Catalyst and a method for conversion of hydrocarbon feedstock containing paraffins with 4-24 carbon atoms

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention provides catalyst composed of heteropolyacid: phosphorotungstic acid and/or phosphoromolybdenic acid, at least one precious metal deposited on essentially inert inorganic amorphous or crystalline carrier selected from group including titanium dioxide, zirconium dioxide, aluminum oxide, and silicon carbide, which catalyst retains characteristic structure of heteropolyacid confirmed by oscillation frequencies of the order 985 and 1008 cm-1 recorded with the aid of laser combination scattering spectroscopy and which has specific surface area larger than 15 m2/g, from which surface area in pores 15 Å in diameter is excluded. Method of converting hydrocarbon feedstock containing C4-C24-paraffins in presence of above-defined catalyst is likewise described.

EFFECT: increased catalyst selectivity and enhanced hydrocarbon feedstock conversion.

5 cl, 7 tbl, 7 ex

 

The present invention relates to a process for the conversion of hydrocarbons, in particular to a catalyst and method of converting a hydrocarbon feedstock containing paraffins with 4-24 carbon atoms.

As an example, the conversion of hydrocarbons containing 4-24 carbon atoms, may be mentioned the isomerization of saturated hydrocarbons, which is widely used for chemical processing of oil, used mainly to increase the octane number fraction of alkanes having 5-6 carbon atoms in the refined products of crude oil. It is also used, for example, in the preparation of industrial raw materials for alkylation, for example, isomerization of butane, when obespylivanii lubricating oils, or a decrease in the boiling point or temperature fluidity loss diesel fraction.

A known catalyst for hydrocarbon processing, which is a complex of boron TRIFLUORIDE and heteropolysaccharide received from one or more oxides of elements of the III, IV, V, VI groups and one or more metal salts with the General formula (IU)x(XO4)y, where Me is the metal III, IV groups, x=1-2, y=2-3, X is sulfur or phosphorus, taken in molar ratio of oxides, salts of 0.5-20, preferably 1.5 to 10, or from compounds that form when preparing heteropolysaccharide these oxides and salts, on Esenia on a porous carrier, preferably the carbon media containing 0.1-10 wt.% metal of group VIII (see EN 2142931 S1). When using a known catalyst for the isomerization of saturated hydrocarbons conversion and selectivity are insufficient.

The closest analogue of the invention is a catalyst for the conversion of wax hydrocarbons, particularly for the isomerization of paraffins, representing phosphonoformate acid and platinum on the zirconium hydroxide or silicon dioxide as a carrier (see EP 623386 A2). Known catalyst provides maximum conversion of about 60% at a temperature of 240°With (see table 4. EP 623386 A2).

The present invention is highly effective catalyst for the conversion of hydrocarbon feedstock containing paraffins with 4-24 carbon atoms.

The task to solve the proposed catalyst for the conversion of hydrocarbon feedstock containing paraffins with 4-24 carbon atoms, which is heteroalicyclic - phosphomevalonate acid and/or phosphomolybdenum acid, at least one noble metal deposited on an essentially inert inorganic amorphous or crystalline medium selected from the group comprising titanium dioxide, zirconium dioxide, aluminium oxide, silicon carbide keeps the speaker characteristic structure heteroalicyclic, as evidenced by the frequency of oscillation of about 985 and 1008 cm-1registered using laser Raman spectroscopy, and which has a surface area of more than 15 m2/g with the exception of surface area in pores with a diameter of less than 15Å.

As the noble metal, the proposed catalyst contains a metal of group VIII of the Periodic system of elements, preferably contains platinum and/or palladium.

An additional object of the invention is a method of converting a hydrocarbon feedstock containing paraffins with 4-24 carbon atoms, by contacting the feedstock at reaction conditions which are effective for the conversion of raw materials and a catalyst, which is heteroalicyclic - phosphomevalonate acid and/or phosphomolybdenum acid, at least one noble metal deposited on an essentially inert inorganic amorphous or crystalline medium selected from the group comprising titanium dioxide, zirconium dioxide, aluminium oxide, silicon carbide, preserving the characteristic structure of heteroalicyclic, as evidenced by the frequency of oscillation of about 985 and 1008 cm-1registered using laser Raman spectroscopy, and which has a surface area of more than 15 m2/the exception of the surface area in pores with a diameter of less than 15Å .

A noble metal of group VIII of the Periodic system of elements applied to the surface of the catalyst so that the degree of dispersion was as high as possible. For the manufacture of the catalyst can be used in a variety of chemical compounds, such as chlorides, nitrates, iodides, acetylacetonates, acetates, complexes containing ammonia, or platinochloride acid. Such metal may be introduced using standard methods, for example cationic exchange saturation when the source of moisture exchange in the solid phase or chemical deposition from the vapor phase co-deposition and joint saturation. The content of the metal of group VIII of the Periodic system of the elements in accordance with the present invention may preferably be about 0.01 to 30 wt.%, more preferably about 0.05-5 wt.%, in particular about 0.1 to 1.0 wt.% from the total mass of the catalyst.

The above oxides, are suitable as the material of the carrier, have a low concentration of basic sites and do not react with supported heteroalicyclic, thus preserving the structure of the acid and intact. Standard and preferred examples of such carriers are chemical compounds of titanium dioxide and zirconium dioxide with a high developed surface.

Heteroalicyclic may be applied to the carrier by any known method, including the saturation of the aqueous and non-aqueous solutions. The content of heteroalicyclic on the media may vary from 1 to 50%. The preferred content is from 5 to 30%, more preferred from 10 to 25%.

Preferred treatment of the catalyst precursor containing heteroalicyclic, put on essentially inert carrier, provides for the calcination in a stream of air, oxygen, nitrogen or inert gas at a temperature in the range of 200-600°and preferably in the range of 350-500°C. the Final catalyst containing a noble metal, activate the flow of air, nitrogen or inert gas at a temperature in the range of 200-600°and preferably in the range of 350-500°C. the Catalyst may be recovered in a stream of hydrogen at a temperature of 100-500°or it can be used without prior recovery.

Isomerization is aimed at obtaining a branched isomer for various purposes, for example, to increase the octane number, such as light naphtha, reduce the viscosity of long-chain saturated hydrocarbons, reduce the temperature of the higher boiling saturated hydrocarbons or to obtain branched isomers as industrial with the earth with the total amount for further processing. Isomerization of saturated hydrocarbons, as a rule, is carried out in a continuous flow or batch reactor, the catalyst and preferably in the presence of hydrogen. The reaction temperature may vary in the range 100-450°C. Can also be used temperature is outside the specified range, although they are less preferred. The most preferred temperature for the isomerization of light naphtha is the temperature range 100-250°C. the Pressure of the reaction typically is between 1 and 40 bar. The preferred pressure is the pressure of 10-20 bar. To increase the selectivity of the products of the isomerization, the stability of the catalyst and to reduce gassing isomerization continue in the presence of hydrogen. A typical molar ratio of hydrogen : the raw material is from 0.1 to 10, and typically from 0.5 to 2.0. The hydrogen may be diluted with an inert gas such as nitrogen or helium. Hourly space velocity generally ranges from 0.1 to 10 h-1and usually from 0.5 to 3 h-1.

Fed n-saturated hydrocarbons, for example n-butane, n-pentane, n-hexane, n-heptane, n-octane and higher marginal carbon (having 9-16 carbon atoms) or their mixtures are common substances in the isomerization process. Raw materials may contain other hydrocarbons, aromaticheskiye naphthenic hydrocarbons, which do not interfere with the isomerization reactions.

The present invention is illustrated by the following examples.

Example 1

Titanium dioxide (TiO2) modification of anatase (specific surface area of 40.9 m2/g) was used as a carrier to obtain a catalyst corresponding to the present invention containing heteroalicyclic. Heteroalicyclic General formula H3PW12O40(20 wt.%) inflicted on the media TiO2from aqueous solution (0.2 g HPW/ml) by gradual saturation.

Rich media was dried at a temperature of 120°C for two hours and then was progulivali at a temperature of 350°C for four hours in air flow. Pt (0.5 wt.%) applied from a water solution of H2PtCl6by saturating. Thus obtained the final catalyst was dried at a temperature of 120°C for two hours and calcination at a temperature of 350°C for two hours in air flow. The final catalyst was placed in a catalytic reactor and used without prior recovery.

Example 2

The catalyst obtained in accordance with Example 1, was used in the reactor with a fixed bed isomerization of pentane. The reaction was carried out at the total pressure of 0.1 MPa, while the hour space velocity of the liquid was 1 hour-1. Surround with the ratio of hydrogen : hydrocarbon was 3:1. Performance characteristics of the catalyst are shown in Table 1.

Table 1
Temperature, °Conversion, %Selectivity, %
19052,899,0
21070,0for 95.3
23073,184,8

Example 3

The catalyst obtained in accordance with Example 1 was tested in the isomerization of n-hexane. The reaction was carried out at the total pressure of 0.1 MPa, while the hour space velocity of the liquid was 1 hour-1and volume ratio of hydrogen : n-hexane was 4:1. Performance characteristics of the catalyst are shown in Table 2.

Table 2
Temperature, °Conversion, %Selectivity, %
19081,195,6
20083,291,8
21084,487,6

Example 4

Fluorinated sample γ-aluminum oxide (specific surface area 180 m2/g, the fluorine content of 3.5 wt.%) used to obtain a catalyst of 0.5%Pt/20%N3PW12With40/Al2O 3-F in accordance with the procedure described in Example 1. Thus, the resulting catalyst was tested in the isomerization of n-pentane in the conditions described in Example 2. Performance characteristics of the catalyst are shown in Table 3.

Table 3
Temperature, °Conversion, %Selectivity, %
29061,9to 97.1
31064,196,9
33063,5to 97.1

The catalyst obtained in accordance with Example 4, was tested in the isomerization of n-hexane under the conditions described in Example 5. Performance characteristics of the catalyst are shown in Table 4.

Table 4
Temperature, °Conversion, %Selectivity, %
27070,798,3
29075,497,5
31075,696,4

Example 5

0.25 g of Pd(NO3)2was dissolved in 50 ml of water. 3,76 g phospholipases heteroalicyclic was dissolved in 50 ml of water. Both solutions were mixed together to obtain a clear light what about the brown solution. In this solution with constant stirring was administered 7 g of titanium dioxide (type Aerolyst, manufactured by Degussa). Water was evaporated in a rotary evaporator. Thus obtained catalyst was progulivali deposited on aluminum foil with linearly increasing heating rate of 0.3°C/min to a temperature of 350°, soaking at a temperature of 350°C for six hours. Specific surface area of the catalyst was 40 m2/year

The catalyst was tested in a reactor with a fixed bed isomerization of n-hexane. The isomerization reaction was carried out at the total pressure of 0.3 MPa, while the hour space velocity of the liquid was 1.5 h-1. The volume ratio of hydrogen : hydrocarbon was 6:1. Performance characteristics of the catalyst are given in Table 5.

Table 5
Temperature, °Conversion, %Selectivity, %
19067,199,2
20077,898,4
22083,6a 94.2

Example 6

0.25 g of Pd(NO3)2was dissolved in 50 ml of water. 3,76 g phospholipases heteroalicyclic was dissolved in 50 ml of water. Both solutions were mixed together to obtain transparent the th light brown solution. In this solution with constant stirring was administered 7 g of silicon carbide. Water was evaporated in a rotary evaporator. Thus obtained catalyst was progulivali in air flow with a linearly increasing heating rate of 0.3°C/min to a temperature of 350°, soaking at a temperature of 350°C for six hours. Specific surface area of the catalyst was 25 m2/year

The catalyst was tested in a reactor with a fixed bed isomerization of n-hexane. The reaction was carried out at the total pressure of 0.3 MPa, while the hour space velocity of the liquid was 1.5 h-1. The volume ratio of hydrogen:hydrocarbon was 6:1. Performance characteristics of the catalyst are shown in Table 6.

Table 6
Temperature, °Conversion, %Selectivity, %
23077,095,6

Example 7

The Zirconia was obtained by precipitation of ZrOCl2using ammonia in aqueous solution. After filtration, the obtained substance was progulivali at a temperature of 300°C for three hours. 0.75 g of Pd(acac)2was dissolved in 90 ml of ethanol. 11,28 g phosphomolybdenum acid as heteroalicyclic was dissolved in 90 ml of ethanol. Both solutions were mixed together which they were received light, transparent solution. Of 27.4 g of this solution was administered 3 g of Zirconia. After evaporation of the ethanol in a rotary evaporator of the thus obtained catalyst was formed into granules with a size of 0.3-0.7 mm and progulivali in air flow with a linearly increasing heating rate of 0.3°C/min to a temperature of 350°C for eight hours, followed by exposure at a temperature of 350°within six hours.

The catalyst used in the reactor with a fixed bed for the isomerization of n-hexane. The reaction was carried out at the total pressure of 0.3 MPa, while the hour space velocity of the liquid was 1.5 h-1. The volume ratio of hydrogen : hydrocarbon was 6:1. Performance characteristics of the catalyst are shown in Table 7.

Table 7
Temperature, °Conversion, %Selectivity, %
20577,4the 98.9

1. The catalyst for the conversion of hydrocarbon feedstock containing paraffins with 4-24 carbon atoms, which is heteroalicyclic - phosphorus-tungsten acid and/or phosphorus molybdenum acid, at least one noble metal deposited on an essentially inert inorganic amorphous or crystalline media, select the config from the group including titanium dioxide, zirconium dioxide, aluminium oxide, silicon carbide, preserving the characteristic structure of heteroalicyclic, as evidenced by the frequency of oscillation of about 985 and 1008 cm-1registered using laser Raman spectroscopy, and which has a surface area of more than 15 m2/g with the exception of surface area in pores with a diameter of less than 15Å.

2. The catalyst according to claim 1, characterized in that the noble metal includes platinum and/or palladium.

3. A method of converting a hydrocarbon feedstock containing paraffins with 4-24 carbon atoms, by contacting the feedstock at reaction conditions which are effective for the conversion of raw materials and a catalyst, which is heteroalicyclic - phosphorus-tungsten acid and/or phosphorus molybdenum acid, at least one noble metal deposited on an essentially inert inorganic amorphous or crystalline medium selected from the group comprising titanium dioxide, zirconium dioxide, aluminium oxide, silicon carbide, preserving the characteristic structure of heteroalicyclic, as evidenced by the frequency of oscillation of about 985 and 1008 cm-1registered using laser Raman spectroscopy, and which has a square is the area of a surface of more than 15 m 2/g with the exception of surface area in pores with a diameter of less than 15Å.

4. The method according to claim 3, characterized in that the reaction is carried out at a pressure of 1-60 bar and at a temperature of 100-450°in the presence of hydrogen at a molar ratio of hydrogen: hydrocarbon comprising from 0.1:10 to 10:1.

5. The method according to claim 3 or 4, characterized in that the use of a catalyst containing platinum and/or palladium as the noble metal.



 

Same patents:

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-paraffins and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-paraffins utilizing above-defined catalyst is also described.

EFFECT: lowered isomerization process temperature and pressure and increased productivity of catalyst.

17 cl, 3 tbl, 25 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-butane into isobutane and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-butane into isobutane utilizing above-defined catalyst is also described.

EFFECT: lowered butane isomerization process temperature and pressure and increased productivity of catalyst.

13 cl, 1 tbl, 24 ex

FIELD: production of catalysts.

SUBSTANCE: proposed method is used for production of catalyst containing zeolite and heat-resistant oxide binder at low acidity practically containing no aluminum; proposed method includes the following operations; (a) preparation of mass suitable for extrusion and containing homogeneous mixture of zeolite, water, binder of heat-resistant binder at low acidity which is present as acid sol and aminocompounds; (b) extrusion of mass obtained at stage (a) suitable for extrusion; (c) drying extrudate obtained at stage (b); and (d) calcination of dried extrudate obtained at stage (c).

EFFECT: increased strength of catalyst at high resistance to crushing.

10 cl, 1 tbl, 2 ex

FIELD: petrochemical processes.

SUBSTANCE: pentane-into-isopentane isomerization is carried out on platinum catalyst (IP-62) at 370-395°ะก, pressure 2.302.7 MPa, and hydrogen-to-hydrocarbon molar ratio (0.2-0.8):1, preferably 0.5:1.

EFFECT: enhanced process efficiency and reduced power consumption.

3 dwg, 3 ex

The invention relates to processes and catalysts for medium-temperature isomerization of hydrocarbons

The invention relates to a method of preparation of the catalyst of the isomerization of n-alkanes, in particular the skeletal isomerization of n-butane, and can be used in the petrochemical and refining industries

The invention relates to a mixture of branched primary alcohols from C11to C36and to mix them sulfates, alkoxylated, alkoxylates and carboxylates, which have high washing ability in cold water and good biological degradability

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-paraffins and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-paraffins utilizing above-defined catalyst is also described.

EFFECT: lowered isomerization process temperature and pressure and increased productivity of catalyst.

17 cl, 3 tbl, 25 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-butane into isobutane and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-butane into isobutane utilizing above-defined catalyst is also described.

EFFECT: lowered butane isomerization process temperature and pressure and increased productivity of catalyst.

13 cl, 1 tbl, 24 ex

The invention relates to a method of continuous hydration of ethylene, propylene or mixtures thereof with water in the vapor phase to the corresponding alcohols in the presence of salts heteroalicyclic as a catalyst at a molar ratio of water to olefin passing through the reactor, in the range of 0.1 to 3.0, an average hourly rate of gas supply water/olefin through the catalytic system 0,010 - 0.25 g/min/cm3concentrations of heteroalicyclic 5 to 60 wt.% from the total mass of the catalytic system, at a temperature of 150 - 350oC and a pressure ranging from 1000 to 25000 kPa

The invention relates to a catalyst based on aluminum, which contains, calculated on the weight content of the oxide 2-10 wt.% of cobalt oxide COO, 10-30 wt.% molybdenum oxide of Moo3and 4-10 wt.% oxide of phosphorus P2ABOUT5with a surface area by BET method in the range of 100 - 300 m2/g crushing strength CSH more than 1.4 MPa and an average diameter of pores in the range of 8-11 nm, the volume of pores of diameter greater than 14 nm is less than 0.08 ml/g, volume of pores with a diameter of less than 8 nm is not more than 0.05 ml/g and a volume of pores with a diameter of 8 to 14 nm in the range 0,20 - 0,80 ml/g

The invention relates to catalysts and methods of hydroperiod of crude oil

The invention relates to the refining catalysts, in particular catalysts for Hydrotreating of crude oil

The invention relates to the field of oil refining, in particular, to a method of preparation of the catalyst intended for use in the hydrogenation processes for hydrotreatment of diesel fuel

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-paraffins and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-paraffins utilizing above-defined catalyst is also described.

EFFECT: lowered isomerization process temperature and pressure and increased productivity of catalyst.

17 cl, 3 tbl, 25 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to catalytic methods of isomerizing n-butane into isobutane and provides catalyst constituted by catalytic complex of general formula MexOy*aAn-*bCnXmH2n+2-m, where Me represents group III and IV metal, x=1-2, y=2-3, An- oxygen-containing acid anion, a=0.01-0.2, b=0.01-0.1; CnXmH2n+2-m is polyhalogenated hydrocarbon wherein X is halogen selected from a series including F, Cl, Br, I, or any combination thereof, n=1-10, m=1-22, dispersed on porous carrier with average pore radius at least 500 nm and containing hydrogenation component. Method of preparing this catalyst is also disclosed wherein above-indicated catalytic complex is synthesized from polyhalogenated hydrocarbon CnXmH2n+2-m wherein X, n, and m are defined above, group III and IV metal oxide, and oxygen-containing acid anion, and dispersed on porous carrier with average pore radius at least 500 nm, hydrogenation component being introduced either preliminarily into carrier or together with catalytic complex. Process of isomerizing n-butane into isobutane utilizing above-defined catalyst is also described.

EFFECT: lowered butane isomerization process temperature and pressure and increased productivity of catalyst.

13 cl, 1 tbl, 24 ex

FIELD: exhaust gas neutralization catalysts.

SUBSTANCE: catalyst contains at least one zeolite and additionally at least one oxide carrier selected from alumina, silica, titanium dioxide, and aluminum silicate, and also at least one precious metal selected from platinum, palladium, rhodium, and iridium. The latter are characterized by average oxidation degree below +2.5, average number of metal ligands more than 3, and average number of oxygen ligands less than 3, whereas precious metal atoms are present on zeolites and oxide carriers in the form of crystallites with average particle size 1-6 nm. Catalyst is prepared on an solid cellular element, for which oxide carriers and zeolites are first separately impregnated with precious metal precursors and then calcined in yet wet state by blowing them into gaseous combustion gases at 500-1000°C for 0.1 to 10 sec. Thereafter, common coating dispersion is processed, which is further used to coat solid cellular element. Coating is then dried, calcined, and reduced.

EFFECT: increased catalytic activity, prolonged lifetime of catalyst, and lowered minimum working temperature at which carbon monoxide and hydrocarbons start being catalytically converted.

10 cl, 8 tbl, 11 ex

Up!