RU2529680C1 - Normal hydrocarbon cyclisation catalyst and method for production thereof (versions) - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: catalyst comprises a support which is prepared using high-silica zeolite KL and boehmite, and the catalytically active substance is both platinum crystallites immobilised on the surface of the catalyst and platinum particles localised inside the zeolite channel, having size of 0.6-1.2 nm. The boehmite particles have a size of no more than 45 mcm. The zeolite particles have size of no more than 0.2 mm. The ingredients are in the following ratios (wt %): platinum - 0.3-0.8; boehmite - 19.9-59.5; zeolite KL - 79.8-39.7. The catalyst may further include an oxide and/or metal promoter selected from: Sn, In, Ir, Re, Ba. The group of inventions also includes methods of producing catalysts, which include preparing a granular support based on zeolite and aluminium hydroxide and depositing platinum on the support.

EFFECT: improved catalyst.

4 cl, 1 tbl, 6 ex

Description

The group of inventions relates to oil refining and petrochemicals and can be used in the production of normal alkanes cyclization catalysts from both petroleum feedstocks and synthetic hydrocarbons. The cyclization process is one of the most important in the processing of synthetic hydrocarbons due to the very low content of aromatic compounds in the composition of Fischer-Tropsch synthesis products.

In recent decades, the development of fundamentally new catalysts for the aromatization of normal paraffin hydrocarbons containing platinum and zeolite L. Zeolite L belongs to the group of high-silica zeolites and is characterized by the absence of acid centers. The basicity of a carrier containing zeolite L in potassium form (zeolite KL) is a necessary property for the selective aromatization of normal paraffin hydrocarbons. In the channels of zeolite KL as a result of the isomerization reaction, equilibrium is maintained in the mixture of branched, cyclic and normal alkanes.

This is a fundamentally new approach to the creation of a catalyst for the aromatization of normal paraffin hydrocarbons, since the classic alumina-platinum reforming catalyst is bifunctional and is characterized by the presence of metal and acid centers.

An important criterion for the aromatization catalyst is the Pt particle size, which largely determines the occurrence of adverse reactions (mainly hydrogenolysis of alkanes) (P. Meriaudeau, C. Naccache. Catal. Rev. - Sci. Eng. 39, 1997, p.5-48 ) The small particle size of platinum (less than 1-2 nm) in combination with one-dimensional channels of KL zeolite limits the degree of hydrogenolysis of alkanes, increasing the efficiency of the catalytic system.

A known catalyst for the cyclization of normal paraffin hydrocarbons. The catalyst is prepared by introducing platinum into a zeolite containing aluminum, silicon and germanium. The catalyst is activated by sequential treatment with hydrogen, a sulfur compound and re-hydrogen, US 7247593 B2, 07.24.2007.

The disadvantages of the catalyst include the complex activation procedure using sulfur-containing compounds, which makes it inapplicable for the processing of synthetic hydrocarbons, as well as low activity in the process of aromatization of alkanes.

Known platinum catalyst for producing aromatic hydrocarbons, containing as a carrier zeolite or alumina and a modifier, for example germanium, tin, lead, rhenium, gallium, indium or titanium. To prepare the system using the method of impregnation with organometallic compounds. Depending on the composition of the system, both single and multi-stage impregnation of the oxide component is used. In the case of multi-stage impregnation, intermediate calcination is used. As an alternative preparation of the catalyst indicated the introduction of modifiers in the composition of the media at the gel stage before the molding procedure (US 6153090 A1, 11.28.2000).

The disadvantage of the proposed method for the preparation of the catalyst is the complexity of its preparation and high cracking activity.

A known catalyst for aromatization of a gasoline fraction containing platinum, tin and zeolite L. The catalyst carrier is a type L zeolite molded with a binder (preferably in the form of KL). As a modifier, tin is used, which is introduced into the catalyst composition by impregnation with a solution of the corresponding halide (chloride or fluoride). Before the activation step, the catalyst is subjected to oxidative heat treatment. Carried out in the presence of this catalyst, the process of aromatization of the gasoline fraction allows to obtain aromatic hydrocarbons with high yield and selectivity.

The disadvantages of this catalyst include the complex stage of activation, the low degree of conversion of raw materials into aromatic products, as well as the low working pressure (100-300 kPa) required for the effective implementation of the process. Under the conditions of the industrial cyclization process at low pressures (below 1 MPa), the risk of system deactivation due to coke formation is significantly increased (US 6117601, 2001).

Closest to the proposed group of inventions is a catalyst for the aromatization of a hydrocarbon mixture enriched in normal C ₆ -C ₇ alkanes, and a method for producing it. The catalyst contains platinum and a zeolite-containing support based on industrial zeolite L (Tosoh, Ltd, Japan). The carrier is prepared by mixing powders of zeolite L and a binder, followed by extrusion. The resulting extrudates are dried and calcined, treated with a solution of the corresponding halide (chloride and / or fluoride), dried and calcined. Before the introduction of the active component, the carrier is subjected to repeated washing with distilled water. Platinum is introduced from a solution of platinum tetraammonium chloride, followed by drying. The method involves the introduction of a promoter in the preparation of a carrier with intermediate calcination before the introduction of platinum (US 6190539 B1, 02.20.2001.

A disadvantage of the known catalyst and the method of its preparation is low catalytic activity, and the content of aromatic hydrocarbons in the product C ₅₊ is 46.5-48.5 wt.%.

The technical task of the proposed group of inventions is the development of a catalyst for the cyclization of normal paraffin hydrocarbons with increased activity and selectivity in relation to the formation of aromatic hydrocarbons and the method for its production (options).

The technical result from the implementation of the proposed group of inventions is to increase the catalytic activity of the catalyst, which reduces the degree of hydrogenolysis, increasing the yield and selectivity for the target product.

The technical result of the catalyst is achieved in that the carrier as a binder contains boehmite with a particle size of not more than 45 microns, high-silica zeolite KL with a particle size of not more than 0.2 mm, platinum with a particle size of 0.6-1.2 nm, while the ratio of ingredients is in the following ranges, wt.%:

Platinum 0.3-0.8 Boehmite 19.9-59.5 Zeolite KL 79.8-39.7

The technical result of the catalyst (option) is achieved in that the carrier as a binder contains boehmite with a particle size of not more than 45 microns, high-silica zeolite KL with a particle size of not more than 0.2 mm, platinum with a particle size of 0.6-1.2 nm and the promoter is selected from metals: Sn, In, Ir, Re, Ba, while the ratio of ingredients is in the following ranges, wt.%:

Platinum 0.3-0.8 Boehmite 19.92-58.6 Zeolite KL 79.73-39.1 Promoter 0.05-1.5

The technical result of the method is achieved in that boehmite with a particle size of not more than 45 microns is used as a binder, the carrier is prepared by mixing high-silica zeolite KL powder with a particle size of not more than 0.2 mm and fine boehmite powder, the mixture is moistened and peptized 5-15 % solution of nitric acid, stirring until a homogeneous mass is obtained, which is granulated by extrusion, the granules are dried and calcined, and platinum with a particle size of 0.6-1.2 nm is applied from an aqueous solution of platinum tetraammonia a platinum concentration 1.5-5.0 mg / ml.

The technical result by the method (option) is achieved by using boehmite with a particle size of not more than 45 microns as a binder, preparing the carrier by mixing high-silica zeolite KL powder with a particle size of not more than 0.2 mm and finely divided boehmite powder, moisten and peptize the mixture A 5-15% solution of nitric acid, stirring until a homogeneous mass, contribute a promoter selected from: Sn, In, Ir, Re, Ba, in an amount of 0.05-1.5 wt.% From an aqueous solution of the salt of the corresponding metal , the resulting mass is granulated extruded pellets are dried and calcined, and platinum with a particle size of 0.6-1.2 nm is deposited from an aqueous solution with platinum tetraammiakata platinum concentration 1.5-5.0 mg / ml.

Before carrying out the cyclization process of normal paraffin hydrocarbons, the catalysts were reduced with a hydrogen-containing gas at a temperature of 450 ° C.

The efficiency of the catalyst was evaluated in the process of cyclization of normal paraffin hydrocarbons by passing a hydrogen-containing gas and feedstock with a molar ratio of hydrogen to feedstock from 1: 1 to 10: 1 through a fixed catalyst bed loaded into a tubular reactor with a space velocity of 0.5-4 hours ^{- 1} in the temperature range 340-550 ° C under a pressure of 0.1-4 MPa in yield and aromatic hydrocarbon content in the products.

A specific implementation of the method is disclosed in the following examples.

Example 1

The example illustrates the preparation of a platinum catalyst based on a granular zeolite-containing carrier in which commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm is used, as a binder, boehmite with a particle size of not more than 45 microns, platinum with a particle size of 0, 6 nm.

A sample of the catalyst composition, wt.%: Pt - 0.3, high-silica zeolite KL - 79.8, boehmite - 19.9, prepared in the following way.

To obtain a granular support, 8.0 g of powdered high-silica zeolite KL and 2.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 5% solution of HNO ₃ containing 0.0645 ml of HNO ₃ (65%) and 6.2 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass is obtained and extruded on a piston extruder through a 1.5 mm diameter die. The extrudates are kept in air for 6 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 550 ° C. At a temperature of 550 ° C, they stand for 4 hours.

Platinum is introduced by cation exchange from an aqueous solution of [(NH ₃ ) ₄ Pt] Cl ₂ . The complex compound, platinum tetraammonium acetate [Pt (NH ₃ ) ₄ ] Cl _2, is obtained by reacting ammonium hexachloroplatinate (NH ₄ ) ₂ PtCl ₆ with concentrated ammonia solution (25%).

20 ml of a prepared solution with a concentration of platinum of 1.5 mg / ml is added to 10 g of the obtained calcined carrier. The mixture is stirred in a porcelain dish for 10 minutes at room temperature and left in the air for 10 hours, then the excess solution is separated by decantation. Then the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at a temperature of 450 ° C for 3 hours. Cyclization is carried out in a tubular reactor with a stationary catalyst bed at a pressure of 0.1 MPa, a molar ratio of hydrogen to feed 3: 1 and a space velocity of 2 hours ^-1 in the temperature range 340-550 ° C.

Example 2

The example illustrates the preparation of a platinum catalyst based on a granular zeolite-containing carrier in which commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm is used, as a binder, boehmite with a particle size of not more than 45 microns, platinum with a particle size of 0, 8 nm.

A sample of the catalyst composition, wt.%: Pt - 0.5, zeolite KL - 59.7, boehmite - 39.8, prepared in the following way.

To obtain a granular support, 6.0 g of powdered high-silica zeolite KL and 4.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 10% HNO ₃ solution containing 0.129 ml of HNO ₃ (65%) and 6.15 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass is obtained and extruded on a piston extruder through a 1.5 mm diameter die. The extrudates are kept in air for 6-8 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

The temperature is then increased at a rate of 2 ° C / min to 550 ° C. At a temperature of 550 ° C, they stand for 4 hours.

Platinum is introduced according to Example 1. 20 ml of a prepared solution with a concentration of platinum of 2.5 mg / ml is added to 10 g of the obtained carrier. The mixture is stirred in a porcelain cup for 5 minutes at room temperature and left in air for 10 hours, then the excess solution is separated by decantation. After that, the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at a temperature of 450 ° C for 3 hours. Cyclization is carried out in a tubular reactor with a stationary catalyst layer at a pressure of 1 MPa, the molar ratio of hydrogen to feed is 1: 1 and a space velocity of 0.5 h ^-1 in the temperature range 340-550 ° C.

Example 3

An example illustrates the preparation of a platinum catalyst based on a granular zeolite-containing carrier in which commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm is used, as a binder, boehmite with a particle size of not more than 45 microns, platinum with a particle size of 1, 2 nm.

A sample of the catalyst composition, wt.%: Pt - 0.8, zeolite KL - 39.7, boehmite - 59.5, prepared in the following way.

To obtain a granular support, 4.0 g of powdered commercial high-silica zeolite KL and 6.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 15% HNO ₃ solution containing 0.1935 ml of HNO ₃ (65%) and 6.1 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass is obtained and extruded on a piston extruder through a 1.5 mm diameter die. The extrudates are kept in air for 7 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 550 ° C. At a temperature of 550 ° C incubated for 4 hours

Platinum is introduced according to Example 1. 16 ml of a prepared solution with a concentration of platinum of 5.0 mg / ml is added to 10 g of the obtained carrier. The mixture is stirred in a porcelain dish for 10 minutes at room temperature and left in the air for 10 hours, then the excess solution is separated by decantation.

After that, the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at a temperature of 450 ° C for 3 hours. Cyclization is carried out in a tubular reactor with a stationary catalyst bed at a pressure of 2 MPa, a molar ratio of hydrogen to feed 6: 1 and a space velocity of 2 h ^-1 in the temperature range 340-550 ° C.

Example 4

An example illustrates the preparation of a rhenium-promoted platinum catalyst based on a granular zeolite-containing carrier that uses commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm, as a binder, boehmite with a particle size of not more than 45 microns, platinum with a particle size 0.6 nm.

A sample of the catalyst composition, wt.%: Pt - 0.3, Re - 0.05, zeolite KL - 79.73, boehmite - 19.92, prepared in the following way.

To obtain a granular support, 8.0 g of powdered commercial high-silica zeolite KL and 2.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 10% solution of HNO ₃ containing 0.0645 ml of HNO ₃ (65%) and 6.2 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass is obtained and extruded on a piston extruder through a 1.5 mm diameter die. The extrudates are kept in air for 6 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 550 ° C. It is held at 550 ° C for 4 hours. Rhenium is applied from an aqueous HReO ₄ solution in one impregnation (the rhenium content in the solution is 0.25 mg / ml). 20 ml of the solution (in terms of rhenium is 0.05 wt.%) Is added to 10 g of the obtained carrier. The mixture is stirred in a porcelain cup for 8 minutes at room temperature and left in air for 12 hours, then the excess solution is separated by decantation. After that, the catalyst is dried in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 450 ° C. At a temperature of 450 ° C incubated for 4 hours

Platinum is introduced according to Example 1. To a rhenium-promoted sample, 20 ml of a prepared solution with a platinum concentration of 1.5 mg / ml are added. The mixture is stirred in a porcelain cup for 5 minutes at room temperature and left in air for 10 hours, then the excess solution is separated by decantation. After that, the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at a temperature of 450 ° C for 3 hours. Cyclization is carried out in a tubular reactor with a stationary catalyst layer at a pressure of 2 MPa, the molar ratio of hydrogen to feed is 8: 1 and a space velocity of 1.5 h ^-1 in the temperature range 340-550 ° C.

Example 5

An example illustrates the preparation of a platinum catalyst based on a granular zeolite-containing carrier promoted with tin, in which commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm is used as a zeolite, and boehmite with a particle size of not more than 45 μm is used as a binder. platinum with a particle size of 0.6 nm.

A sample of the catalyst composition, wt.%: Pt - 0.3, Sn - 0.1, zeolite KL - 79.7, boehmite - 19.9, prepared in the following way.

To obtain a granular support, 8.0 g of powdered commercial high-silica zeolite KL and 2.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 10% solution of HNO ₃ containing 0.0645 ml of HNO ₃ (65%) and 6.2 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass. Add 2 ml of an aqueous solution containing 0.03 g of SnCl ₄ · 5H ₂ O (in terms of tin is 0.1 mass%), mix thoroughly until a homogeneous mass is obtained and extruded on a piston extruder through a die with a diameter of 1.5 mm. The extrudates are kept in air for 6 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 550 ° C. At a temperature of 550 ° C, incubated for 4 hours

Platinum is introduced according to Example 1. 20 ml of a prepared solution with a concentration of platinum of 1.5 mg / ml is added to 10 g of a tin-promoted carrier. The mixture was stirred in a porcelain dish for 8 min at room temperature and left in air for 11 h, then the excess solution was separated by decantation. After that, the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at 450 ° C for 3 hours. Cyclization is carried out in a tubular reactor with a stationary catalyst layer at a pressure of 3 MPa, a molar ratio of hydrogen to feed 10: 1 and volumetric speeds of 0.5 h ^-1 in the temperature range 340-550 ° C.

Example 6

An example illustrates the preparation of a platinum catalyst based on a granular zeolite-containing carrier promoted with barium, which uses commercial high-silica zeolite KL (Zeolyst) with a particle size of not more than 0.2 mm, as a binder, boehmite with a particle size of not more than 45 microns, platinum with a size particles 1.0 nm.

A sample of the catalyst composition, wt.%: Pt - 0.8, Ba - 1.5, zeolite KL - 39.1, boehmite - 58.6, prepared in the following way.

To obtain a granular support, 4.0 g of powdered commercial high-silica zeolite KL and 6.0 g of boehmite grade Pural SB (SASOL) are placed in a porcelain bowl, mixed thoroughly. A 15% HNO ₃ solution containing 0.1935 ml of HNO ₃ (65%) and 6.1 ml of distilled water was added. The mixture is thoroughly mixed until a homogeneous mass. Add 2 ml of an aqueous solution containing 0.187 g of Ba (OH) ₂ (in terms of barium is 1.5 wt.%), Mix thoroughly until a homogeneous mass and extrude on a piston extruder through a die with a diameter of 1.5 mm. The extrudates are kept in air for 6 hours and crushed to a fraction of 1.5 × 4-5 mm. Then the extrudates are placed in a muffle furnace. The drying mode is stepwise: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours. Next, the temperature is increased at a rate of 2 ° C / min to a temperature of 550 ° C. At a temperature of 550 ° C incubated for 4 hours

Platinum is introduced according to Example 1. 16 ml of a prepared solution with a concentration of platinum of 5.0 mg / ml is added to 10 g of the obtained barium promoted carrier. The mixture is stirred in a porcelain cup for 5 minutes at room temperature and left in the air for 12 hours, then the excess solution is separated by decantation. After that, the catalyst is dried in an electric cabinet. The drying mode is as follows: 60 ° C - 2 hours, 80 ° C - 2 hours, 110 ° C - 2 hours.

The efficiency of the catalyst was evaluated by the yield and content of aromatic hydrocarbons in the products obtained during cyclization of normal paraffin hydrocarbons by passing a hydrogen-containing gas and a model feed - n-alkane - with a molar ratio of hydrogen to feed from 1: 1 to 10: 1 through a fixed catalyst bed loaded into a tubular reactor. Before the process, the catalyst sample is activated in a stream of hydrogen (v = 3000 h ^-1 ) at a temperature of 450 ° C for 3 hours. The tests were carried out at a space velocity of 0.5-4 h ^-1 in the temperature range 340-550 ° C under pressure 0.1-4.0 MPa. As model raw materials, n-hexane or n-octane was used.

The indicators of the cyclization process of n-octane and n-hexane, carried out using samples of the catalysts corresponding to the invention, are presented in the table.

Example Raw materials The content of aromatic hydrocarbons in the product C ₅₊ , wt.% The yield of aromatic hydrocarbons in the product C ₅₊ , wt.% one n-hexane 68.1 38.6 n-octane 62.7 33.5 2 n-octane 72,2 34.3 3 n-octane 64.0 33.0 four n-octane 66.5 42,2 5 n-octane 73,2 39.0 6 n-octane 74.1 39.7

Claims (4)

1. The catalyst for cyclization of normal paraffin hydrocarbons containing a carrier of a porous zeolite KL and a binder, a catalytically active substance is platinum, characterized in that boehmite with a particle size of not more than 45 microns is used as a binder, while the KL zeolite has a particle size of not more than 0 , 2 mm, and platinum has a particle size of 0.6-1.2 nm, and the ratio of ingredients is in the following ranges, wt.%:
Platinum 0.3-0.8 Boehmite 19.9-59.5 Zeolite KL 79.8-39.7 2. The catalyst for cyclization of normal paraffin hydrocarbons containing a carrier of a porous zeolite KL and a binder, a catalytically active substance - platinum and a promoter, characterized in that boehmite with a particle size of not more than 45 microns is used as a binder, while the KL zeolite has a particle size of not more than 0.2 mm, and platinum has a particle size of 0.6-1.2 nm, and the promoter is selected from metals: Sn, In, Ir, Re, Ba and the ratio of ingredients is in the following ranges, wt.%:
Platinum 0.3-0.8 Boehmite 19.92-58.6 Zeolite KL 79.73-39.1 Promoter 0.05-1.5 3. The method for producing a cyclization catalyst for normal paraffin hydrocarbons according to claim 1, comprising preparing a granular support based on porous KL zeolite and a binder, applying an aqueous solution containing a platinum salt to the support by cationic exchange and drying, characterized in that the binder is used boehmite with a particle size of not more than 45 microns, and the preparation of the carrier is carried out by mixing zeolite KL powder with a particle size of not more than 0.2 mm and fine boehmite powder, the mixture is moistened and pept is izoviruyut 5-15% solution of nitric acid, mixing until a homogeneous mass is obtained, which is granulated by extrusion, the obtained granules are dried and calcined, and platinum is applied from an aqueous solution of platinum tetraammonia with a concentration of platinum of 1.5-5.0 mg / ml until particle size of 0.6-1.2 nm. 4. The method of producing a catalyst for cyclization of normal paraffin hydrocarbons according to claim 2, comprising preparing a granular support based on porous KL zeolite, a binder and a promoter, applying an aqueous solution containing a platinum salt to the support by cation exchange and drying, characterized in that as binder using boehmite with a particle size of not more than 45 microns, the preparation of the carrier is carried out by mixing zeolite KL powder with a particle size of not more than 0.2 mm and finely divided boehmite powder, the mixture is moistened ute and peptize with a 5-15% solution of nitric acid, stirring until a homogeneous mass is made, a promoter selected from: Sn, In, Ir, Re, Ba is introduced in an amount of 0.05-1.5 wt.% from an aqueous solution salts of the corresponding metal, the resulting mass is granulated by extrusion, the obtained granules are dried and calcined, and platinum is applied from an aqueous solution of platinum tetraammonium with a concentration of platinum of 1.5-5.0 mg / ml until a particle size of 0.6-1.2 nm is reached.