Vacuum gas oil and mazut purification process

FIELD: petroleum processing.

SUBSTANCE: invention, in particular, relates to purification of vacuum gas oils, mazuts, and/or dewaxed products used further as feedstock for hydrocracking and catalytic cracking as well as high-quality fuel oils and marine oils. Purification contemplates removal of polycyclic aromatic hydrocarbons, heteroatomic compounds, resins, asphaltenes, and heavy metal compounds. Process consists in liquid extraction of undesired components with two mutually immiscible solvents: polar N-methylpyrrolidone with 3-5% water at 40-60°C and nonpolar n-undecane or undecane fraction forming azeotropic mixtures with N-methylpyrrolidone having minimal boiling temperature (about 179°C). Weight ratio of nonpolar solvent to raw material is (0.4-0.5):1.

EFFECT: increased selectivity of process in reduced risk of thermooxidative and hydrolytic decomposition of N-methylpyrrolidone as well as corrosion of equipment.

1 dwg, 4 tbl, 4 ex

 

The invention relates to the refining industry and can be used when cleaning vacuum gas oils and fuel oils raw material for the process of hydrocracking and catalytic cracking of tars, asphaltenes, polycyclic aromatic hydrocarbons, heteroatomic compounds, heavy metals.

Raw material processes, hydrocracking and catalytic cracking are vacuum gas oils, which imposed strict requirements on the content of the resins, politicalarena, heteroatomic compounds, heavy metals. Increased their content in the vacuum gas oil reduces technical and economic performance of the cracking processes leads to increased coxworthy, accelerated deactivation of the catalyst, reducing the degree of conversion of raw materials and output of light oil products, low quality fuels [Ind.Eng.Chem.Res. 1998. V.37. No. 12. R-4640].

An even higher content of the above undesirable components are characterized by residual oil - fuel oil, which are mainly used as fuel and as raw material of thermal processes. In the USA, Germany and other Western European countries, the law provides more stringent environmental requirements for the quality of not only gasoline and diesel fuels, but also to the quality of the boiler is different fuels and bunker oils. So, in the US, the sulfur content in fuel oil is limited at the level of 0.2-0.5% wt. [Oil and Gas J. 2002. V.100. No. 48. P.42-44, 46-47]. In Germany since 2003 established the maximum allowable sulfur content in fuel oil 1% wt., and since 2008 - 0.9% wt. [Erdol-Erdgas-Kohle. 2001. Bd. 117. No. 12. S.552]. The sulphur content in marine fuels in accordance with Directive of the European Commission should be reduced from 2.7% wt. (average current) up to 1.5% wt. in 2005, for vessels operating in the North and Baltic seas, and up to 0.2% wt. for cabotage navigation and anchored in EU ports [Oil and gas technology. 2004. No. 2. P.59-60].

Known methods for cleaning vacuum gas oil in order to obtain lubricating oils, operational properties are also reduced with increased content of polycyclic aromatic hydrocarbons and heteroatomic compounds, liquid extraction using selective solvent is furfural, phenol, N-methylpyrrolidone, dimethylformamide, dimethylacetamide, etc. [Kazakov, L.P., crane CE Physico-chemical basis for the production of oil. M.: Chemistry, 1978. - 320 S.]. Closest to the technical essence and the achieved effect of the method of cleaning oil oil fractions N-organic.

The main drawback of these methods is not sufficiently selective removal of undesirable components in the process is selective treatment with the extract lost up to 20% wt. saturated hydrocarbons contained in the raw materials.

In addition, a significant disadvantage of the process of selective purification oil fractions N-organic - high temperature regeneration (300° (C)where possible partial decomposition of N-methylpyrrolidone and increased corrosion of equipment [World oil. 2003. No. 2. P.4-12].

To improve the selectivity of the process of removing unwanted components from the vacuum gas oil and fuel oil and reduce the maximum temperature of the regeneration of the extractant is proposed to carry out the extraction with two solvents, polar and nonpolar, and as a selective polar solvent using N-organic containing 3-5% wt. water, as well as non-polar n-undecane or undecanoyl fraction, isolated by distillation fractions of n-alkanes With10-C14received by adsorption on zeolites in the process of "Parex". N-Organic forms with n-undecanol azeotropic mixture containing 64% by weight. undecane with a normal boiling point 179°, 25°below the boiling point of N-methylpyrrolidone, so there is less danger of decomposition and corrosion activity.

Table 1 presents the conditions of the experiments extraction cleaning heavy vacuum gas oil obtained from the installation of the primary distillation of crude oil AND THE T-6 "Kirishi-petrochemical". Feature heavy vacuum gas oil obtained from it refined and extracts are presented in table 2.

Table 1

Conditions for extraction cleaning vacuum gasoil
IndexExperience 1Experience 2
The extractantN-MPN-MP
Water content, % wt.5% wt. water5% wt. water
The number of stages of extraction44
Temperature, °With: top6050
bottom5040
Non-polar solvent-undecane
Mass ratio:
solvent/raw material2/13/1
undecane/raw-0.4/1

Table 2

Characteristics of vacuum gasoil, the raffinate and extract
IndexVacuum gasoilThe raffinateExtract
Opit Experience 2Experience 1Experience 2
Yield, % wt.10076.278.523.821.5
Density at 40°C, g/cm30.8890.8850.8670.9020.969
Cocking behavior, % wt.0.370.260.220.760.92
T-RA pour, °22-23323328-
Sulfur content, % wt.1.981.11.044.85.41

All indicators extraction purification in the presence of n-undecane more effective: the loss of raw materials in the form of the extract is reduced by 10% Rel., the raffinate experience 2 has a lower density, cocking behavior and sulfur, which indicates a higher quality. Extract experience 2 shows a significantly higher density, cocking behavior, sulfur, indicating a more selective removal of impurities, their concentration in the extract.

Extraction refining of oil from organic sulfur compounds, asphaltenes, resins and politicalarena was carried out with N-organic 3% wt. water in Pris is accordance undecanol faction. Undecanoate fraction, isolated by distillation in the apparatus ARN-2 fraction of n-paraffins With10-C14installation of Parex had a composition, % wt.: Dean - 26.5; undecane - 44.0; dodecan - 25.4; tridecan - 4.1.

Conditions of extraction cleaning fuel oil:

the number of theoretical stages - 5;

temperature 50°C;

the mass ratio of N-organic/oil - 3/1;

undecanoate fraction/oil - 0.5/1.

Characteristics of the oil, selected on the installation of the at-6 "Kirishinefteorgsintez", and the resulting raffinate is given in table 3.

Due to the low solubility of asphaltenes in N-organic and insufficient reduction of maksuameti the raffinate, the following test was carried out prior beastaltiy fuel oil under the following conditions:

the mass ratio of solvent (pentane) fuel oil - 3/1;

temperature 20°C;

the number of steps for deasphalting - 1.

The output of the vacuum residue amounted to 97.1% wt.

Further extraction was carried out cleaning of vacuum residue under the conditions specified above for extraction cleaning of fuel oil. Characteristics of the raffinate obtained from the asphalt-free oil, also shown in table 3.

Table 3

Characteristics of oil and refined selective treatment
IndexThe MAZ is The raffinate (experiment 3)The raffinate from the asphalt-free oil (experiment 4)Mazut M-40 GOST 10585-75
Yield, % wt.10070.062.0-
Sulfur content, % wt.1.950.940.570.5;1.0;2.0;3.5
Cocking behavior, % wt.9.06.34.7-
Density at 60°C, kg/m3924897894-
T-RA pour, °294335≤25
T-RA flare (o/t), °178170172≥90
Viscosity,°WU: 50°36.327.827.6≤34.2
80°C9.05.95.8≤8.0
Ash content, % wt.0.210.140.12≤0.12
The aromaticity factor
(from the NMR data13C)0.214-0.155-

Feature e is Strakhov, obtained by selective cleaning of fuel oil are given in table 4.

Table 4

Characterization of the extracts obtained from fuel oil and fuel oil asphalt-free oil
IndicatorsThe extract oilExtract from the asphalt-free oil
Yield, % wt.3036,9 (on the original oil)
Pour point °2827
Sulfur content, % wt.4,3the 3.8
Cocking behavior, % wt.1513
Density at 60°C, g/cm30,9940,970
Ash content, % wt.0,370,34

From tables 3 and 4 we can draw the following conclusions:

- extraction cleaning of fuel oil N-organic in the presence undecanol fraction with mass ratios of the raw material 3:1 and 0.5:1, respectively, reduces the sulfur content of more than twice and cocking behavior in 1.5 times;

- the combined method pentanol the deasphalting under mild conditions with subsequent extraction cleaning asphalt-free oil under the same conditions allows to obtain low-sulfur fuel oil with a sulfur content of about 0.5% wt. from chamois the buffer of net oil (S≈ 2% wt.) with half cocking behavior;

a significant decrease in the density, viscosity and aromaticity factor refined compared with the original oil, and high density extracts indicate the selective removal of polycyclic aromatic hydrocarbons;

data about ash indicate the degree of removal of metals from oil and 53.3 64.6% wt. in experiments 3 and 4, respectively;

- the resulting refined comply with the requirements of fuel oil M-40 without adding more expensive atmospheric gas oil or diesel fraction and the high pour point can be easily reduced to the required level by adding small amounts of depressants;

- significant improvement of the quality of the refined compared with the original oil will allow you to use them as raw material for catalytic cracking and hydrocracking.

Extracts isolated from heavy vacuum gas oil and fuel oil, can be used as high-quality components for the production of road bitumen, and as plasticizers for rubber mixtures and polymer compositions.

Schematic diagram of the extraction cleaning heavy vacuum gas oil or heating oil is represented in the drawing.

Schematic diagram of the extras is klonoa cleaning heavy vacuum gas oil or fuel oil N-organic in the presence of undecane or undecanol fraction of N-organic is fed into the top of extractor I, and fuel oil or vacuum gas oil and undecanoate fraction having less density in the lower part of the extractor. From rafinate phase is distilled over azeotropic mixture of N-methylpyrrolidone components undecanol the first fraction in the atmospheric raffinates column 2, then in vacuum column 3. Azeotropic mixture after condensation and cooling (chillers-condensers, tube furnaces and heat exchangers on the diagram are not listed) represent a heterogeneous system, which is divided into the separator 7. The upper hydrocarbon layer is returned to the bottom of the extractor, and the lower layer (N-organic impurities water) in the upper part of the extractor.

From the extract phase in the atmospheric extract column 4 mixture is distilled over N-methylpyrrolidone with undecanol faction. Then a large part of the N-methylpyrrolidone located in a large excess in the extract phase, Argonauts in column 5. The remaining small amount of N-methylpyrrolidone Argonauts from the extract in vacuum column 6. To reduce the temperature in the lower part of this column can be submitted undecanoate faction - the top layer of the separator 8. In the separator 8 is concentrated most of the water entering the extractor with water N-organic, so its solubility in undecanol fraction decreases sharply, and return impurities of the extractant in column 6 p is essentially none.

Thus, conducting extraction cleaning of fuel oil (heavy vacuum gas oil) in the presence of undecanol fraction leads to the following advantages in comparison with extraction without nonpolar solvent:

- increases the selectivity of the separation - concentration of undesirable components in estrace and the yield of raffinate;

- increases the difference between the densities of the phases, which allows to increase the performance of the extractor;

- decreases the temperature in the columns 2, 3, 4, 6 as a result of azeotrope N-methylpyrrolidone components undecanol fraction, resulting in lower energy consumption and reduce the risk of oxidative and hydrolytic decomposition of N-methylpyrrolidone and corrosion of equipment.

Example 1 (prototype).

In the lower part of the Packed extraction columns efficiency 4 theoretical stages is served at 50°heavy vacuum gas oil (consumption of 100 g/h), and in the upper part of the 60°C - N-organic 5% wt. water (flow rate of 200 g/h). In the countercurrent extraction after stable mode are selected at the same time raffinata (97.5 g) and the extract phase (202.5 g).

From rafinate phase rectification apparatus oil ARN-2 Argonauts under vacuum 21.3 g of N-methylpyrrolidone, and as residue obtained 76.2 g of raffinate, the characteristics of which are presented in TA is L.2.

From the extract phase at the ARN-2 Argonauts 10 g of water and under vacuum 168.7 g of N-methylpyrrolidone. The temperature of the VAT balance at the end of the experiment 300°With the mass of the cubic residue (extract) - 23.8, Characteristic of the extract are given in table 2.

Example 2.

In the lower part of the Packed extraction columns efficiency 4 theoretical stages is served at 40°heavy vacuum gas oil (consumption of 100 g/h) and n-undecane (40 g/h), and in the upper part at 50°C - N-organic 5% wt. water (flow rate of 300 g/h). In the countercurrent extraction after stable mode are selected at the same time raffinata (108.7 g) and the extract phase (331.3 g).

From rafinate phase ARN-2 Argonauts 30.19 g of a mixture of solvents containing 0.05 g of water, 3.77 g of N-methylpyrrolidone and 26.37 g of n-undecane the results of analysis by gas chromatography. VAT residue represents the raffinate (78.5 g), the characteristics of which are given in table 2.

From the extract phase at the ARN-2 Argonauts 14.95 g of water and 21.3 g of azeotropic mixtures undecane - N-organic, boiling at 179°and containing 64% by weight. n-undecane (13.63 g) and 36% wt. N-methylpyrrolidone (7.67 g). Then under vacuum Argonauts 265.9, N-methylpyrrolidone. To kubulau residue is added to the upper hydrocarbon layer combined water and azeotropically factions, 13.6 g of n-undecane. Vacuum rivers is eficacia Argonauts azeotrope of n-undecane with the remaining small amount (7.66 g) N-methylpyrrolidone. The temperature of the VAT balance at the end of the experiment amounted to 275°s, and its mass (extract) - 21.5,

Example 3.

In the lower part of the Packed extraction columns efficiency 5 theoretical stages is served at 50°With oil (consumption of 100 g/h) and undecanoyl fraction (50 g/h), and in the upper part at the same temperature - N-organic 3% wt. water consumption 309 g/h). In the countercurrent extraction after stable mode are selected at the same time raffinata (128.2 g) and extract (330.8 g) phase.

From rafinate phase ARN-2 Argonauts under vacuum 58.2 g of a mixture of solvents containing the results of chromatographic analysis of 0.9 g of water, 27.3 g undecanol fraction and 30 g of N-methylpyrrolidone. VAT residue represents the raffinate (70.0 g), the characteristics of which are given in table 3.

From the extract phase at the ARN-2 Argonauts 8.1 g of water and 35.5 g of azeotropic mixtures containing 12.8 g of N-methylpyrrolidone and 22.7 g undecanol faction. Then under vacuum Argonauts 245.0 g of N-methylpyrrolidone. The upper hydrocarbon layer of the previous two fractions, water and azeotropically, is separated and added to kubulau residue. Vacuum distillation Argonauts azeotropic mixture undecanol fraction with the remaining small amount (12.2 g) N-methylpyrrolidone. The temperature of the VAT balance at the end of the experiment amounted to 260°C. Cube the new balance - extract (30 g), the characteristics of which are given in table 4.

Example 4.

The oil was subjected deasphalting at 20°and the mass ratio of pentane 3:1. The output of the vacuum residue amounted to 97.1% wt., coking ability to Conradson asphalt-free oil - 6.2 wt.%, the sulfur content of 1.8 wt.%.

Next in terms of experience 3 was carried out extraction cleaning 100 grams of vacuum residue. Received 92.5 g raffinates and 366.5 g of the extract phase.

From rafinate phase ARN-2 Argonauts under vacuum 30.5 g of a mixture of solvents containing the results of chromatographic analysis of 0.6 g of water, 13.9 g undecanol faction and 16 g of N-methylpyrrolidone. VAT residue represents the raffinate (62 g), the characteristics of which are given in table 3.

From the extract phase Argonauts 8.4 g of water and 56.4 g of azeotropic mixtures containing 20.3 g of N-methylpyrrolidone and 36.1 g undecanol faction. Then under vacuum Argonauts USD 243.7 g of N-methylpyrrolidone. The upper hydrocarbon layer of the previous two fractions, water and azeotropically, is separated and added to kubulau residue. Vacuum distillation Argonauts azeotropic mixture undecanol fraction with the remaining small amount (20.0 g) N-methylpyrrolidone. The temperature of the VAT balance at the end of the experiment amounted to 255°C. VAT residue extract (38.0 g), the characteristics of which are given in table 4.

The way the eyes of the TCI vacuum gas oil, fuel oil and/or deasphaltization by liquid extraction of polycyclic aromatic hydrocarbons, heteroatomic compounds, resins, asphaltenes and heavy metals N-organic containing 3-5 wt.% water at a temperature of 40-60°C, characterized in that the extraction is carried out in the presence of n-undecane or undecanol faction, which form azeotropic mixtures with N-organic, boiling at 25°With lower N-methylpyrrolidone, when the mass ratio of non-polar solvent and raw material 0.4 to 0.5:1.



 

Same patents:

The invention relates to the extraction methods of cleaning oil from sulfur compounds

The invention relates to the refining industry and can be used for cleaning vacuum gas oil from aromatic hydrocarbons, heteroatomic compounds and heavy metals with the aim of obtaining high-quality raw materials for the process of hydrocracking and catalytic cracking

The invention relates to a process for recovering organic acids including naphthenic acids, heavy metals and sulfur from the source of crude oil

The invention relates to a process for recovering organic acids from the source of crude oil

The invention relates to the refining industry and can be used when cleaning the raw material for hydrocracking and catalytic cracking from polycyclic aromatic hydrocarbons, heteroatomic compounds and heavy metals

The invention relates to the refining industry and can be used for simultaneous receipt of hydrotreated diesel fraction environmentally friendly diesel fuel that meets the requirements for the content of aromatic hydrocarbons, and aromatic solvents "type Nefras AR" and "Solvent oil with a content of aromatic hydrocarbons of not less than 98 wt.%

The invention relates to the refining industry and can be used to remove aromatic hydrocarbons from hydrotreated oil fraction with the aim of obtaining high-quality jet fuel with simultaneous extraction of aromatic solvent

The invention relates to the cleaning of oil fractions of crude oil and can be used in the refining industry

The invention relates to methods of cleaning oil from sulphides and can be used in refining and petrochemical industries

The invention relates to the separation of aromatic hydrocarbons, C8of the xylene fraction catalyzate reforming by azeotropic distillation

FIELD: petroleum processing.

SUBSTANCE: invention, in particular, relates to purification of vacuum gas oils, mazuts, and/or dewaxed products used further as feedstock for hydrocracking and catalytic cracking as well as high-quality fuel oils and marine oils. Purification contemplates removal of polycyclic aromatic hydrocarbons, heteroatomic compounds, resins, asphaltenes, and heavy metal compounds. Process consists in liquid extraction of undesired components with two mutually immiscible solvents: polar N-methylpyrrolidone with 3-5% water at 40-60°C and nonpolar n-undecane or undecane fraction forming azeotropic mixtures with N-methylpyrrolidone having minimal boiling temperature (about 179°C). Weight ratio of nonpolar solvent to raw material is (0.4-0.5):1.

EFFECT: increased selectivity of process in reduced risk of thermooxidative and hydrolytic decomposition of N-methylpyrrolidone as well as corrosion of equipment.

1 dwg, 4 tbl, 4 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: lube fractions are brought into contact with N-methylpyrrolidone in extraction tower according to three-step countercurrent purification scheme to form raffinate and extract solutions. When distillate fraction II (300-400°C) is purified, of sulfoxide is preliminarily added in amount of 0.1-0.5% based on the weight of solvent. Distillate fraction III (350-420°C) is then purified after addition to solvent of 0.5-1.5% of extract obtained from purification of distillate fraction II.

EFFECT: deepened purification of raffinate, increased yield of raffinate as commercial product, and enabled qualified application of extract by-product.

11 tbl, 6 ex

FIELD: oil and gas production.

SUBSTANCE: invention refers to procedure of clarification of oil distillate under effect of magnetic field consisting in clarification of oil distillate with N-methyl-pyrrolidone, also, oil distillate is subjected to effect of constant magnetic field with induction 0.05-0.25 tesla. Force lines of constant magnetic field are directed perpendicular to vector of flow of oil distillate, while linear rate of flow in an active gap of a magnetizator amounts to 0.01-03 m/sec, whereupon oil distillate is mixed with N-methyl-pyrrolidone.

EFFECT: improved quantitative and qualitative indices of finish product, reduced critical temperature of oil distillate dissolving in N-methyl-pyrrolidone and reduced temperature of extraction.

2 cl, 4 ex, 2 tbl

FIELD: oil-and-gas production.

SUBSTANCE: invention relates to method whereby initial hydrotreated diesel fraction is separated by rectification into light and heavy components. Heavy component is subjected to liquid extraction with subsequent regeneration of solvent from refined and extracted solutions and blending of obtained refined product with light component of diesel fraction. Note here that solvent in liquid extraction is N-methylpyrrolidone. Hydrotreated diesel fractions with final boiling point approximating to 300C are used as light component. Hydrotreated diesel fractions with initial boiling point approximating to 260C are used as heavy component. Weight ratio between hydrotreated diesel fraction heavy component and N-methylpyrrolidone varies from 1:0.5 to 1:2. Temperature in liquid extraction is kept varying from 40C to 70C.

EFFECT: better ecological properties.

1 tbl, 2 ex

FIELD: oil-and-gas production.

SUBSTANCE: invention relates to production of diesel fuel. Proposed method comprises oil desalting, extraction of diesel fractions, their mixing and mix hydrofining. In distillation in atmospheric column, two diesel fractions are run off that boil away at 171-341C and 199-360C, 199-360C-fraction is directed to fluid extraction to remove benzalkylthiophens at the stock-to-extragent ratio of 1:1 to 1:4. Note that said extragent represents the product of interaction of organic amine with organic acid, that is amide. Thereafter, fractions 171-341C and 199-360C are mixed after purification in percentage composition of 70-85% and 15-30%, respectively. Note here that said mix at distillation by ASTM D-86 method features dry point of 360C. Produced mix is subjected to hydrofining to get diesel fuel.

EFFECT: diesel fuel with sulfur content not exceeding 10 ppm.

1 tbl, 6 ex

FIELD: oil and gas industry.

SUBSTANCE: task is settled by extraction of nitrogen-containing compounds from hydrocarbon phase into ion fluid (process solution). Process solution represents ion fluid, for example, on the base of alkilimidazol cation and tetrafluoroborate anion or chloride, that contains diluted compounds of transition metals selected from the group including complexes of cobalt (II) and cuprum (I) with 4,5- dicarboxyphtalocianin. Method includes further separation of hydrocarbon fracture from ion fluid and electrochemical regeneration of ion fluid. Ion fluid regeneration is done by electrochemical oxidation of nitrogen-containing compounds.

EFFECT: improvement of hydrocarbon raw materials quality.

3 cl, 1 tbl, 15 ex

FIELD: oil and gas industry.

SUBSTANCE: invention refers to diesel fuel denitration. The invention is related to the method of diesel fuel denitration which includes contact of diesel fuel containing one or several nitrogen-containing compounds with acid ionic liquid at mass ration of diesel fuel and acid ionic liquid equal from 1:0.2 up to 1:2 in at least one extraction zone for selective removal of nitrogenous compounds and production of effluent of denitrated diesel fuel that contains denitrated diesel fuel and acid ionic liquid with nitrogen-containing molecules and extraction of denitrated diesel fuel from effluent of denitrated diesel fuel; at that acid ionic liquid is hydrosulphate butyl methyl imidazoline (BMIMHSO4) or methyl sulphate butyl methyl imidazoline (BMIMCH3SO4).

EFFECT: production of the product with low content of nitrogen.

8 cl, 8 dwg, 7 tbl, 6 ex

FIELD: oil and gas industry.

SUBSTANCE: invention relates to the method of treatment of light hydrocarbon fractions containing sulphureous compounds and carbon dioxide, by means of contact in a counterflow absorber within a single stage with a circulating modified aqueous solution of alkanolamine regenerated to preserve a modifying additive by means of temperature desorption of carbon dioxide and sulphureous compounds. The modifying additive is sodium hydroxide in the amount of 0.005-1%, which after regeneration together with the absorbent is returned into the process. Absorbent supply into the absorber column is carried out by two flows into the upper and medium part of the column, the flow of saturated absorbent is discharged accordingly from the medium and the lower part of the absorber, flows are combined and sent for regeneration into a desorber.

EFFECT: high extent of treatment from carbon dioxide, hydrogen sulfide and other sulphureous compounds.

1 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention is related to oil refining processes, in particular, to production of pollution-free diesel fuel. Invention is referred to the method including division of source straight run diesel into light (fr. 150-315C) and heavy (fr. 315-360C) components with further oxidation of the heavy component by 30% water solution of hydrogen peroxide in presence of acetone as catalyst at temperature of 90C, time of oxidation is 20 minutes and at intensive mixing and extracting oxidation products after water separation by N-methylpyrrolidone with receipt of extraction and raffinate solutions with further regeneration of N-methylpyrrolidone from the above solutions with obtainment of refined oil and its compounding with light component of straight run diesel. The received compound is subjected to hydrofining with production of hydrogenation product being pollution-free diesel fuel.

EFFECT: fuels complying with requirements of Euro-4 and Euro-5 standards with low content of sulphur and polycyclic aromatic hydrocarbons.

2 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of dearomatising a gasoline fraction - pyrolysis material, which involves extraction of aromatic hydrocarbons from a gasoline fraction at 62-180C, obtaining a raffinate with low content of aromatic hyrocarbons, wherein the selective solvent used is a mixture containing 50-65 wt % N-methylpyrrolidone, 30-45% triethylene glycol, 3-7 wt % water.

EFFECT: low content of aromatic hydrocarbons in the gasoline fraction.

1 tbl, 2 ex

Up!