RU2731216C2 - Method for complex production and processing of matrix oil - Google Patents

Abstract

FIELD: oil and gas industry.

SUBSTANCE: invention relates to processing of heavy hydrocarbon material with high content of resins and can be used in processing of high-boiling fractions of matrix oil. Invention relates to an integrated method for complex production and processing of matrix oil, which includes: a) a step of extracting matrix oil from the formation using an aromatic solvent of a heavy portion of matrix oil with a weight ratio of said solvent to matrix oil of 1:1 to 2:1; b) a step for dehydration and desalting of a mixture of matrix oil with an aromatic solvent with subsequent atmospheric distillation and extraction of diesel fraction 180–350 °C, residue more than 350 °C and mixture of hydrocarbon gas, gasoline fraction and aromatic hydrocarbons; c) stage of secondary fractionation of mixture from stage b) to mixture of hydrocarbon gases with light gasoline—fraction up to 105 °C, heavy gasoline—fraction 140–180 °C and a fraction of aromatic hydrocarbons with a boiling point of 105–140 °C; d) hydroconversion of residue of more than 350 °C from step b), characterized by that an aqueous solution of a molybdenum catalyst precursor is added to said residue, the obtained mixture is dispersed to form a stable inverted emulsion, mixed with hydrogen, heated to reaction temperature 380–460 °C and performing hydrogenation in a reactor with an upward flow at said temperature and pressure of 7–10 MPa in the presence of a nanosized catalyst formed from a precursor, to obtain hydrocarbon gas, which is removed as a commercial product, gasoline fraction, diesel fraction 180–350 °C and residue more than 350 °C; e) metal extraction stage, according to which residue is more than 350 °C from step d) is directed to atmospheric vacuum distillation with separation of residue with boiling point of more than 520 °C, from which molybdenum catalyst precursor and metals are separated as a commercial product; e) a step for separating and concentrating aromatic hydrocarbons from the benzene fraction of step d) and aromatic hydrocarbons of step c) by fractionation to obtain a benzene-toluene-xylene fraction with a boiling point of 105–140 °C and content of toluene of not less than 70 wt % for use as an aromatic solvent of heavy part of matrix oil at step a) and residual heavy gasoline fraction; g) stage of hydro-enrichment of mixture of diesel fractions from stages b) and d) together with heavy gasoline of stage c) and residual gasoline fraction of stage e) and hydrogen-containing gas with production of diesel fuel and sulfur as commercial products, hydrocarbon gas and gasoline distillate; h) stage of liquefaction of mixture of hydrocarbon gas and light gasoline of stage c) and hydrocarbon gas of stage g); i) stage of mixing liquefied hydrocarbon gas of stage h) and gasoline distillation of stage g) and discharge of obtained mixture as commercial product—gas condensate component.

EFFECT: technical result is maximum extraction of valuable commercial products: petroleum products, including hydrocarbon gases, sulfur and metals from heavy matrix oil by ecofriendly, non-waste method.

4 cl, 9 tbl, 1 dwg, 2 ex

Description

The invention relates to methods for processing heavy hydrocarbon feedstock with a high content of resins and asphaltenes under hydrogen pressure in the presence of heterogeneous nanosized catalysts and can be used in the processing of high-boiling fractions of matrix oil.

Matrix oil of gas condensate and oil and gas condensate fields is a natural formation, unique in its properties, a special type of oils containing complex bulk high-molecular compounds associated with a dense part of carbonate rocks, in other words, a carbonate matrix.

At present, matrix oil is a new unconventional source of hydrocarbon resources and a promising feedstock for the petrochemical industry in Russia.

The total geological reserves of matrix oil are very significant, for example, the reserves of the Orenburg oil and gas condensate field are 2.56 billion tons.

The physical and chemical properties as well as the composition of the heavy oil depend on its origin. It is known that heavy and high-viscosity oils are enriched in heavy impurity elements, many of which have pronounced toxic properties. Thus, the hydrocarbon composition of the initial matrix oil contains general resins (alcohol-benzene) - 22.45% by weight, asphaltenes - 40.64% by weight, oils - 36.91% by weight, including 14.72% by weight. solid paraffins, resins and asphaltenes contain a significant amount of metals (V, Ni, Fe, etc.). It has been established that heavy oils are the most enriched in metal complexes, especially vanadium and nickel.

According to expert estimates, the world's potential resources of vanadium in heavy oil and bitumen are about 125 million tons, and recoverable along the way with oil - about 20 million tons. Now vanadium and nickel are lost when burning oil products, causing great damage to the environment. Moreover, with the depletion of light oil reserves and the transition to the massive development of heavy oil with a high content of vanadium, nickel and other toxic elements, the volumes of metal complexes simultaneously recovered with oil will inevitably increase and, without appropriate measures for their extraction and treatment to protect the environment, they will be developed. will be invalid.

High-molecular components of matrix oil (asphaltenes, resins) contain high concentrations of trace elements, rare and rare-earth metals, and the concentration of gallium, a number of noble, rare and rare-earth metals in them is characterized by abnormally high values. Some metals, such as titanium, nickel, chromium, lead, zinc, vanadium and gallium, are tentatively found in matrix oil at commercial concentrations

At present, the most acceptable technology for the extraction of matrix oil is the technology of "flushing" the reservoir with a solvent from the injection well to the producing well with additional pumping of a gaseous agent for displacement. The composition of the mixture extracted from the well will change cyclically - from 100% of the mass. the content of the light part (without IUD - 0 wt%) to a mixture containing 30 wt%. Navy. The content of the aromatic solvent (toluene) also changes cyclically: from 0% of the mass. up to 60% of the mass. on the recoverable matrix oil mixture. However, to date, there is not a single commercially realized plant or production that processes matrix oil. Most Russian refineries are not designed to process heavy, high-viscosity oils. Some heavy high-viscosity oils can be processed at refineries in a mixture with conventional oils using traditional technologies.

Other such oils can be processed only at specialized enterprises that produce a limited range of petroleum products and have special installations and processes in their composition.

It should be noted that complex methods of processing heavy matrix oil have not been found in the patent literature, and there are no analogues to the proposed invention.

The objective of the present invention is to develop an environmentally safe, waste-free method for complex processing of heavy matrix oil with maximum recovery of valuable commodity products: petroleum products, including hydrocarbon gases, sulfur and metals.

The task is solved by the fact that the proposed method for the integrated production and processing of matrix oil, including:

a) the stage of extracting matrix oil from the formation using an aromatic solvent of the heavy part of the matrix oil at a weight ratio of said solvent to matrix oil from 1: 1 to 2: 1;

b) the stage of dehydration and desalting of a mixture of matrix oil with an aromatic solvent, followed by atmospheric distillation and isolation of a diesel fraction of 180-350 ° C, a residue of more than 350 ° C and a mixture of hydrocarbon gas, gasoline fraction and aromatic hydrocarbons;

c) the stage of secondary fractionation of the mixture from stage b) into a mixture of hydrocarbon gases with light gasoline - a fraction up to 105 ° C, heavy gasoline - a fraction of 140-180 ° C and a fraction of aromatic hydrocarbons with a boiling point of 105-140 ° C;

d) the stage of hydroconversion of the residue of more than 350 ° C from stage b), characterized in that an aqueous solution of a precursor of a molybdenum-containing catalyst is introduced into the said residue, the resulting mixture is dispersed until a stable inverse emulsion is formed, mixed with hydrogen, heated to a reaction temperature of 380-460 ° C and hydrogenation is carried out in a reactor with an ascending flow at the specified temperature and pressure of 7-10 MPa in the presence of a nano-sized catalyst formed from the precursor to obtain a hydrocarbon gas, which is withdrawn as a commercial product, a gasoline fraction, a diesel fraction of 180-350 ° C and a residue of more than 350 ° C;

e) the stage of metal extraction, according to which the residue of more than 350 ° C from stage d) is sent to atmospheric-vacuum distillation with the isolation of the residue with a boiling point of more than 520 ° C, from which the precursor of the molybdenum-containing catalyst and metals are isolated as a commercial product;

f) the stage of separation and concentration of aromatic hydrocarbons from the gasoline fraction of stage d) and aromatic hydrocarbons of stage c) by fractionation to obtain a benzene-toluene-xylene (BTX) fraction with a boiling point of 105-140 ° C and a toluene content of at least 70 wt%. , for use as an aromatic solvent of the heavy part of the matrix oil in stage a) and the residual heavy gasoline fraction;

g) the stage of hydrofining the mixture of diesel fractions from stages b) and d) together with heavy gasoline of stage c) and the residual gasoline fraction of stage g) to obtain diesel fuel and sulfur as marketable products, hydrocarbon gas and gasoline distillate;

h) a stage of liquefaction of a mixture of hydrocarbon gas and light gasoline of stage c) and a hydrocarbon gas of stage g);

i) the stage of mixing the liquefied hydrocarbon gas of stage h) and the gasoline distillate of stage g) and the withdrawal of the resulting mixture as a commercial product - a component of gas condensate.

A particular case of the proposed method consists in the fact that at stage d) the hydrocarbon gas is purified by absorption with amine before being withdrawn as a commercial product.

A special case of the proposed method also consists in the fact that at stage e) the residue of more than 520 ° C is first subjected to gasification under superadiabatic conditions in the filtration combustion mode to obtain fuel gas, after which the fuel gas is burned to obtain heat or electricity, and is extracted from the flue gases with using a filter, molybdenum trioxide and washed with an aqueous solution of ammonia to obtain a precursor of a molybdenum-containing hydroconversion catalyst, which is directed to stage d), and metals as a commercial product are separated from the ash.

A particular case of the proposed method also consists in the fact that in step f) the residual gasoline fraction is obtained by mixing two fractions leaving the aromatic hydrocarbon separation and concentration unit boiling higher and lower than the specified benzene-toluene-xylene fraction, respectively.

The method of complex processing of matrix oil according to the invention is implemented as follows.

Since at the moment it is not possible to extract the "whole" matrix oil from the oil-forming formation, model mixtures of matrix oil are prepared, simulating the matrix oil of the Orenburg gas condensate field, consisting of high-molecular compounds obtained by extraction with toluene from asphalt-resin-paraffin deposits, and a light part matrix oil (gas condensate from the well of the Orenburg gas condensate field, taken in different proportions.

Prepare model mixtures containing 30, 20 and 15% of the mass. Heavy part of matrix oil. The resulting samples containing 30 and 20% of the mass. heavy parts, are gel-like black substances, non-flowing at room temperature. A model mixture containing 15% of the mass. heavy part, is a viscous semi-liquid product of black color. The relative density, measured in relation to the density of water, for all obtained model mixtures is 0.773. The content of metals in the remains of matrix oil, boiling above 350 ° C, depending on the composition of the matrix oil, averages from 80 to 1150 ppm: vanadium - from 40 to 300 ppm; nickel - from 10 to 180 ppm; sodium - from 10 to 170 ppm; copper - from 5 to 100 ppm; zinc - from 8 to 90 ppm; chromium - from 5 to 80 ppm; manganese - from 3 to 85 ppm; potassium - from 3 to 45 ppm; strontium - from 1 to 45 ppm; , barium - from 1 to 25 ppm; molybdenum - from 1 to 20 ppm; lead - from 1 to 10 ppm; titanium - from 0 to 8 ppm; gallium - 0 to 3 ppm; cadmium - from 0 to 2 ppm, etc. The sulfur content in the fraction boiling above 350 ° C, depending on the location and matrix oil in the OOGCF formations and its composition, can vary in the range from 2.0 to 11.0 wt% ...

The fractional composition and physicochemical characteristics of the matrix oil, presented in table 1, are estimated using the Potstill distillation method.

Oil dehydration and desalting can be carried out in separators and electric dehydrators of various types, as well as by heating and subsequent holding in a settling tank.

Fractionation is carried out in two stages: 1) atmospheric distillation; 2) secondary fractionation. The separation of light and aromatic hydrocarbons allows you to minimize the influence of the aromatic part of the feed, the composition of which can fluctuate, on other fractions.

The bottoms of atmospheric distillation (fraction more than 350 ° C) are processed using the technology of hydroconversion of heavy oil feedstock in the presence of nanosized catalyst particles at a reaction temperature of 380-460 ° C and a pressure of 7-10 MPa. The use of a nano-sized catalyst, which provides a highly developed contact surface between the catalyst and the components of the feedstock, makes it possible to achieve a high conversion of oil residues at a relatively low hydrogen pressure with a maximum decrease in the rate of polymerization reactions. An additional advantage of such catalysts is a high yield of distillate products suitable for subsequent processing by traditional methods to obtain commercial motor fuels.

The use of technology for the separation of metals from the residual fraction of matrix oil allows obtaining the maximum amount of valuable components during its processing, as well as a precursor of a nano-sized molybdenum-containing catalyst for hydroconversion. The separation of metals from the heaviest fraction (more than 520 ° C) of the matrix oil can be carried out by known methods for the separation of metals from heavy oils, for example, by treating the residue with solid adsorbents followed by the separation of the concentrate from the adsorbent, as described in and.with. USSR No. 499289, or leaching the residue with sulfuric acid followed by washing with water vanadium compounds, as described in and.with. USSR No. 1177337, extraction, etc. However, to increase the recovery of valuable metals, it is preferable to first use a combination of two combustion stages: filtration combustion under superadiabatic conditions and subsequent combustion of the resulting fuel gas. Filtration combustion means the process of oxidation of a solid fuel layer when a gaseous oxidizer is filtered through it - the most widespread case of wave combustion in a heterophase system.

The separation of the benzene-toluene-xylene fraction, which is then returned to the stage of oil recovery as an aromatic solvent, is carried out by fractionation in a column. The target fraction is taken out as a side strap. The overhead fraction and bottoms (fractions boiling higher and lower than said benzene-toluene-xylene fraction, respectively) are preferably mixed and discharged as residual gasoline fraction. If necessary, some of these fractions, with the exception of the target one, can be used for refluxing the column.

Diesel fractions, heavy gasoline and residual (heavy) gasoline fraction are subjected to hydrotreating under milder conditions than the conditions of hydroconversion: reactor pressure 2-4 MPa, temperature 360-380 ° C. Low-sulfur hydrocarbon fractions are removed from the hydrofining unit: diesel fuel (commercial product), hydrocarbon gas and gasoline distillation, as well as hydrogen sulfide. Hydrogen sulfide is captured in the gas cleaning system and sulfur is obtained from it by known methods - for example, using the Claus process or its modifications.

The hydrocarbon gas is liquefied together with a mixture of hydrocarbon gas and light gasoline from the secondary fractionation stage. Then the liquefied petroleum gas is mixed with gasoline distillate. The resulting mixture is a commercial product - a component of gas condensate.

The possibility of carrying out the invention is confirmed by examples.

Example 1. Model mixture - matrix oil with a heavy part content of 20 wt%. - mixed with an aromatic solvent containing 90% of the mass. toluene, in a mass ratio solvent: oil 1: 1. A mixture of matrix oil with an aromatic solvent is dehydrated and desalted by separating water in an electric dehydrator at the ELOU unit (electric desalting unit).

Further, the dehydrated and demineralized raw material enters the atmospheric distillation unit - a partial topping column, in which it is divided into three fractions:

hydrocarbon gases С ₁ -С ₄ , released during stabilization and being the top product of the column, gasoline fraction and aromatic hydrocarbons - a mixture of these fractions (light fraction) in one stream goes into the next fractionation column;

- diesel fraction (180-350 ° C), which is sent for hydrotreating;

- VAT residue - a fraction of more than 350 ° C, which is sent to hydroconversion.

The characteristics of the obtained fractions (light, diesel and still bottoms over 350 ° C) are given in table. 2-4.

In the second fractionating column, secondary fractionation of the previously isolated light fraction is carried out by atmospheric distillation. The following products are discharged from the second fractionating column: light gasoline and hydrocarbon gas as a mixture (fraction up to 105 ° С) - the overhead product, heavy gasoline (fraction 140-180 ° С) - distillation residue. The fraction of aromatic hydrocarbons with a boiling point of 105-140 ° C, which is a side product of this column, is fed further to the aromatic hydrocarbon separation and concentration unit.

The remainder over 350 ° C from the atmospheric distillation stage is processed using the hydroconversion technology. An aqueous solution of a precursor of a molybdenum-containing nanoscale catalyst - ammonium molybdate - with a concentration of 5 wt% is introduced into the residue. until the content of the catalyst precursor in the feed is 2.5% of the mass. at a temperature of 100 ° C. The resulting mixture is dispersed with a dispersant until a stable inverse emulsion is formed, and then mixed with hydrogen. Hydrogen for hydroconversion is supplied in an amount of 2% by weight of the residue over 350 ° C.

The mixture of feedstock and hydrogen is fed into an upflow hydroconversion reactor, where the hydrogenation reaction is carried out at a pressure of 7 MPa and a temperature of 450 ° C. Under the reaction conditions, a nanosized catalyst, molybdenum sulfide, is formed from the precursor. The hydroconversion products are cooled to 350 ° C by introducing light vacuum gas oil and fed to the separation unit, where they are separated into hydrocarbon gas, a gasoline fraction, a diesel fraction of 180-350 ° C and a residue of more than 350 ° C. The composition of the hydroconversion products is given in table. five.

Hydroconversion hydrocarbon gas is discharged as a commercial product. It can be used for the needs of the plant itself.

The remainder of the hydroconversion of more than 350 ° C is sent to atmospheric-vacuum distillation with the isolation of the residue with a boiling point of more than 520 ° C, from which the metals are isolated and a precursor of the molybdenum-containing catalyst is obtained. To do this, the residue above 520 ° C is first subjected to gasification under superadiabatic conditions in the filtration combustion mode, passing air through the layer of residues mixed with an inert carrier, at 1300 ° C and atmospheric pressure. At the outlet of the gasifier, fuel gas is obtained - a complex mixture of combustible and non-combustible gases (CO, H ₂ , CH ₄ , other hydrocarbons, N ₂ , H ₂ O) with a fog of pyrolysis resins saturated with molybdenum compounds, as well as ash.

The fuel gas together with the entrained aerosol of molybdenum compounds of pyrolysis resins is fed into a steam boiler, where it is burned to produce a large amount of heat. In the process of combustion, the smallest droplets of hydrocarbons from pyrolysis resins are burned, and molybdenum compounds are converted into the form of molybdenum trioxide. As the flue gases cool down to 800 ° C, molybdenum trioxide condenses into dust particles, which are extracted by trapping with a ceramic filter. The recovered molybdenum trioxide is washed with an aqueous ammonia solution to form an ammonium molybdate solution, a precursor of a nanosized hydroconversion catalyst. In this case, approximately 71.5% of the mass is recovered. molybdenum compounds contained in the residue with a boiling point of more than 520 ° C and supplied to the gasifier.

The composition of ash from gasification is presented in table. 6.

Metals are isolated from this ash by leaching, filtration and extraction. The degree of extraction of gallium is 98.3% of the mass. aluminum - 100% of the mass. vanadium and nickel - 98% of the mass.

Fractions leaving the atmospheric-vacuum distillation with a boiling point of 350-520 ° C are used to irrigate the atmospheric-vacuum distillation column and to cool the products of hydroconversion.

The gasoline fraction of hydroconversion contains a large amount of aromatic hydrocarbons. This fraction and aromatic hydrocarbons from the secondary fractionation stage are fed to the inlet of the aromatic hydrocarbon separation and concentration unit in a mass ratio of 93.9: 6.1. The separation of aromatic hydrocarbons is carried out by fractionation in a column. The benzene-toluene-xylene fraction is withdrawn as a side cut (with a boiling point of 105-140 ° C). Part of the gasoline fraction of the hydroconversion is sent to the reflux of the fractionation column. Its other part, the top fraction and the still bottoms are mixed to obtain a residual gasoline fraction.

The output of benzene-toluene-xylene fraction, wt% - 74.3, residual (heavy) gasoline fraction - 25.7. The toluene content in the benzene-toluene-xylene fraction is 90% of the mass.

The recovery of the aromatic solvent is 94% of the mass.

The diesel fraction from the secondary fractionation stage is mixed with the diesel fraction of the hydroconversion before being fed to the hydrotreating, to obtain a combined diesel fraction. A feedstock containing 34.9% of the mass is fed to the hydrotreating unit. combined diesel fraction, 38.4% of the mass. residual heavy gasoline fraction and 26.6% of the mass. heavy gasoline. Hydrogen-containing gas is supplied to the hydrofining unit in the amount of 1% of the hydrocarbon raw material weight. The reaction is carried out at a pressure of 2 MPa and a temperature of 380 ° C.

The composition of the obtained products is presented in table. 7.

Hydrogen sulfide is captured in the gas cleaning system and sulfur is obtained from it.

Hydrocarbon gas from the secondary fractionation and hydrotreating stages is liquefied and sold as a component of gas condensate mixed with gasoline hydrotreating reagent.

Example 2

The model mixture - matrix oil with a heavy part content of 30% by weight - is mixed with an aromatic solvent containing 90% by weight. toluene, in a mass ratio solvent: oil 1.5: 1. A mixture of matrix oil with an aromatic solvent is dehydrated and desalted by heating it to 220 ° C and keeping it in a settling tank. Atmospheric distillation and secondary fractionation of the light fraction is carried out analogously to example 1.

The composition and properties of the light and diesel fractions of atmospheric distillation are close to those shown in example 1. The characteristics of the distillation residue over 350 ° C are shown in table 8.

The remainder over 350 ° C is processed by the hydroconversion technology. An aqueous solution of a precursor of a molybdenum-containing nanoscale catalyst - ammonium tetramolybdate - with a concentration of 5 wt% is introduced into the residue. until the content of the catalyst precursor in the feed is 2.5% of the mass. at a temperature of 100 ° C. The resulting mixture is dispersed with a dispersant until a stable inverse emulsion is formed, and then mixed with hydrogen. Hydrogen for hydroconversion is supplied in an amount of 2% by weight of the residue over 350 ° C.

The mixture of feedstock and hydrogen is fed into an upflow hydroconversion reactor, where the hydrogenation reaction is carried out at a pressure of 8 MPa and a temperature of 420 ° C. Under the reaction conditions, a nanosized catalyst, molybdenum sulfide, is formed from the precursor. The hydroconversion products are cooled to 350 ° C by introducing a diesel fraction and fed to a separation unit, where they are separated into hydrocarbon gas, a gasoline fraction, a diesel fraction of 180-350 ° C and a residue of more than 350 ° C.

The composition of the hydroconversion products does not differ from the composition of the products obtained in Example 1.

Hydroconversion hydrocarbon gas is purified by absorption with amine and discharged as a commercial product.

The remainder of the hydroconversion over 350 ° C is sent to atmospheric vacuum distillation with the isolation of the residue with a boiling point of more than 520 ° C. Metals are isolated from the latter by incineration of the residue and ash leaching. The degrees of extraction of molybdenum, gallium and aluminum are equal to 98% by mass, the degree of extraction of vanadium is 90% of the mass.

The gasoline fraction of hydroconversion contains a large amount of aromatic hydrocarbons, therefore it can be sent to the aromatic hydrocarbon recovery and concentration unit. The gasoline fraction from the hydroconversion stage and aromatic hydrocarbons from the secondary fractionation stage are fed to the inlet of the aromatic hydrocarbon separation and concentration unit in a mass ratio of 94.8: 5.2. The separation of aromatic hydrocarbons is carried out by fractionation in a column. The benzene-toluene-xylene fraction is withdrawn as a side cut (with a boiling point of 105-140 ° C). The upper fraction is sent to the reflux of the column, and the bottom residue is taken out as a residual heavy gasoline fraction.

The output of benzene-toluene-xylene fraction, wt% - 80.4, residual gasoline fraction - 19.6. The toluene content in the benzene-toluene-xylene fraction is 90% of the mass.

The recovery of the aromatic solvent is 94% of the mass.

The diesel fraction from the secondary fractionation stage is mixed with the diesel fraction of the hydroconversion before being fed to the hydrotreating, to obtain a combined diesel fraction. A feedstock containing 38.5% wt. Is fed to the hydrotreating unit. combined diesel fraction, 38.2% of the mass. residual gasoline fraction and 23.3% of the mass. heavy gasoline. Hydrogen-containing gas is supplied to the hydrofining unit in the amount of 1% of the hydrocarbon raw material weight. The reaction is carried out at a pressure of 42 MPa and a temperature of 360 ° C. The composition of the obtained products is presented in table 9.

Hydrogen sulfide is captured in the gas cleaning system and sulfur is obtained from it.

Hydrocarbon gas from the secondary fractionation and hydrotreating stages is liquefied and sold as a component of gas condensate mixed with gasoline hydrotreating reagent.

A schematic diagram of a method for complex processing of matrix oil is shown in Fig. 1.

Claims (13)

1. A method of complex production and processing of matrix oil, including: a) the stage of extracting matrix oil from the formation using an aromatic solvent of the heavy part of the matrix oil at a weight ratio of said solvent to matrix oil from 1: 1 to 2: 1; b) the stage of dehydration and desalting of a mixture of matrix oil with an aromatic solvent, followed by atmospheric distillation and isolation of a diesel fraction of 180-350 ° C, a residue of more than 350 ° C and a mixture of hydrocarbon gas, gasoline fraction and aromatic hydrocarbons; c) the stage of secondary fractionation of the mixture from stage b) into a mixture of hydrocarbon gases with light gasoline - a fraction up to 105 ° C, heavy gasoline - a fraction of 140-180 ° C and a fraction of aromatic hydrocarbons with a boiling point of 105-140 ° C; d) the stage of hydroconversion of the residue of more than 350 ° C from stage b), characterized in that an aqueous solution of a precursor of a molybdenum-containing catalyst is introduced into the said residue, the resulting mixture is dispersed until a stable inverse emulsion is formed, mixed with hydrogen, heated to a reaction temperature of 380-460 ° C and hydrogenation is carried out in a reactor with an ascending flow at the specified temperature and pressure of 7-10 MPa in the presence of a nano-sized catalyst formed from the precursor to obtain a hydrocarbon gas, which is withdrawn as a commercial product, a gasoline fraction, a diesel fraction of 180-350 ° C and a residue of more than 350 ° C; e) the stage of metal extraction, according to which the residue of more than 350 ° C from stage d) is sent to atmospheric-vacuum distillation with the release of the residue with a boiling point of more than 520 ° C, from which the precursor of the molybdenum-containing catalyst and metals are isolated as a commercial product; f) the stage of separation and concentration of aromatic hydrocarbons from the gasoline fraction of stage d) and aromatic hydrocarbons of stage c) by fractionation to obtain a benzene-toluene-xylene fraction with a boiling point of 105-140 ° C and a toluene content of at least 70 wt% for use in as an aromatic solvent for the heavy part of the matrix oil in stage a) and the residual heavy gasoline fraction; g) the stage of hydrofining the mixture of diesel fractions from stages b) and d) together with heavy gasoline of stage c) and the residual gasoline fraction of stage e) and hydrogen-containing gas to obtain diesel fuel and sulfur as marketable products, hydrocarbon gas and gasoline distillate; h) a stage of liquefaction of a mixture of hydrocarbon gas and light gasoline of stage c) and a hydrocarbon gas of stage g); i) the stage of mixing the liquefied hydrocarbon gas of stage h) and the gasoline distillate of stage g) and the withdrawal of the resulting mixture as a commercial product - a component of gas condensate. 2. The method according to claim 1, characterized in that at stage d) the hydrocarbon gas is purified by absorption with amine before being withdrawn as a commercial product. 3. The method according to claim 1, characterized in that at stage e) the residue of more than 520 ° C is first subjected to gasification under superadiabatic conditions in the filtration combustion mode to obtain fuel gas, after which the fuel gas is burned to obtain heat or electricity, is extracted from the flue gas gases using a filter of molybdenum trioxide and washed with an aqueous solution of ammonia to obtain a precursor of a molybdenum-containing hydroconversion catalyst, which is directed to stage d), and metals as a commercial product are separated from the ash. 4. The method according to claim 1, characterized in that in step f) the residual gasoline fraction is obtained by mixing two fractions leaving the aromatic hydrocarbon separation and concentration unit boiling higher and lower than said benzene-toluene-xylene fraction, respectively.

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