The method according to claim 20, in which the processing includes a distillation of the crude product or mixture, to obtain one or more distillate fractions.

22. The method according to claim 20 or 21, in which processing is a Hydrotreating.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: description of the elongated mould particles is provided, the particles have two asperities which start from and end at the central position where it aligns the longitudinal axis of the particle, and the cross-section of the particle takes the space, that is surrounded by peripheral edge of six circles which are located around the central circle; each of the six circles contacts two adjacent circles, while two interlacing circles are located at the equal distance from them the central circle and can be connected to the central circle; at that, two circles adjacent to the interlacing circles (but not the common circle) contact the central circle, except for the space taken by four remained external circles, and four remained interstitial areas; the elongated mould particles have complementary one to four asperities which are connected, preferably one or two, to the existing end asperity in a way specified above, and the complimentary asperity is specified as described above, while existing end asperity becomes a new central circle and the initial central circle becomes another asperity; also, the description is provided for the mould catalyst or its precursor for hydrocarbon synthesis by Fischer-Tropsch, mould carrier, method for producing the mould carrier, matrix disk, method for producing the hydrocarbons and method for producing the fuel and basic oil from hydrocarbons.

EFFECT: method for producing hydrocarbons is improved.

14 cl, 1 tbl, 2 dwg, 4 ex

FIELD: chemistry, organic, processing of hydrocarbons.

SUBSTANCE: invention is related to an improved method for hydroprocessing of hydrocarbon raw stock containing sulphur- and/or nitrogen-bearing contaminants. The method comprises the first contact interaction of hydrocarbon raw stock with hydrogen in the presence of at least one first catalyst based on VIII group metals on an acidic carrier, the carrier being selected from the group of zeolites and zeolite-bearing carriers, and then the flow leaving the first catalyst directly contacts hydrogen in the presence of at least one second catalyst based on a VIII group metal on a less acidic solid carrier, said solid carrier being selected from the group of carriers based on silicon dioxide-aluminium oxide and other solid carriers that are not zeolites. Said combination of two catalyst layers allows processing of raw stock with a high content of contaminating impurities without high-level cracking that involves the use of highly acidic carriers.

EFFECT: processing of hydrocarbon raw stock with contaminating impurities without high-level cracking.

14 cl, 1 ex

FIELD: petroleum processing.

SUBSTANCE: catalyst is characterized by that content of rare-earth elements in crystalline lattice of Y-zeolite, based on RE2O3, is 4 to 15 wt %, initial size of elementary cell is 2.450 to 2.458 nm, and size of equilibrium structure of elementary cell after its treatment with 100% steam at 800°C for 17 h exceeds 2.430 nm. Also described is a method for preparation of above catalyst for hydrocarbon cracking comprising (1) drying Y-zeolite with rare-earth element ions to water level below 10%, then, at a weight ratio SiCl4/Y-zeolite, interacting zeolite with gaseous SiCl4 supplied with dry air at 150-600°C for a period of time from 5 min to 2 h after reaction followed by removing residual soluble by-products in zeolite by washing with decationized water; (2) mixing and suspending 10-50% Y-zeolite with rare-earth element ions prepared in step (1), 10-60% binder, and 2-75% clay followed by forming catalyst by spray drying and using it.

EFFECT: increased catalytic activity, hydrothermal stability, degree of heavy oil conversion, and selectivity with respect to gasoline, dry gas, and coke, and considerably reduced content of olefin in produced gasoline.

33 cl, 3 dwg, 17 tbl, 36 ex

FIELD: petroleum processing.

SUBSTANCE: invention relates to technologies of obtaining feedstock sources such as crude oil, high-boiling petroleum fractions, petroleum residues, coal liquefaction and by-product-cock plant products, spent lubricating oils, household and industrial wastes of various hydrocarbon fuels, and hydrocarbon raw materials for basic and petrochemical synthesis. Method according to invention comprises: provision and/or synthesis hydrogen donors; hydrocarbon, hydrogen donor, and catalyst stirring step; separation of resulting mixture; isolation of light and heavy fractions; and recycling of heavy fraction together with catalyst to mixing step and hydrogenation of light fraction followed by recovering synthesized hydrogen donors, which are also directed to mixing step.

EFFECT: enhanced process efficiency.

9 cl, 1 dwg, 4 ex

FIELD: petroleum processing.

SUBSTANCE: petroleum feedstock hydrocracking catalyst is prepared by compounding zeolite Y with aluminonickel(cobalt)-molybdenum(tungsten) oxide system. Specifically, low-alkalinity zeolite Y having silicate modulus 5.5-7.0 and crystallinity at least 70% is mixed with aluminum hydroxide having pseudoboehmite structure in proportion (1-9):1. Thus obtained mix is molded, dried, and calcined under water steam atmosphere to give molded thermally treated zeolite. The latter is impregnated with aqueous Ni(Co) and Mo(W) salt solutions or ground and compounded with aluminonickel(cobalt)-molybdenum(tungsten) oxide system by mixing with aluminum hydroxide and Ni(Co) and Mo(W) salts, after which follow molding and impregnation with aqueous Ni(Co) and Mo(W) salt solutions.

EFFECT: expanded catalyst preparation possibilities.

2 cl, 5 tbl, 4 ex

FIELD: petrochemical processes.

SUBSTANCE: group of inventions relates to processing of hydrocarbon feedstock having dry point from 140 to 400°C and is intended for production of fuel fractions (gasoline, kerosene, and/or diesel) on solid catalysts. In first embodiment of invention, processing involves bringing feedstock into contact with regenerable catalyst at 250-500°C, pressure 0.1-4 MPa, and feedstock weight supply rate up to 10 h-1, said catalyst containing (i) crystalline silicate or ZSM-5 or ZSM-14-type zeolite having general empiric formula: (0.02-0.35)Na2O-E2O3-(27-300)SiO2-kH2O), where E represents at least one element from the series: Al, Ga, B, and Fe and k is coefficient corresponding to water capacity; or (ii) silicate or identically composed zeolite and at least one group I-VIII element and/or compound thereof in amount 0.001 to 10.0 % by weight. Reaction product is separated after cooling through simple separation and/or rectification into fractions: hydrocarbon gas, gasoline, kerosene, and/or diesel fractions, after which catalyst is regenerated by oxygen-containing gas at 350-600°C and pressure 0.1-4 MPa. Hydrocarbon feedstock utilized comprises (i) long hydrocarbon fraction boiling away up to 400°C and composed, in particular, of isoparaffins and naphtenes in summary amount 54-58.1%, aromatic hydrocarbons in amount 8.4-12.7%, and n-paraffins in balancing amount; or (ii) long hydrocarbon fraction boiling away up to 400°C and composed, in particular, of following fractions, °C: 43-195, 151-267, 130-364, 168-345, 26-264, 144-272. In second embodiment, feedstock boiling away up to 400°C is processed in presence of hydrogen at H2/hydrocarbons molar ratio between 0.1 and 10 by bringing feedstock into contact with regenerable catalyst at 250-500°C, elevated pressure, and feedstock weight supply rate up to 10 h-1, said catalyst containing zeolite having structure ZSM-12, and/or beta, and/or omega, and/or zeolite L. and/or mordenite, and/or crystalline elemento-aluminophosphate and at least one group I-VIII element and/or compound thereof in amount 0.05 to 20.0 % by weight. Again, reaction product is separated after cooling through simple separation and/or rectification into fractions: hydrocarbon gas, gasoline, kerosene, and/or diesel fractions, after which catalyst is regenerated by oxygen-containing gas at 350-600°C and pressure 0.1-6 MPa.

EFFECT: improved flexibility of process and enlarged assortment of raw materials and target products.

12 cl, 3 tbl, 22 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalyst (water-soluble silicon compound) solution is added to hydrocarbons, which are then subjected to cracking in presence of hydrogen at temperature and overpressure providing explosive transfer of catalyst solution into vapor phase. Motor fuel components are predominantly obtained. Yearly processing of 0.5 to 1.0 million ton petroleum is thus envisaged.

EFFECT: simplified process, increased yield of commercial products, and enabled creation of mediate-scale cracking plants.

5 cl, 2 tbl, 3 ex

FIELD: petroleum processing.

SUBSTANCE: at least part of heavy feed is supplied to deasphalting section in presence of hydrocarbon solvents to form two streams, of which one stream is composed of deasphalted petroleum products and the other of asphalts. The latter is mixed with hydrogenation catalyst and optionally with the rest of heavy feed not directed to deasphalting section. Resulting mixture is fed to hydrofining reactor, to which also hydrogen or H2/H2S mixture is supplied. Stream containing hydrofining reaction product and dispersed catalyst is routed to one or more distillation or evaporation stages, by means of which most volatile fractions, including hydrofining gases, are separated. At least 60 wt % of bottom residue (goudron) or liquid leaving evaporation unit containing dispersed catalyst, sulfide-rich metals obtained in feed demetallization stage, and optionally coke is recycled to deasphalting zone.

EFFECT: simplified technology.

18 cl, 2 dwg, 4 tbl, 3 ex

FIELD: petroleum processing.

SUBSTANCE: blend composed of vacuum distillate and distilled fraction of secondary destruction processes is subjected to hydrogenation processing at elevated temperature and pressure in presence of catalyst, said secondary destruction process fraction containing sulfur up to 1% and being taken in amount 2 to 25% based on total weight of feedstock, while vacuum distillate boils up to 560°C. More particularly, secondary destruction process fraction is catalytic cracking, visbreaking, or retarded coking gas oil fraction. Process is carried out at 340-415°C, pressure 4-10 MPa, and feedstock supply volume flow rate 0.5-2.0 h-1.

EFFECT: improved purification degree of residue and enabled involvement of heavy vacuum distillate.

2 cl, 3 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: to crude oil with 2-10% water content is added catalyst followed by activation of hydrogen donors and hydrogenation of crude oil. Catalyst is used in the form of water-soluble group VI and VIII element compounds, which dissolves in water contained in crude oil to form true solution. Hydrogen donors are own crude oil fractions and products obtained from own crude oil fractions.

EFFECT: simplified and deepened oil processing.

10 cl, 1 dwg, 1 tbl

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: to crude oil with 2-10% water content is added catalyst followed by activation of hydrogen donors and hydrogenation of crude oil. Catalyst is used in the form of water-soluble group VI and VIII element compounds, which dissolves in water contained in crude oil to form true solution. Hydrogen donors are own crude oil fractions and products obtained from own crude oil fractions.

EFFECT: simplified and deepened oil processing.

10 cl, 1 dwg, 1 tbl

FIELD: petroleum processing.

SUBSTANCE: blend composed of vacuum distillate and distilled fraction of secondary destruction processes is subjected to hydrogenation processing at elevated temperature and pressure in presence of catalyst, said secondary destruction process fraction containing sulfur up to 1% and being taken in amount 2 to 25% based on total weight of feedstock, while vacuum distillate boils up to 560°C. More particularly, secondary destruction process fraction is catalytic cracking, visbreaking, or retarded coking gas oil fraction. Process is carried out at 340-415°C, pressure 4-10 MPa, and feedstock supply volume flow rate 0.5-2.0 h-1.

EFFECT: improved purification degree of residue and enabled involvement of heavy vacuum distillate.

2 cl, 3 ex

FIELD: petroleum processing.

SUBSTANCE: at least part of heavy feed is supplied to deasphalting section in presence of hydrocarbon solvents to form two streams, of which one stream is composed of deasphalted petroleum products and the other of asphalts. The latter is mixed with hydrogenation catalyst and optionally with the rest of heavy feed not directed to deasphalting section. Resulting mixture is fed to hydrofining reactor, to which also hydrogen or H2/H2S mixture is supplied. Stream containing hydrofining reaction product and dispersed catalyst is routed to one or more distillation or evaporation stages, by means of which most volatile fractions, including hydrofining gases, are separated. At least 60 wt % of bottom residue (goudron) or liquid leaving evaporation unit containing dispersed catalyst, sulfide-rich metals obtained in feed demetallization stage, and optionally coke is recycled to deasphalting zone.

EFFECT: simplified technology.

18 cl, 2 dwg, 4 tbl, 3 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalyst (water-soluble silicon compound) solution is added to hydrocarbons, which are then subjected to cracking in presence of hydrogen at temperature and overpressure providing explosive transfer of catalyst solution into vapor phase. Motor fuel components are predominantly obtained. Yearly processing of 0.5 to 1.0 million ton petroleum is thus envisaged.

EFFECT: simplified process, increased yield of commercial products, and enabled creation of mediate-scale cracking plants.

5 cl, 2 tbl, 3 ex

FIELD: petrochemical processes.

SUBSTANCE: group of inventions relates to processing of hydrocarbon feedstock having dry point from 140 to 400°C and is intended for production of fuel fractions (gasoline, kerosene, and/or diesel) on solid catalysts. In first embodiment of invention, processing involves bringing feedstock into contact with regenerable catalyst at 250-500°C, pressure 0.1-4 MPa, and feedstock weight supply rate up to 10 h-1, said catalyst containing (i) crystalline silicate or ZSM-5 or ZSM-14-type zeolite having general empiric formula: (0.02-0.35)Na2O-E2O3-(27-300)SiO2-kH2O), where E represents at least one element from the series: Al, Ga, B, and Fe and k is coefficient corresponding to water capacity; or (ii) silicate or identically composed zeolite and at least one group I-VIII element and/or compound thereof in amount 0.001 to 10.0 % by weight. Reaction product is separated after cooling through simple separation and/or rectification into fractions: hydrocarbon gas, gasoline, kerosene, and/or diesel fractions, after which catalyst is regenerated by oxygen-containing gas at 350-600°C and pressure 0.1-4 MPa. Hydrocarbon feedstock utilized comprises (i) long hydrocarbon fraction boiling away up to 400°C and composed, in particular, of isoparaffins and naphtenes in summary amount 54-58.1%, aromatic hydrocarbons in amount 8.4-12.7%, and n-paraffins in balancing amount; or (ii) long hydrocarbon fraction boiling away up to 400°C and composed, in particular, of following fractions, °C: 43-195, 151-267, 130-364, 168-345, 26-264, 144-272. In second embodiment, feedstock boiling away up to 400°C is processed in presence of hydrogen at H2/hydrocarbons molar ratio between 0.1 and 10 by bringing feedstock into contact with regenerable catalyst at 250-500°C, elevated pressure, and feedstock weight supply rate up to 10 h-1, said catalyst containing zeolite having structure ZSM-12, and/or beta, and/or omega, and/or zeolite L. and/or mordenite, and/or crystalline elemento-aluminophosphate and at least one group I-VIII element and/or compound thereof in amount 0.05 to 20.0 % by weight. Again, reaction product is separated after cooling through simple separation and/or rectification into fractions: hydrocarbon gas, gasoline, kerosene, and/or diesel fractions, after which catalyst is regenerated by oxygen-containing gas at 350-600°C and pressure 0.1-6 MPa.

EFFECT: improved flexibility of process and enlarged assortment of raw materials and target products.

12 cl, 3 tbl, 22 ex

FIELD: petroleum processing.

SUBSTANCE: petroleum feedstock hydrocracking catalyst is prepared by compounding zeolite Y with aluminonickel(cobalt)-molybdenum(tungsten) oxide system. Specifically, low-alkalinity zeolite Y having silicate modulus 5.5-7.0 and crystallinity at least 70% is mixed with aluminum hydroxide having pseudoboehmite structure in proportion (1-9):1. Thus obtained mix is molded, dried, and calcined under water steam atmosphere to give molded thermally treated zeolite. The latter is impregnated with aqueous Ni(Co) and Mo(W) salt solutions or ground and compounded with aluminonickel(cobalt)-molybdenum(tungsten) oxide system by mixing with aluminum hydroxide and Ni(Co) and Mo(W) salts, after which follow molding and impregnation with aqueous Ni(Co) and Mo(W) salt solutions.

EFFECT: expanded catalyst preparation possibilities.

2 cl, 5 tbl, 4 ex

FIELD: petroleum processing.

SUBSTANCE: invention relates to technologies of obtaining feedstock sources such as crude oil, high-boiling petroleum fractions, petroleum residues, coal liquefaction and by-product-cock plant products, spent lubricating oils, household and industrial wastes of various hydrocarbon fuels, and hydrocarbon raw materials for basic and petrochemical synthesis. Method according to invention comprises: provision and/or synthesis hydrogen donors; hydrocarbon, hydrogen donor, and catalyst stirring step; separation of resulting mixture; isolation of light and heavy fractions; and recycling of heavy fraction together with catalyst to mixing step and hydrogenation of light fraction followed by recovering synthesized hydrogen donors, which are also directed to mixing step.

EFFECT: enhanced process efficiency.

9 cl, 1 dwg, 4 ex

FIELD: petroleum processing.

SUBSTANCE: catalyst is characterized by that content of rare-earth elements in crystalline lattice of Y-zeolite, based on RE2O3, is 4 to 15 wt %, initial size of elementary cell is 2.450 to 2.458 nm, and size of equilibrium structure of elementary cell after its treatment with 100% steam at 800°C for 17 h exceeds 2.430 nm. Also described is a method for preparation of above catalyst for hydrocarbon cracking comprising (1) drying Y-zeolite with rare-earth element ions to water level below 10%, then, at a weight ratio SiCl4/Y-zeolite, interacting zeolite with gaseous SiCl4 supplied with dry air at 150-600°C for a period of time from 5 min to 2 h after reaction followed by removing residual soluble by-products in zeolite by washing with decationized water; (2) mixing and suspending 10-50% Y-zeolite with rare-earth element ions prepared in step (1), 10-60% binder, and 2-75% clay followed by forming catalyst by spray drying and using it.

EFFECT: increased catalytic activity, hydrothermal stability, degree of heavy oil conversion, and selectivity with respect to gasoline, dry gas, and coke, and considerably reduced content of olefin in produced gasoline.

33 cl, 3 dwg, 17 tbl, 36 ex

FIELD: chemistry, organic, processing of hydrocarbons.

SUBSTANCE: invention is related to an improved method for hydroprocessing of hydrocarbon raw stock containing sulphur- and/or nitrogen-bearing contaminants. The method comprises the first contact interaction of hydrocarbon raw stock with hydrogen in the presence of at least one first catalyst based on VIII group metals on an acidic carrier, the carrier being selected from the group of zeolites and zeolite-bearing carriers, and then the flow leaving the first catalyst directly contacts hydrogen in the presence of at least one second catalyst based on a VIII group metal on a less acidic solid carrier, said solid carrier being selected from the group of carriers based on silicon dioxide-aluminium oxide and other solid carriers that are not zeolites. Said combination of two catalyst layers allows processing of raw stock with a high content of contaminating impurities without high-level cracking that involves the use of highly acidic carriers.

EFFECT: processing of hydrocarbon raw stock with contaminating impurities without high-level cracking.

14 cl, 1 ex

FIELD: chemistry.

SUBSTANCE: description of the elongated mould particles is provided, the particles have two asperities which start from and end at the central position where it aligns the longitudinal axis of the particle, and the cross-section of the particle takes the space, that is surrounded by peripheral edge of six circles which are located around the central circle; each of the six circles contacts two adjacent circles, while two interlacing circles are located at the equal distance from them the central circle and can be connected to the central circle; at that, two circles adjacent to the interlacing circles (but not the common circle) contact the central circle, except for the space taken by four remained external circles, and four remained interstitial areas; the elongated mould particles have complementary one to four asperities which are connected, preferably one or two, to the existing end asperity in a way specified above, and the complimentary asperity is specified as described above, while existing end asperity becomes a new central circle and the initial central circle becomes another asperity; also, the description is provided for the mould catalyst or its precursor for hydrocarbon synthesis by Fischer-Tropsch, mould carrier, method for producing the mould carrier, matrix disk, method for producing the hydrocarbons and method for producing the fuel and basic oil from hydrocarbons.

EFFECT: method for producing hydrocarbons is improved.

14 cl, 1 tbl, 2 dwg, 4 ex

Up!