Method for production hydrocarbon liquids with low content of aromatic compounds

Invention relates to a method of producing base oil, involving: providing a first catalyst containing at least one group VIII metal deposited on a M41S catalyst support, such as MCM-41, and having density of 600 kg/m³ or less; providing a second catalyst containing at least one group VIII metal, having dewaxing efficiency which is sufficient to facilitate treatment of a stream of light neutral (150 N) hydrocarbons from a medium-pressure hydrocracking apparatus, having kinematic viscosity at 100°C of less than 5 and end boiling point lower than 550°C, at 320°C and liquid hourly space velocity (LHSV) of 1 h^-1, to obtain base oil having chilling temperature lower than 15°C; bringing the material into contact with the first catalyst at adequate conditions for treating the material, wherein said adequate conditions are adequate for one of the processes selected from hydrotreatment, hydrofining or hydrogenation of aromatic compounds, and bringing the treated material into contact with the second catalyst at conditions adequate for dewaxing the treated material. The invention also relates to another method of producing base oil.

Invention refers to oil processing, notably to method of producing sweetened ecologically pure diesel fuel with ultra low contents of sulphur. The method of producing diesel fuel consists in the following: at the first stage oil virgin diesel fraction boiled out within ranges of 172-365°C or the said fraction in mixture with diesel fractions of secondary processes is subject to hydro-fining on catalyst containing (wt %): nickel oxide - 3.0-8.0; molybdenum oxide - 11.0-22.0; promoter - 0.2-4.0; aluminium oxide - the rest at temperature 280-410°C, at hydrogen pressure 3.0-7.0 MPa, at volume rate of crude oil supply 0.5-2.5 h^-1 and at ratio of hydrogen containing gas to crude oil 300-500:1 nm³/m³. Further obtained product is subject to sweetening combined with iso-de-waxing on catalyst containing (wt %): platinum - 0.15-0.6; tungsten oxide - 1.0-4.0; promoter - 0.2-1.0; zeolite ZSM-5 in H-form - 5.0-40.0, aluminium oxide - the rest at temperature 220-360°C, hydrogen pressure 2.5-4.5 MPa, volume rate of crude oil supply 0.5-2.5 h^-1 and at ratio of hydrogen containing gas to crude oil 500-1500:1 nm³/m³; also contents of hydrogen sulphide in hydrogen containing gas circulating at stage of sweetening combined with iso-de-waxing does not exceed 10 ppt.

Invention refers to method of aromatic compound and olefin hydrogenation in hydrocarbon flows. Method concerns hydrogenation of incoming hydrocarbon flow containing unsaturated components, which involves: a) formation of the catalyst including at least one metal of group VIII on noncrystalline mesoporous inorganic oxide support with at least 97 vl % of interconnected mesopores in relation to mesopores and micropores with "БЭТ" surface area at least 300 m²/g and pore space at least 0.3 cm³/g; and b) interaction of incoming hydrocarbon flow and hydrogen with the specified catalyst added in reaction hydrogenation zone in hydrogenation environment to make product with lowered content of unsaturated components. Herewith hydrogenation conditions include hourly volume liquid velocity (HVLV) within approximately more than 0.33 h^-1 to approximately 10.0 h^-1 and hydrogen circulation rate within approximately 500 SCF/barrel to approximately 20000 SCF/barrel.

Invention relates to the content of benzene in commercial gasoline. Invention claims a method for decreasing the content of benzene in gasoline fractions by hydrogenation and isomerization in the presence of catalysts at increased temperatures and pressure of raw consisting of HK-85C fraction of the stable reforming fraction containing paraffins, naphthtenes and aromatic hydrocarbons with a directly distilled fraction wherein a directly distilled fraction represents HK-70C fraction and with recycle of flow isolated from products of isomerization of a hydrogenated fraction, regulation of temperature in the isomerization block of hydrogenation by measurement of amount of recycle taken in the amount 10-30% as measured for the parent raw.

Major amount of hydrocarbon stock is brought into countercurrent contact with hydrogen in first reaction zone under hydrogenation reaction conditions in presence of hydrogenation catalyst in at least first catalyst bed wherein liquid leaving stream comes out of the bottom of the first reaction zone and hydrogen-containing gas stream comes out of the top of the first reaction zone. After that, insignificant part of hydrocarbon-containing stock comes into contact with above-mentioned hydrogen-containing gas stream in the second reaction zone accommodating catalyst bed disposed in such a way as to receive hydrogen-containing stream from the first reaction zone.

Diesel distillates are passed through "filtering" bed composed by ceramic ball bed, which occupies 0.2 to 5.0% of reaction space. Feed is then subjected (i) to hydrofining in presence of catalyst present in the form of contact bed containing alumina-supported molybdenum oxide (2-10%) occupying 0.5 to 10% of reaction space and (ii) to hydrogenation in presence of alumino-nickel-molybdenum and/or alumino-cobalt-molybdenum catalyst. Process is conducted at 340-400 C, pressure 4-10 MPa, volumetric feed supply rate 0.5-3.0 h-1, and hydrogen-containing gas-to-feed volume ratio 400-1200. Invention allows level of sulfur to be lowered to 0.005 wt % or below with amount of polycyclic aromatics being below 11 wt %.

The invention is pertaining to the field of oil-processing industry, in particular, to the method of production of the base oil with the high content of the saturated hydrocarbons. The method provides, that the selectively purified base oil raw stock is subjected at the stage of (a) to the contact with the hydrogen-containing gas in the first reaction zone containing of one or more the fixed beds of the catalytic agent containing at least one metal of VI-B group and at least one base metal of VIII group deposited the refractory, oxide carrier. On the stage (b) the stream of the outgoing gas makes the contact with the hydrogen-carrying gas in the second reaction zone containing one or more the fixed beds of the catalytic agent containing the alloy of platinum and palladium and the silica-alumina carrier. At that the base oil raw stock at the stage of (a) moves as a counter current to the up-going stream of the hydrogen-containing gas. The technical result of the invention is the improved quality of the target product.

Invention relates to production of colorless basic lubricating oil containing more than 90% saturated hydrocarbons and less than 0.03% sulfur, and possessing viscosity coefficient 80-120. In particular, starting hydrocarbon feedstock is brought into contact with hydrogen in presence of hydrogenation catalyst at temperature above 300°C and WSHV value 0.3 to 2 kg oil per 1 L catalyst/h, after which rectification intermediate product is kept in contact with hydrogen in presence of catalyst at temperature below 280°C.

Hydrocarbon raw material with boiling point between 200°C and 600°C is brought into contact with hydrogen over hydropurification catalyst at hydropurification conditions. Hydropurification effluent is cooled and brought into contact over hydropurification catalyst in afterpurification reactor at temperature sufficient to reduce polyaromatic hydrocarbon content.

The invention relates to the refining and can be used in the production of high-octane gasoline

First raw stock comprises mainly hydrocarbons containing at least 4 hydrocarbon atoms and includes at least one unsaturated compound, including benzene, with the property that the above first raw stock is treated in a distillation zone, a zone of impoverishment and a zone of rectification united with a zone of hydrogenation reaction, at least partial, in regard to the zone of distillation, containing at least one catalytic layer. Hydrogenation of at least a part of unsaturated compounds comprising the first raw stock is carried out in the presence of a hydrogenation catalyst and a gas flow containing hydrogen. The first raw stock is extracted from the reaction area, at least at a level of extraction in the distillation zone. The reaction zone effluent, at least partially, is again introduced to the distillation zone, at least at the level of repeated introduction in order to ensure continuity of distillation and to receive the effluent impoverished by the unsaturated compounds in the upper part of the distillation zone, a lateral branch to the distillation zone and in the lower part of the distillation zone. The method includes treatment of at least one second raw stock comprising at least one unsaturated compound, including benzene, at least partially injected to the zone of hydrogenation reaction being external in regard to the distillation zone. At that in the second raw stock benzene content varies from 2 vol.% up to 10 vol. %.

Invention relates to a method which involves steps of hydrogenating a mixture of secondary gas oil fractions in severe conditions at pressure of 270-300 kg/cm² (hydrogen pressure not lower than 200 kg/cm²), temperature of 300-400°C, volume rate of feeding material of 0.3-1.0 h^-1 and ratio of circulation gas to material of not less than 2000:1 (ratio of hydrogen to material of not less than 1500:1); a diesel fraction is separated from the hydrogenation products by fractionation; the diesel fraction is oxidised by mixing with oxidised diesel fuel to content of peroxide compounds of 3-5 mmol/kg, where aromatic (monocyclic, bicyclic, tricyclic) compounds, as well as paraffin-naphthene compounds are oxidised to form peroxide compounds in amount of 20-350 mmol/kg. The oxidised diesel fraction is compounded with the diesel fraction separated from hydrogenation products (non-oxidised) by fractionation to the required amount based on antiwear and cetane characteristics.

Invention relates to methods of producing liquid hydrocarbons from methane. Disclosed is a method of converting methane into liquid hydrocarbons, in which material containing methane is brought into contact with a dehydrocyclisation catalyst under conditions suitable for conversion of said methane to aromatic hydrocarbons, including naphthalene, and obtaining a first effluent containing hydrogen and at least 5 wt % aromatic hydrocarbons more than said starting material. At least a portion of aromatic hydrocarbons from the first effluent then reacts with hydrogen to form a second effluent having lower content of benzene compared to said first effluent, and at least a portion of hydrogen from the first effluent reacts with carbon monoxide, carbon dioxide or mixture thereof to obtain an additional effluent containing water and a hydrocarbon, and at least a portion of the hydrocarbon in said additional effluent is returned to said contact step.

The invention relates to the petrochemical and refining industries, namely the recovery of solvents

Invention relates to methods of producing liquid hydrocarbons from methane. Disclosed is a method of converting methane into liquid hydrocarbons, in which material containing methane is brought into contact with a dehydrocyclisation catalyst under conditions suitable for conversion of said methane to aromatic hydrocarbons, including naphthalene, and obtaining a first effluent containing hydrogen and at least 5 wt % aromatic hydrocarbons more than said starting material. At least a portion of aromatic hydrocarbons from the first effluent then reacts with hydrogen to form a second effluent having lower content of benzene compared to said first effluent, and at least a portion of hydrogen from the first effluent reacts with carbon monoxide, carbon dioxide or mixture thereof to obtain an additional effluent containing water and a hydrocarbon, and at least a portion of the hydrocarbon in said additional effluent is returned to said contact step.

Invention relates to a method which involves steps of hydrogenating a mixture of secondary gas oil fractions in severe conditions at pressure of 270-300 kg/cm² (hydrogen pressure not lower than 200 kg/cm²), temperature of 300-400°C, volume rate of feeding material of 0.3-1.0 h^-1 and ratio of circulation gas to material of not less than 2000:1 (ratio of hydrogen to material of not less than 1500:1); a diesel fraction is separated from the hydrogenation products by fractionation; the diesel fraction is oxidised by mixing with oxidised diesel fuel to content of peroxide compounds of 3-5 mmol/kg, where aromatic (monocyclic, bicyclic, tricyclic) compounds, as well as paraffin-naphthene compounds are oxidised to form peroxide compounds in amount of 20-350 mmol/kg. The oxidised diesel fraction is compounded with the diesel fraction separated from hydrogenation products (non-oxidised) by fractionation to the required amount based on antiwear and cetane characteristics.

First raw stock comprises mainly hydrocarbons containing at least 4 hydrocarbon atoms and includes at least one unsaturated compound, including benzene, with the property that the above first raw stock is treated in a distillation zone, a zone of impoverishment and a zone of rectification united with a zone of hydrogenation reaction, at least partial, in regard to the zone of distillation, containing at least one catalytic layer. Hydrogenation of at least a part of unsaturated compounds comprising the first raw stock is carried out in the presence of a hydrogenation catalyst and a gas flow containing hydrogen. The first raw stock is extracted from the reaction area, at least at a level of extraction in the distillation zone. The reaction zone effluent, at least partially, is again introduced to the distillation zone, at least at the level of repeated introduction in order to ensure continuity of distillation and to receive the effluent impoverished by the unsaturated compounds in the upper part of the distillation zone, a lateral branch to the distillation zone and in the lower part of the distillation zone. The method includes treatment of at least one second raw stock comprising at least one unsaturated compound, including benzene, at least partially injected to the zone of hydrogenation reaction being external in regard to the distillation zone. At that in the second raw stock benzene content varies from 2 vol.% up to 10 vol. %.

Invention is related to the hydrogenisation of a low-sulphur raw material containing less than 15 mln^-1 of sulphur up to liquids with a very low content of sulphur and aromatic compounds containing less than 5 mln^-1 of sulphur and less than 100 mln^-1 of the aromatic compounds boiling within the range from 150 up to 400°C and having the boiling temperature range less than 80°C. The method includes a stage of the catalytic hydrogenation of the above raw material at a temperature from 80 up to 180°C and pressure from 60 up to 160 bar, consisting of two or three stages of hydrogenisation with a nickel-containing catalyst wherein each stage of hydrogenisation is carried out in a separate reactor, and a stage of hydrogenised products fractionating up to the liquids having certain boiling ranges.

Hydrocarbon raw material with boiling point between 200°C and 600°C is brought into contact with hydrogen over hydropurification catalyst at hydropurification conditions. Hydropurification effluent is cooled and brought into contact over hydropurification catalyst in afterpurification reactor at temperature sufficient to reduce polyaromatic hydrocarbon content.

Invention relates to production of colorless basic lubricating oil containing more than 90% saturated hydrocarbons and less than 0.03% sulfur, and possessing viscosity coefficient 80-120. In particular, starting hydrocarbon feedstock is brought into contact with hydrogen in presence of hydrogenation catalyst at temperature above 300°C and WSHV value 0.3 to 2 kg oil per 1 L catalyst/h, after which rectification intermediate product is kept in contact with hydrogen in presence of catalyst at temperature below 280°C.

The invention is pertaining to the field of oil-processing industry, in particular, to the method of production of the base oil with the high content of the saturated hydrocarbons. The method provides, that the selectively purified base oil raw stock is subjected at the stage of (a) to the contact with the hydrogen-containing gas in the first reaction zone containing of one or more the fixed beds of the catalytic agent containing at least one metal of VI-B group and at least one base metal of VIII group deposited the refractory, oxide carrier. On the stage (b) the stream of the outgoing gas makes the contact with the hydrogen-carrying gas in the second reaction zone containing one or more the fixed beds of the catalytic agent containing the alloy of platinum and palladium and the silica-alumina carrier. At that the base oil raw stock at the stage of (a) moves as a counter current to the up-going stream of the hydrogen-containing gas. The technical result of the invention is the improved quality of the target product.