Method of producing high octane gasoline from low-grade gasoline fractions

 

(57) Abstract:

Usage: petrochemistry. Essence: straight-run gasoline fraction of gas condensates, crude oil, stable gas gasoline in contact in the presence of high zeolite catalysts with simultaneous supply of raw materials methanol or pre-heat the raw material is higher than the optimal temperature of transformation on 50 - 150oC. Conduct the rise of the reaction temperature according to the mathematical dependence f(t)=F(j), where t is the temperature in the reactor,oC; j is the duration from the beginning of the cycle reactions, including Dependency is calculated by the formula for the soft-mode: t=A-B^-02j+C^-03j^2-D^j^3, where A, B, C, D are coefficients having values: A - 300 - 400, B - 0,7 - 3,0; C - 50,0 - 10,0; D - 2,0 - 5,0; for hard mode: t=A+Bj+C^-03j^2-D^-04j^ 3, where A Is 300 - 400; B - 0,0 - 2,0; C - 4,0 - 8,0; D - 1,0 is 3.5.

The invention relates to a method of processing light gasoline fractions and may find application in oil refineries and petrochemical plants, as well as enterprises, processing of natural gas.

There is a method of processing low-octane gasoline fractions [1] on which the latter are subjected to deep Hydrotreating and subsequent reforming in the environment of wodorosoda, that catalytic process reformirovania is carried out in the presence of hydrogen-containing gas under a pressure of 1.5 to 4.0 MPa, which is associated with increased fire risk, as well as the need for preliminary Hydrotreating raw materials in connection with the removal of sulfur compounds, which are poisons for platinum reforming catalyst. All this greatly complicates the technology and increases operating costs.

The closest technical solution adopted for the prototype, is a method of processing gasoline fractions [2] in which low-octane light gasoline fraction without any treatment comes in the hollow reactor heated, filled with zeolite-containing catalyst, where at a pressure of 2MPa and a temperature of 320 450oWith proceeds endothermic catalytic process with the redistribution of hydrogen with the formation of hydrocarbon gas and catalyzate. The catalytic reactions on the catalyst surface are deposited coke deposits, which leads to a partial loss of catalyst activity. Therefore, the catalyst is subjected to periodic regeneration. To increase the duration mezhregionalnogo period in the cycle of reaction is URS is carried out depending on the reaction products, and then adjusting the temperature. Gasoline isolated from catalyzate, has high anti-knock properties and match brands of gasoline a-76 and AI-93 national standard.

The disadvantages of this method are considerable delay commands to adjust the temperature in the reactor in the series of reactions due to the time consuming operations of sampling, analysis of samples of products and subsequent adjustments of the temperature regime, which ultimately leads to reduced output and poor quality of the target product, as well as significant energy consumption and increased demands for activities to ensure safe work practices due to heat transfer in the reactor heated.

The aim of the present invention is to increase output, improve the quality of high-octane gasoline and reduced energy consumption.

This objective is achieved in that, during the cycle of the reaction temperature in the area of the catalyst increases according to the mathematical dependences obtained by approximatevalue experimental data. Mathematical dependencies installed for conducting a catalytic process in soft technological mode of obtaining liquid hydrocarbon is ECCA under severe process conditions to form a liquid hydrocarbon product, the corresponding Marche AU-93 state standard for gasoline. The duration of the cycle of reactions at mild operating conditions is 80 120 h, hard 60 80. The reaction products after the reactor is cooled and separated into hydrocarbon gases C1C4gasoline fraction NC-180 200oWith and hydrocarbon fraction, wikipaedia above 180 200oC.

The mathematical dependence of temperature rise in the reaction zone:

f(t)=F(J)

where t is the temperature in the reactor, oC;

J duration from the beginning of the cycle reactions, watch for soft mode:

t=A-B^-02*J+C^-03*J^2-D^-06*J^3,

where t is the temperature in the reactor,oC;

J duration from the beginning of the cycle of reaction, h;

* multiplication symbol;

the symbol for exponentiation;

A, B, C, D coefficients having values:

A=300 400

B=0,8 3,0

C=5,0 10,0

D=2,0 5,0

hard mode:

t=A+B*J+C^-03*J^2-D^-04*J^3,

where t is the temperature in the reactor,oC;

J duration from the beginning of the cycle of reaction, h;

* multiplication symbol;

the symbol for exponentiation;

A, B, C, D coefficients having values:

A=300 400

B=0,0 2,0

C=4,0 8,0

D=1,0 3,5

The process is carried out with simultaneous supply of raw materials in the reactor of methanol and/ingenia catalyst.

As catalysts in this way (without limitation essence of the proposed technical solution) can be used in catalytic systems containing high zeolites in the source and decationizing forms, with a molar ratio of 20 -800 synthesized using organic cations (Quaternary ammonium salts, and Quaternary aromatic amines, aminoalcohols, alcohols and other compounds) and without organic compounds. Zeolites can be modified by cations of metals such as aluminum, iron, zirconium, boron, zinc, copper. The metals may be introduced into the composition of zeolites as ion exchange, and isomorphic substitution of structural silicon or aluminum. The catalyst is prepared by mixing the zeolite with aluminum hydroxide (or other binder) followed by granulation, drying and calcining the obtained granules. The finished catalyst contains 30 to 70 wt. zeolite. The catalyst can be obtained also on the basis of granulated zeolite containing no binders.

Example 1 (the prototype).

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. served in the reactor C gasoline fraction hydrocarbon gases are formed, high-octane gasoline fraction, fraction above 195oWith and coke on the catalyst. Compensatory increase in temperature in the cycle reactions were carried out periodically by sampling, analytical determination of the quality of the samples and subsequent adjustments of the temperature in the reactor. This deviation from the optimal temperature was +5 15% Rel. and the output of gasoline and the quality was in a few cycles: 75 to 80% wt. when 91,5 86 points on THEM or 58 67% at 94 93,2 points on THEM given the quality of gasoline is not less than 93 points octane number by the research method (IM) and not less than 70% wt. output of gasoline.

Example 2.

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. served in the reactor with high catalyst, where at a temperature of 350 450oWith the catalytic process of the gasoline fraction are formed hydrocarbon gases, high-octane gasoline fraction and a coke on the catalyst. At reactor unit installation completed the automation of operations on compensatory rise in temperature in the cycle of the reaction according to the mathematical dependence of the required temperature in zavicaj continuously automatically according to a mathematical formula, for hard mode.

The coefficients of the formula have the following meanings:

A=378,733

B=0,437

C=6,441

D=1,895

This deviation from the optimal temperature was +0,1% and the yield of gasoline and the quality was 72% at 93,05 points on THEM that correspond to the task.

In addition, to improve the compensation of heat in the reaction zone in the reactor serves raw straight-run gasoline fraction and methanol in a weight ratio of raw materials to 1:10. Methanol on the catalyst is converted with the formation of hydrocarbon gases, high-octane gasoline fractions and water. The flow of methanol into the reaction zone compensates andterminal effect of the main process, because the conversion of methanol is an exothermic reaction.

The composition of the catalyst utilized:

Rentgenostrukturnyi analysis of the zeolite pentasil. The content of the binder, of aluminum oxide is 30 wt. The residual sodium oxide is 0.01 wt. the weight ratio of silica to alumina in the zeolite is 90.

Example 3 (prototype).

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. when the initial temperature is a result of the catalytic process of the gasoline fraction hydrocarbon gases are formed, gasoline fraction in the number and 63.4% wt. octane number by the motor method 85 p. and research 93,2 p. the Process is indeterminism, and to maintain a constant temperature at the height of the catalyst layer is heat input to the reactor heat transfer through the wall. The average temperature in the reactor zone was 420oC. the Share of energy costs for compensation of endeffect is 7.6% of all energy consumption in the process.

Example 4.

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. if the initial temperature 420oC and a pressure of 2.0 MPa fed into the reactor where it comes into contact with high catalyst. The catalytic process of the gasoline fraction and the methanol formed hydrocarbon gases, gasoline fraction in the number 76,0% wt. octane on the research method 91,8 p. Supply heat to the reactor heat transfer through the wall was not. The average temperature in the reactor zone was 409oC. the Share of energy costs for compensation of andeffect makes 1.61% of total energy consumption.

Example 5.

A gasoline fraction with a boiling within 40 -145oWith octane which it is in contact with high catalyst. The catalytic process of the gasoline fraction and the methanol formed hydrocarbon gases, gasoline fraction in the amount of 51,3% wt. octane on the research method 93,8 p. Supply heat to the reactor heat transfer through the wall was not. The average temperature in the reactor zone was 445oC. the Share of energy costs for compensation of andeffect amounted to 3.45% of total energy consumption.

Example 6.

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. if the initial temperature 420oC and a pressure of 2.0 MPa fed into the reactor where it comes into contact with high catalyst. The catalytic process of the gasoline fraction and the methanol formed hydrocarbon gases, gasoline fraction in the amount of 78,1% wt. octane on the research method 93,7 p. Supply heat to the reactor heat transfer through the wall was not. The average temperature in the reactor zone was 409oC. the Share of energy costs for compensation of andeffect was 2.30% of all energy consumption.

Additionally, this goal can be achieved technique, which consists in overheating raw cat is alopiidae from superheated raw material in the reaction zone and subsequent submission to the cooled heat transfer to the feedstock in the reaction zone. Moreover, after the heat in the reaction zone the temperature of the raw material is optimal for catalysis.

Example 7.

A gasoline fraction with a boiling within 40 -145oWith having the octane number by the motor method 61 p. heated to a temperature of 520oC at a pressure of 2.0 MPa and serves for heating the reactor heat transfer through the wall, while the heated stream is cooled to 440oWith, then douglasdale in the refrigerator up to 420oSi serves in the reactor zone with high catalyst. The catalytic process of the gasoline fraction are formed hydrocarbon gases, gasoline fraction in the number and 63.4% wt. octane number by the motor method 85 p. and research 93,2 p. the Average temperature in the reactor zone was 420oC. the Share of energy costs for compensation of andeffect amounted to 2.1% of total energy consumption of the process.

The inventive method has been pilot-tested in Groznii.

Sources of information

1. E. C. Smidovich. The technology of oil and gas. M. Chemistry, 1989, ch. II, sec. 194 202.

2. Century, Stepanov and other Gas industry, 1989, 1, S. 54 57.

Method of producing high octane gasoline from low-grade gasoline is emperature and pressure in the presence of high zeolite catalysts using alternating cycles of reaction and regeneration at elevated temperature and pressure with compensation for loss of catalyst activity gradual rise of temperature in the cycle reactions characterized in that the temperature rise in the cycle of the reaction carried out according to the mathematical dependencies

f(t) F(J)

where t is the temperature in the reactor,oC;

J duration from the beginning of the cycle of reaction, h, calculated by the formula for the soft mode

t=A-B-02y+C-03y2-D-06y3,

where t is the temperature in the reactor,oC;

J duration from the beginning of the cycle of reaction, h;

A, B, C, D coefficients having values: A 300 To 400; (B 0,8 - 3,0; C 5,0 10,0; D 2,0 5,0,

for hard mode

t=A+BJ+C-03J2-D-04J3,

where t is the temperature in the reactor,oC;

J duration from the beginning of the cycle of reaction, h;

A, B, C, D coefficients having values for A 300 To 400; (B 0,0 2,0; C 4,0 8,0; D 1,0 3,5,

and the process is carried out with simultaneous supply of raw materials in the reactor of methanol and/or pre-heat the raw material is higher than the optimal temperature of turning 50 150oWith subsequent heat transfer in the zone of a catalyst.

 

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FIELD: petrochemical processes.

SUBSTANCE: high-octane fuels and propane-butane fraction are obtained via conversion of hydrocarbon feedstock on contact with hot catalyst placed in reactor, into which diluting gas is supplied at elevated pressure. Catalyst is Pentasil-type zeolite with general formula xM2/nO,xAl2O3,ySiO2,zMe2/mO wherein M represents hydrogen and/or metal cation, Me group II or VII metal, n is M cation valence, m is Me metal valence, x, y, z are numbers of moles of Al2O3, SiO2, and Me2/mO, respectively, and y/x and y/z ratios lie within a range of 5 to 1000. Metal oxide Me2/mO is formed during calcination, in presence of oxygen, of Me-containing insoluble compound obtained in zeolite reaction mixture.

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11 cl, 4 dwg, 3 tbl, 16 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: hydrocarbon feed is converted in presence of porous catalyst at 250-500°C and pressure not higher than 2.5 MPa, feed uptake being not higher than 10 h-1. Hydrocarbon feed utilized are various-origin hydrocarbon distillates with dry point not higher than 400°C. Catalyst is selected from various aluminosilicate-type zeolites, gallosilicates, galloaluminosilicate, ferrosilicates, ferroaluminosilicates, chromosilicates, and chromoaluminosilicates with different elements incorporated into structure in synthesis stage. Resulting C1-C5-hydrocarbons are separated from gasoline and diesel fuel in separator and passed to second reactor filled with porous catalyst, wherein C1-C5-hydrocarbons are converted into concentrate of aromatic hydrocarbons with summary content of aromatics at least 95 wt %. In other embodiments of invention, products leaving second reactor are separated into gas and high-octane fraction. The latter is combined with straight-run gasoline fraction distilled from initial hydrocarbon feedstock.

EFFECT: increased average production of liquid products.

18 cl, 3 dwg, 9 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: invention relates to catalysts for isomerization of paraffins and alkylation of unsaturated and aromatic hydrocarbons contained in hydrocarbon stock. Catalyst of invention is characterized by that it lowers content of benzene and unsaturated hydrocarbons in gasoline fractions in above isomerization and alkylation process executed in presence of methanol and catalyst based on high-silica ZSM-5-type zeolite containing: 60.0-80.0% of iron-alumino-silicate with ZSM-5-type structure and silica ratio SiO2/Al2O3 = 20-160 and ratio SiO2/Fe2O3 = 30-550; 0.1-10.0% of modifying component selected from at least one of following metal oxides: copper, zinc, nickel, gallium, lanthanum, cerium, and rhenium; 0.5-5.0% of reinforcing additive: boron oxide, phosphorus oxide, or mixture thereof; the rest being alumina. Preparation of catalyst includes following steps: hydrothermal crystallization of reaction mixture at 120-180°C during 1 to 6 days, said reaction mixture being composed of precursors of silica, alumina, iron oxide, alkali metal oxide, hexamethylenediamine, and water; conversion of thus obtained iron-alumino-silicate into H-iron-alumino-silicate; further impregnation of iron-alumino-silicate with modifying metal compound followed by drying operation for 2 to 12 h at 110°C; mixing of dried material with reinforcing additive, with binder; mechanochemical treatment on vibrating mill for 4 to 72 h; molding catalyst paste; drying it for 0.1 to 24 h at 100-110°C; and calcination at 550-600°C for 0.1 to 24 h. Lowering of content of benzene and unsaturated hydrocarbons in gasoline fractions in presence of above catalyst is achieved during isomerization and alkylation of hydrocarbon feedstock carried out at 300-500°C, volumetric feedstock supply rate 2-4 h-1, weight ratio of hydrocarbon feedstock to methanol 1:(0.1-0.3), and pressure 0.1 to 1.5 MPa. In particular, hydrocarbon feedstock utilized is fraction 35-230°C of hydrostabilized liquid products of pyrolysis.

EFFECT: facilitated reduction of benzene and unsaturated hydrocarbons in gasoline fractions and other hydrocarbon fuel mixtures.

3 cl, 1 tbl, 13 ex

FIELD: petrochemical processes.

SUBSTANCE: feedstock is brought into contact with catalyst based on Pentasil family zeolite in at least two zones differing from each other in conditions of conversion of aliphatic hydrocarbons into aromatic hydrocarbons, first in low-temperature conversion zone to covert more active feedstock components to produce aromatic hydrocarbons containing product followed by recovering C5+-hydrocarbons therefrom and, then, contacting the rest of hydrocarbons produced in low-temperature conversion zone with catalyst in high-temperature conversion zone, wherein less active component(s) is converted into aromatic hydrocarbons containing product followed by recovering C5+-hydrocarbons therefrom.

EFFECT: enabled production of aromatic hydrocarbons under optimal conditions from feedstock containing aliphatic C1-C4-hydrocarbons with no necessity of separating the latter.

4 cl, 1 dwg, 1 tbl

FIELD: petrochemical processes.

SUBSTANCE: hydrocarbon feedstock, containing narrow and wide hydrocarbon fractions boiling within a range from boiling point to 205°C and C1-C4-alcohols and/or dimethyl ether, which are blended in a system, to which they are supplied separately (by two pumps) at volume ratio (20.0-90.0):(10-80), respectively, is brought into contact with zeolite-containing catalyst at 380-420°C, pressure 0.2-5.0 MPa, and liquid feedstock volume flow rate 0.5-2.0·h-1, whereupon reaction products are liberated from water produced in the reaction. Above-mentioned zeolite-containing catalyst is comprised of (i) Pentasil-type zeolite with silica ratio (SiO2/Al2O3) 25-100 in amount 65-70% including residual amount of sodium ions equivalent to 0.05-0.1% sodium oxide, (ii) modifiers: zinc oxide (0.5-3.0%), rare-earth element oxides (0.1-3.0%), cobalt oxide (0.05-2.5%) or copper chromite (0.1-0.3%), and (iii) binder: alumina or silica in balancing amount.

EFFECT: increased octane number of gasoline.

2 tbl, 9 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: petrochemical processes and catalysts.

SUBSTANCE: invention provides isodewaxing catalyst for petroleum fractions containing supported platinum and modifiers wherein supporting carrier is fine powdered high-purity alumina mixed with zeolite ZSM 5 in H form having SiO2/Al2O3 molar ratio 25-80 or with zeolite BETA in H form having SiO2/Al2O3 molar ratio 25-40 at following proportions of components, wt %: platinum 0.15-0.60, alumina 58.61-89.43, zeolite 5-40, tungsten oxide (modifier) 1-4, and indium oxide (modifier) 0.24-0.97. Preparation of catalyst comprises preparing carrier using method of competitive impregnation from common solution of platinum-hydrochloric, acetic, and hydrochloric acids followed by drying and calcinations, wherein carrier is prepared by gelation of fine powdered high-purity alumina with the aid of 3-15% nitric acid solution followed by consecutive addition of silicotungstenic acid solution and indium chloride solution, and then zeolite ZSM 5 in H form having SiO2/Al2O3 molar ratio 25-80 or with zeolite BETA in H form having SiO2/Al2O3 molar ratio 25-40.

EFFECT: increased yield of isoparaffin hydrocarbons.

7 cl, 2 tbl, 7 ex

FIELD: CHEMISTRY.

SUBSTANCE: zeolite catalyst for process of conversion of straight-run gasoline to high-octane number component is described. The said catalyst contains high-silica zeolite with SiO2/Al2O3=60 and residual content of Na2О of 0.02 wt.% maximum, metal-modified, Pt, Ni, Zn or Fe metals being in nanopowder form. Content of the said metals in the catalyst is 1.5 wt.% maximum. Method to manufacture zeolite catalyst for conversion of straight-run gasoline to high-octane number component is described. The said method implies metal modification of zeolite, Pt, Ni, Zn or Fe metals being added to zeolite as nanopowders, produced by electric explosion of metal wire in argon, by dry pebble mixing in air at room temperature. Method to convert straight-run gasoline using the said catalyst is also described.

EFFECT: increase in catalyst activity and gasoline octane number, accompanied by increase in yield.

4 cl, 3 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention describes zeolite-containing catalyst for transformation of aliphatic hydrocarbons C2-C12 to a mix of aromatic hydrocarbons or high-octane gasoline component containing zeolite ZSM-5 with silicate module SiO2/Al2O3=60-80 mol/mol and 0.02-0.05 wt % of residual sodium oxide content, zeolite structural element, promoter and binding component, with zirconium or zirconium and nickel oxides as zeolite structural component, and zinc oxide as promoter, at the following component ratio (wt %): zeolite 65.00-80.00; ZrO2 1.59-4.00; NiO 0-1.00; ZnO 0-5.00; Na2O 0.02-0.05, the rest being binding component. Also, a method for obtaining zeolite-containing catalyst is described, which involves mixing reagents, hydrothermal synthesis, flushing, drying and calcinations of sediment. The reaction mix of water solutions of aluminum, zirconium and nickel salts, sodium hydroxide, silicagel and/or aqueous silicate acid, inoculating zeolite crystals with ZSM-5 structure in Na or H-form, and structure-former, such as n-butanol, is placed in an autoclave, where hydrothermal synthesis is performed at 160-190°C for 10-20 hours with continuous stirring; the hydrothermal synthesis over, Na-form pulp of the zeolite is filtered; the obtained sediment is flushed with domestic water and transferred to salt ion exchange by processing by water ammonium chloride solution with heating and stirring of the pulp; the pulp obtained from salt ion exchange is filtered and flushed with demineralised water with residual sodium oxide content of 0.02-0.05 wt % on the basis of dried and calcinated product; flushed sediment of ammonium zeolite form proceeds to zinc promoter introduction and preparation of catalyst mass by mixing of ammonium zeolite form modified by zinc and active aluminum hydroxide; obtained catalyst mass is extruded and granulated; the granules are dried at 100-110°C and calcinated at 550-650°C; calcinated granules of zeolite-containing catalyst are sorted, ready fraction of zeolite-containing catalyst is separated, while the granule fraction under 2.5 mm is milled into homogenous powder and returned to the stage of catalyst mass preparation. The invention also describes method of transformation of aliphatic hydrocarbons to high-octane gasoline component or a mix of aromatic hydrocarbons (variants), involving heating and passing raw material (gasoline oil fraction direct sublimation vapours or gas mix of saturated C2-C4 hydrocarbons) through stationary layer of the aforesaid catalyst.

EFFECT: reduced number of components and synthesis stages of zeolite-containing catalyst; increased transformation degree of raw material; improved quality and yield of target products with the said catalyst.

4 cl, 8 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: invention refers to production method of high-octane gasoline fractions and/or aromatic hydrocarbons C6-C10 as follows, hydrocarbon materials is heated, evaporated and overheated to process temperature, thereafter providing its contact at temperature 320-480°C and excess pressure with periodically recyclable catalyst containing zeolite of composition ZSM-5 or ZSM-11. Then it is cooled. Contact products are partially condensed, separated into gaseous and liquid fractions by separation. Liquid products of separation are supplied as power primarily to the first distillation column for separation of hydrocarbon gases and liquid stable fraction. The latter is supplied to the second distillation column for separation of high-octane gasoline fraction, or aromatic hydrocarbon fraction, and heavy charge fraction. Gaseous fraction resulted from separation of contact products is supplied to the first distillation column, specifically to intermediate section between infeed and external reflux inlet. External reflux is liquid distillate of the first distillation column.

EFFECT: reduction of power inputs, i.e. quantities of heat and cooling agent, required for reaction products separation.

5 cl, 2 ex

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