Petroleum fraction isodewaxing catalyst and a method for preparation thereof

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

 

The technical field to which the invention relates.

The invention relates to catalytic chemistry, more specifically to the catalysts isodewaxing oil, in particular, diesel and oil fractions, as well as to a method of its preparation and can be used in the oil industry.

The level of technology

Known catalysts for the isomerization of normal paraffin hydrocarbons containing the VIII group metals (Pt, Pd)deposited on γ-Al2O3(US patent 20050000857) or media containing silicon oxide (Patent US 20030017937).

The closest to the proposed invention is a catalyst for the isomerization of normal paraffin hydrocarbons containing platinum deposited on a zeolite-containing carrier of the modified indium oxide of aluminum, and the method of its preparation. This method includes obtaining aminoarabinose media containing 10-50 wt.% zeolite computers in MIS-shaped and modified indium (0.05 to 1.0 wt.%). Indium is made from hydrochloric acid solution oxycarbonate India at the stage of peptization of aluminum hydroxide or in the form of suspension of oxycarbonate India in patinirovannuyu weight of aluminum hydroxide. Molded by extrusion calcined zeolite aminoalkenes media, modified indium, is impregnated with a solution pay hloristovodorodnykh acid in the presence of competitor (RF Patent 2162012, 1999).

A disadvantage of the known catalysts is the high content of silicon oxide, increase the acidity of the medium, which leads to an increase in the activity of the catalyst in the reactions of hydroisomerization, and hydrocracking reactions. As a result of high activity of the catalysts in the hydrocracking reactions the yield of the target product (isoparaffin hydrocarbons) on these catalysts does not exceed 75 wt.%.

The invention

The present invention is to develop a catalyst isodewaxing of oil fractions with high activity in reactions of isomerization of normal paraffin hydrocarbons contained in the composition of diesel and oil fractions, and the method of its preparation.

In accordance with the task one object of the invention is a catalyst isodewaxing oil fractions containing platinum and modifiers on the media, including finely dispersed powder aluminum oxide of high purity mixed with the zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3equal 25-80, or zeolite BETA in H-form with a molar ratio of SiO2/Al2O3equal to 25-40, in the following ratio, wt.%:

Platinum (Pt)0,1-0,60
Aluminum oxide (Al2About3)58,61-89,43
Zeolite ZSM-5 or BETA in H-form5-40
Modifiers
tungsten1-4
the indium oxideof 0.24 to 0.97.

In the particular case of carrying out the invention, the content of impurities in the used superfine powdered aluminum oxide is not more than 1500 ppm (part./million), while it has a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/year

The technical result of the proposed invention is increased isomerizing activity of the catalyst, which allows to significantly increase the yield of the target product - isoparaffin hydrocarbons. This technical result is achieved due to the use of the ratio of components in the catalyst, as well as the use of aluminum oxide of high purity.

Another object of the invention is a method of preparation of the catalyst isodewaxing oil fractions, which includes obtaining the media, drawing on media platinum by the method of competitive impregnation of the joint solution of hexachloroplatinic, acetic and hydrochloric acids, subsequent drying and calcination, and the media get what melirovanie fine powdery aluminum hydroxide of high purity by 3-15%aqueous solution of nitric acid, followed by the introduction of a solution cremaboldrini acid, then a solution of sodium chloride India and the addition of zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3equal 25-80, or zeolite BETA in H-form with a molar ratio of SiO2/Al2O3equal to 25-40.

Preferably, the gelation powder of aluminum hydroxide to exercise at a temperature of 5-10°and With stirring.

In the particular case of the method using fine powdery aluminum hydroxide of high purity, which is characterized by the content of impurities is preferably not more than 1500 ppm, with a particle size of preferably not more than 100 μm and a specific surface area of preferably not less than 260 m2/year

The technical result of the invention is significantly higher isomerizing activity of the catalysts prepared by the proposed method. Thus, the output of Arctic diesel fuel catalysts corresponding to the invention, when the hydrogen pressure of 3.5 MPa, in the temperature range of 280-340°With not less than 85 wt.%. This technical result is achieved in the proposed method through the use of fine powder of aluminum hydroxide of high purity, stages of gelation of aluminum hydroxide 3-15%solution of nitric acid, modifications consistently solution and cremaboldrini acid and chloride India, add zeolite ZSM-5 (or BETA) in H-form with a molar ratio of SiO2/Al2O3equal 25-80 (or respectively 25-40).

Information confirming the possibility of carrying out the invention

The method of preparation of the catalyst is that highly dispersed powder aluminum oxide of high purity, the impurities content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, moisturize first, then heliroute 3-15%solution of nitric acid at a temperature of 5-10°With, in the mixed mass is injected solution cremaboldrini acid, then the solution of chloride India, and then in a jelly-like mass of the modified aluminum hydroxide under continuous stirring, 5-40 wt.% zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2About3equal 25-80, or zeolite BETA in H-form with a molar ratio of SiO2/Al2About3equal to 25-40. The resulting carrier formed into pellets, dried, calcined and impregnated with a joint solution of hexachloroplatinic acid, acetic and hydrochloric acids.

The invention is illustrated by the following examples.

Example 1.

76,92 g of powdery aluminum oxide, impurity content of the metal oxide which does not exceed 1500 ppm,with a particle size of not more than 100 μm and a specific surface area of not less than 260 m 2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 3%solution of nitric acid at a temperature of 5°C. After stirring add in the mass of 10 ml of an aqueous solution containing 1,21 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 0,256 g chloride India.

42,36 g of powder of zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2About3=25 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules of the carrier is dried at room temperature for 24 h, then dried in a stream of air for 2 h at 60°C, 2 h at 80°C and 2 h at 120°C. the Dried granules media then calcined in air flow at 550°C for 3 h with the rise of temperature of calcination 50°With in the hour.

of 99.85 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 315 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

Impregnation of the carrier is carried out at room temperature for 1 h, and then at a temperature of 80°C for 3 h in post what annum stirring. The excess impregnating solution is separated by decantation.

The resulting catalyst is dried in a stream of air for 2 h at 60°C, 2 h at 80°C, 2 h at 100°C, 2 h at 120°C and 2 h at 140°C.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,15
Aluminum oxide (Al2About3)58,61
Zeolite ZSM-5 in the H form with a molar40,00
the ratio of SiO2/Al2O3=25
Tungsten1,00
The indium oxide0,24.

Example 2.

100,38 g of powder of aluminum hydroxide, the impurity content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 6%solution of nitric acid at a temperature of 7.5°C. After stirring add in the mass of 10 ml of an aqueous solution containing 3.03 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 0.64 g of chloride India.

21,18 g of powder of zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3=50 first moistened with distilled water, and then we use the t in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

a 99.6 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 841 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,40
Aluminum oxide (Al2About3)76,49
Zeolite ZSM in the protonated form with a molar20,00
the ratio of SiO2/Al2O3=50
Tungsten2,50
The indium oxide0,61.

Example 3.

117,36 g of powder of aluminum hydroxide, the impurity content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 3%solution of nitric acid at a temperature of 10�B0; C. After stirring add in the mass of 10 ml of an aqueous solution containing 4.83 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 4.83 g chloride India.

5.30 g of powder of zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3=80 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

with 99.4 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 1261 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,06
Aluminum oxide (Al2About3)89,43
Zeolite ZSM in the protonated form with a molar5,00
the ratio of SiO2/Al2O3=80
Tungsten4,00
Oxide indie is 0,97.

Example 4.

76,92 g of powder of aluminum hydroxide, the impurity content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 15%solution of nitric acid at a temperature of 5°C. After stirring add in the mass of 10 ml of an aqueous solution containing 1,21 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 0,256 g chloride India.

45,98 g of powder of zeolite BETA in H-form with a molar ratio of SiO2/Al2O3=25 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

of 99.85 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 315 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,15Aluminum oxide (Al2O3)58,61Zeolite BETA in H-form with a molar40.00the ratio of SiO2/Al2O3=80 Tungsten1,00The indium oxide0,24.

Example 5.

100,38 g of powder of aluminum hydroxide, the impurity content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 6%solution of nitric acid at a temperature of 7.5°C. After stirring add in the mass of 10 ml of an aqueous solution containing 3.03 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 0.64 g of chloride India.

22,99 g of powder of zeolite BETA in H-form with a molar ratio of SiO2/Al2O3=30 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

a 99.6 g of calcined carrier vacuum within 30 mi is, and then placed in a 150 ml joint impregnating solution containing 841 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum(Pt)0,40
Aluminum oxide (Al2About3)76,49
Zeolite BETA in H-form with a molar20,00
the ratio of SiO2/Al2O3=30
Tungsten2,50
The indium oxide0,61.

Example 6.

117,36 g of powder of aluminum hydroxide, the impurity content of the metal oxide which does not exceed 1500 ppm, with a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/g, the first moistened with distilled water, and then with vigorous stirring heliroute 3%solution of nitric acid at a temperature of 10°C. After stirring add in the mass of 10 ml of an aqueous solution containing 4.83 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 1,02 g chloride India.

5.75 g of a powder of zeolite BETA in H-form with the molar soothes is of SiO 2/Al2O3=40 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

with 99.4 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 1261 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,60
Aluminum oxide (Al2About3)89,43
Zeolite BETA in H-form with a molar5,00
the ratio of SiO2/Al2O3=40
Tungsten4,00
The indium oxide0,97.

Example 7.

100,38 g of aluminum hydroxide obtained by precipitation aluminate way, the impurity content of which is 2000 ppm (including Fe2About3200 ppm Na2O 200 ppm), while intense is remesiana peptizer 6%solution of nitric acid at a temperature of 7.5° C. After stirring add in the mass of 10 ml of an aqueous solution containing 3.03 g cremaboldrini acid, and then 5 ml of an aqueous solution containing 0.64 g of chloride India.

21,18 g of powder of zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3=50 first moistened with distilled water, and then add in the modified weight of aluminum hydroxide. The resulting mass is thoroughly mixed and formed into cylindrical pellets by extrusion.

Granules media dried, dried and calcined as in example 1.

a 99.6 g of calcined carrier vacuum for 30 min, and then placed in a 150 ml joint impregnating solution containing 841 mg of hexachloroplatinic acid; 1,49 g of 98.5%concentrated acetic acid and 1.38 g of 37%

concentrated hydrochloric acid.

The impregnation of the support and drying of the catalyst is carried out analogously to example 1.

The composition of the obtained catalyst, wt.%:

Platinum (Pt)0,40
Aluminum oxide (Al2O3)76,49
Zeolite ZSM in the protonated form with a molar20,00
the ratio of SiO2/Al2O3=50
Tungsten2,50
The oxide is ndia 0,61.

The catalysts prepared according to examples 1, 2, 3, 5 and 7, were tested for activity in reactions isodewaxing normal paraffin hydrocarbons in the laboratory running the installation under hydrogen pressure at model raw. The composition model of the raw materials shown in table 1. Pour point model raw+3 C. the Conditions and results of tests of the catalysts are presented in table 2. For comparison, table 2 shows the data obtained when the catalyst test the prototype of NCU-610.

Table 1
Component composition model materials
ComponentContent, wt.%
n-hexadecan60,0
n-dodecan20,0
n-octaneto 12.0
n-heptane8,0
Total:100

From table 2 it is seen that in the whole range of investigated temperatures of process catalysts prepared according to examples 1, 2, 3, and 5, higher than the activity of the catalyst corresponding to the prototype, and the catalyst on the basis of less pure aluminium oxide in example 7.

Industrial applicability

Offered is haunted catalysts isodewaxing can be used in the refining industry for the isomerization of normal paraffin hydrocarbons, included in diesel and oil fractions.

1. The catalyst isodewaxing oil fractions containing platinum and modifiers on the media, including superfine powdered aluminum oxide of high purity mixed with the zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3equal 25-80, or zeolite BETA in H-form with a molar ratio of SiO2/Al2O3equal to 25-40 in the following ratio, wt.%:

Platinum (Pt)0,15-0,60
Aluminum oxide (Al2About3)58,61-89,43
Zeolite ZSM-5 or BETA in H-form5-40
Modifiers tungsten1-4
The indium oxideof 0.24 to 0.97

2. The catalyst according to claim 1, characterized in that the powdered aluminum oxide of high purity characterized by a content of impurities of not more than 1500 million-1.

3. The catalyst according to claim 1 or 2 characterized in that the finely dispersed powder aluminum oxide has a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/year

4. The method of preparation of the catalyst according to claim 1, comprising receiving media, drawing on media platinum by the method of competitive impregnation of owls the local solution of hexachloroplatinic, acetic and hydrochloric acids, subsequent drying and calcination, wherein the carrier is produced by gelation fine powdery aluminum hydroxide of high purity by 3-15%aqueous solution of nitric acid, then enter solution cremaboldrini acid and the chloride solution India, then add the zeolite ZSM-5 in the H form with a molar ratio of SiO2/Al2O3equal 25-80, or zeolite BETA in H-form with a molar ratio of SiO2/Al2O3equal to 25-40.

5. The method according to claim 4, characterized in that the powdered aluminum oxide of high purity characterized by a content of impurities of not more than 1500 million-1.

6. The method according to claim 4, characterized in that the highly dispersed powder aluminum oxide has a particle size of not more than 100 μm and a specific surface area of not less than 260 m2/year

7. The method according to claim 4, characterized in that the gelation of powdery aluminum hydroxide is carried out at a temperature of 5-10°and With stirring.



 

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4 cl, 1 dwg, 1 tbl

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3 cl, 1 tbl, 13 ex

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18 cl, 3 dwg, 9 ex

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4 cl, 2 dwg, 7 tbl, 6 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: invention provides paraffin isomerization catalyst containing platinum or palladium and γ-alumina as binding material and zeolite selected from zeolite beta and/or ZSM-5, zeolite beta and/or mordenite, and mesoporous aluminosilicate of the type Al-MCM-41 at following proportions: platinum and/or palladium 0.2-0.3%, zeolite (beta and/or ZSM-5, beta and/or ZSM-12, beta and/or mordenite) 30-60%, mesoporous aluminosilicate 5-20%, and γ-alumina the rest. In another embodiment, catalyst contains composite material BEA/Al-MCM-41, which is mixture of zeolite beta and mesoporous aluminosilicate Al-MCM-41 at following proportions: platinum and/or palladium 0.2-0.3%, composite material BEA/Al-MCM-41 30-60%, zeolite (ZSM-5 or ZSM-12, or mordenite) 0-10%, and γ-alumina the rest.

EFFECT: increased catalyst stability and selectivity with regard to 2,2-dimethylbutane, and reduced catalyst preparation time.

2 cl, 1 tbl, 25 ex

FIELD: organic chemistry, petroleum chemistry, chemical technology.

SUBSTANCE: the parent mixture consisting of preferably from C4-hydrocarbons comprising n-butenes, impurities of isobutene and/or butadienes and, possibly, butanes is subjected for a single or two-fold rectification with preliminary and/or simultaneous, and/or intermediate isomerization of 1-butene to 2-butenes preferably. From the distillate composition hydrocarbons with normal boiling points below -4°C and, possibly, n-butane in a remained flow containing 2-butenes preferably and, possibly, other part of n-butane are removed, and isomerization of 2-butanes to 1-butene is carried out, and 1-butene is isolated as a distillate, possibly, with impurity of n-butane. Invention provides simplifying technology of the process.

EFFECT: improved preparing method.

13 cl, 3 dwg, 2 tbl, 9 ex

FIELD: petrochemical processes.

SUBSTANCE: hydrocarbon feedstock containing at least 1 vol % of at least one 5- or 6-membered cyclic hydrocarbon is subjected to preliminary processing, which consists in that feedstock is brought into contact with catalyst in presence of hydrogen under conditions favorable for selective opening of the cycle of cyclic hydrocarbon followed by isomerization stage wherein preliminarily processed feedstock comes into contact with isomerization catalyst to produce triptane-containing product stream.

EFFECT: increased selectivity of process.

34 cl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to environmentally friendly processes for production of isoalkanes via gas-phase skeletal isomerization of linear alkanes in presence of catalyst. Invention provides catalyst for production of hexane isomers through skeletal isomerization of n-hexane, which catalyst contains sulfurized zirconium-aluminum dioxide supplemented by platinum and has concentration of Lewis acid sites on its surface 220-250 μmole/g. Catalyst is prepared by precipitation of combined zirconium-aluminum hydroxide from zirconium and aluminum nitrates followed by deposition of sulfate and calcination in air flow before further treatment with platinum salts. Hexane isomer production process in presence of above-defined cat is also described.

EFFECT: increased catalyst activity.

5 cl, 2 tbl, 6 ex

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

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°С, 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

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention relates to a method for preparing spherical supported metal catalysts with metal content from 10 to 70%, to spherical metal catalyst, to a process of hydrogenation of aromatic compounds wherein the latter are hydrogenised using spherical metal catalyst, and to a process of hydrogenation of aromatic compounds wherein the latter are hydrogenised using spherical supported metal catalyst.

EFFECT: increased activity and selectivity of catalyst having high porosity and uniform pore size distribution.

13 cl, 5 tbl, 12 ex

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