The method of cleaning the cracking of gasoline

 

(57) Abstract:

Usage: petrochemistry and oil refining. The inventive mixture of the cracking gasoline with diesel fuel or vacuum gas oil (FR. 248-475°C) in a ratio of 3:7 is subjected to hydrogenation on a catalyst containing 15 to 19 wt.% the tungsten trioxide and 1-5 wt.% dioxide Nickel on alumina, at a temperature of 240-340°C and a pressure of 2.8 to 4 MPa. Effect: improve the quality of the target product - the cracking of gasoline by reducing sulfur and unsaturated compounds. table 2.

The invention relates to the refining and can be used when cleaning the cracking of gasoline from sulfur and unsaturated compounds.

A known method of cleaning gasoline secondary origin by genderaware in pure form on a specialized system at a temperature of 350-420°C, the pressure of 2-7 MPa (Chernozhukov N. And. The technology of oil and gas. O'clock 3. - M., 1966, S. 256-267). The disadvantage of this method is the deposition of a large number of resinous substances on the walls of the equipment.

The closest technical solution to the claimed invention is a method of cleaning the cracking of gasoline from sulfur and unsaturated compounds by Geri lybdenum catalyst at a temperature of 360-400°C the pressure of 3-5 MPa, followed by separation of the target product in a known manner (USSR Author's certificate No. 336994, class C 10 G 23/00, 1969 /prototype/). The disadvantage of this method is the high content of sulfur and unsaturated compounds hydrotreated in the cracking gasoline - target product.

An object of the invention is to improve the quality of the target product by reducing sulfur and unsaturated compounds.

The invention consists in that in the known method of cleaning the cracking of gasoline from sulfur and unsaturated compounds by hydrogenation of a mixture of the cracking gasoline with diesel fuel or vacuum gas oil in a ratio of 3:7 on the catalyst at elevated temperature and pressure followed by separation of the target product in a known manner according to the invention, the hydrogenation is conducted on the catalyst, containing from 15 to 19 wt.% the tungsten trioxide and 1-5 wt.% dioxide Nickel on alumina, at a temperature of 240-340°C and a pressure of 2.8 to 4 MPa.

The method is carried out as follows. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil with diesel fuel (FR. the containing 15-19 wt.% trioxide of Wolfram and 1-5 wt.% dioxide Nickel on alumina at a temperature of 240-340°C and a pressure of 2.8 to 4 MPa, space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The product of hydrogenation (hydrogenation product) is subjected to distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 55 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 84 wt.% commercial gasoline with an octane rating of 85 by the motor method without TPP. The heavy fraction of the hydrogenated feed is separated depending on their boiling temperature is used as a commodity product as diesel fuel or as a feedstock for the catalytic cracking of vacuum gasoil.

The content of sulfur and unsaturated compounds in the target product is 0.01-0.02 wt.% and 0.2-0.4 wt.% respectively, against 0.1 to 0.15 wt.% and 1.5-2 wt.% (known way).

The distinctive feature of the method lies in the hydrogenation of a mixture of the cracking gasoline with diesel fuel or vacuum gas oil in a ratio of 3:7 on a catalyst containing 15 to 19 wt.% the tungsten trioxide and 1-5 wt.% dioxide Nickel on alumina, at a temperature of 240-340°C and a pressure of 2.8 to 4 MPa.

Examples of carrying out the invention

P is sulphur and high-sulphur crude oil with diesel fuel (FR. 200-350°C) in a ratio of 3:7 is subjected to hydrogenation on a catalyst content of 15 wt.% the tungsten trioxide and 5 wt.% dioxide Nickel on alumina, at a temperature of 240°C and a pressure of 2.8 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The product of hydrogenation (hydrogenation product) is subjected to distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 55 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 84 wt.% commercial gasoline with an octane rating of 85 by the motor method without TPP. Heavy fraction of the hydrogenated feed is separated is used as a commodity product - diesel fuel that contains no more than 0.2 wt.% sulfur and has a cetane number of 48.

The content of sulfur and unsaturated compounds in the target product is 0.01 and 0.2 wt.% respectively, against 0.1 to 0.15 and 1.5-2 wt.% (known way).

The data quality of the feedstock and the products obtained are shown in table 1. In the following examples use the cracking gasoline process for thermal cracking of n coking of heavy residues sulfur and sour NEA hydrogenation of the mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil with diesel fuel (FR. 200-350°C) or vacuum gas oil (FR. 248-475°C) in the ratio 3:7 use the specified catalyst containing tungsten trioxide and dioxide Nickel on aluminum oxide.

Example 2. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil and vacuum gas oil (FR. 248-475°C) in the ratio 3:7, containing 2.7 wt.% sulfur and 14 wt.% unsaturated compounds, is subjected to hydrogenation on a catalyst containing 19 wt.% the tungsten trioxide and 1 wt.% dioxide Nickel on alumina, at a temperature of 340°C and a pressure of 4 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The hydrogenation product is subjected to fractional distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 55 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 84 wt.% commercial gasoline with an octane rating of 85 by the motor method without TPP. Heavy f is get the catalytic cracking gasoline with an octane rating of 79 by the motor method without TPP.

The sulfur content of the vacuum gas oil does not exceed 0,35 wt.%.

The content of sulfur and unsaturated compounds in the target product are 0.02 and 0.4 wt.% respectively, against 0.1 to 0.15 and 1.5-2 wt.% (known way).

In further examples, a mixture of original cracking gasoline and diesel fuel or a mixture of original cracking gasoline and vacuum gasoil, which are described in examples 1 and 2.

Example 3. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil with diesel fuel (FR. 200-350°C) in a ratio of 3:7 is subjected to the hydrogenation catalyst, the content of 17 wt.% trioxide of tungsten and 3 wt.% dioxide Nickel on alumina, at a temperature of 300°C and a pressure of 3.4 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The hydrogenation product is subjected to fractional distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 55 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 84 wt.% trademarks of gasoline is oduct - diesel fuel, which contains not more than 0.2 wt.% sulfur and has a cetane number of 48.

The content of sulfur and unsaturated compounds in the target product is 0.015 and 0.3 wt.% respectively, against 0.1 to 0.15 and 1.5-2 wt.% (known way).

Example 4. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil and vacuum gas oil (FR. 248-475°C) in a ratio of 3:7 is subjected to hydrogenation on a catalyst containing 18 wt.% the tungsten trioxide and 2.5 wt.% dioxide Nickel on alumina, at a temperature of 310°C and a pressure of 3 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The hydrogenation product is subjected to fractional distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 55 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 84 wt.% commercial gasoline with an octane rating of 85 by the motor method without TPP. Heavy fraction of the hydrogenated feed is cut vacuum gas oil used as feedstock of catalytic cracking unit, you get a Benz is eule does not exceed 0,35 wt.%.

The content of sulfur and unsaturated compounds in the target product is 0,018 and 0.35 wt.% respectively, against 0.1 to 0.15 and 1.5-2 wt.% (known way).

Example 5. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil with diesel fuel (FR. 200-350°C) in a ratio of 3:7 is subjected to hydrogenation on a catalyst with a content of 22 wt.% the tungsten trioxide and 0.2 wt.% dioxide Nickel on alumina, at a temperature of 120°C and a pressure of 0.8 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The hydrogenation product is subjected to fractional distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) octane 54 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with getting 85,3 wt.% commercial gasoline with an octane rating of 82 by the motor method without TPP. Heavy fraction of the hydrogenated feed is separated is used as a component of commercial products - diesel fuel, which contains 0.25 wt.% sulfur and has a cetane number 46.

The content of sulfur and unsaturated compounds in zemer 6. A mixture of the cracking gasoline (FR. N. K. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil and vacuum gas oil (FR.248-475°C) in a ratio of 3:7 is subjected to hydrogenation on a catalyst containing 8 wt.% the tungsten trioxide and 8 wt.% dioxide Nickel on alumina, at a temperature of 440°C and a pressure of 6 MPa, the space velocity of the raw materials 3 h-1, the ratio of hydrogen containing gas to the raw material 500 nm3/m3. The hydrogenation product is subjected to fractional distillation to obtain the desired product is hydrotreated cracking gasoline (FR. N. K. -180°C) with an octane rating of 54.5 by the motor method without TPP, which is subjected to catalytic reforming in polymetallic catalyst with the receipt of 84.8 wt.% commercial gasoline with an octane rating of 83 by the motor method without TPP. Heavy fraction of the hydrogenated feed is separated is used as raw material of the catalytic cracking unit, while having catalytic cracking gasoline with an octane rating of 78 points on the motor method without TPP. The sulfur content of the vacuum gas oil is 0.55 wt.%.

The content of sulfur and unsaturated compounds in the target product is 0.39 and 3.5 wt.% respectively, against 0.1 to 0.15 and 1.5-2 wt.% (and the. -200°C) processes of thermal cracking and coking of heavy residues sulphur and high-sulphur crude oil with diesel fuel (FR. 200-350°C) or vacuum gas oil (FR. 248-475°C) in the ratio 3:7 with catalyst and quality data of the target product and gasoline catalytic reforming; it contains features known method.

From the table 2 data shows that the proposed method can improve the quality of the target product by reducing sulfur and unsaturated compounds.

The present invention can be used in oil refineries fuel directions for cleaning the cracking of gasoline from sulfur and unsaturated compounds.

An additional advantage of the proposed method in comparison with the known method is the increase of output of commodity catalytic reforming of gasoline with an octane rating of 85 points by the motor method without TES 4 wt.% by reducing sulfur and unsaturated compounds hydrotreated in the cracking gasoline and on this basis the possibility of applying for polymetallic catalyst instead of the AP-64 (known way) when reforming FR. N. K. -180°With the hydrogenated feed is cut.

the cracking gasoline with diesel fuel or vacuum gas oil in a ratio of 3:7 on the catalyst at elevated temperature and pressure followed by separation of the target product in a known manner, characterized in that the hydrogenation is conducted on the catalyst, containing from 15 to 19 wt.% the tungsten trioxide and 1-5 wt.% dioxide Nickel on alumina, at a temperature of 240-340°C and a pressure of 2.8 to 4 MPa.



 

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