The catalyst for the conversion of aliphatic hydrocarbons, c2- c12, method thereof and method for the conversion of aliphatic hydrocarbons, c2-c12in high-octane gasoline and/or aromatic hydrocarbons

 

(57) Abstract:

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons2-C12in high-octane gasoline and/or aromatic hydrocarbons. Described is a catalyst for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons, containing by 60.0 to 90.0 wt.% zhelezohromovye with the structure of zeolite ZSM-5 with silicate module SiO2/Al2O3=20-160, SiO2/Fe2ABOUT3=30-5000; modifying additive selected from the group of oxides of copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium in an amount of 0.1-10.0 wt.%, hardening additive is an oxide of boron, phosphorus, or mixtures thereof in an amount of 0.1-5.0 wt.%, binder is alumina rest; and the catalyst formed during the heat treatment at 500-600°C for 0.1 to 24 hours also Described a method of converting aliphatic hydrocarbons2-C12in high-octane gasoline and/or aromatic hydrocarbons. The technical result is an increase in the activity and selectivity of the catalyst, which allows to increase the output of high-octane of gasoline is oversee in the presence of the above catalyst at 300-5500C, flow rate of feed of 0.5 to 5.0 h-1and a pressure of 0.1 to 1.5 MPa. 3 B.C. and 2 C.p. f-crystals, 1 table.

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons, C2-C12in high-octane gasoline and/or aromatic hydrocarbons.

The main industrial process of producing high octane gasoline and/or aromatic hydrocarbons is catalytic reforming of straight-run gasoline fractions, which is held at high temperatures between 450 and 550 C, the high pressure of 0.1 to 3.5 MPa and a hydrogen-containing gas. Disadvantages of the process of catalytic reforming of straight-run gasolines are the use of expensive Pt-containing catalyst, the hydrogen-containing gas.

There is a method of preparation of the catalyst for oligomerization and aromatization of low molecular weight hydrocarbons WITH2-C12containing zeolite family pentasil with silicate module SiO2/Al2ABOUT3=20-80, modified zinc oxide, platinum, and boron oxide, the binder is alumina (U.S. Pat. RU # 2144845, 01 J 29/44, WITH 10 G 35/095, 1998).

The disadvantages of this innovation is mswb reaction conversion of NGL at 600 C.

A known method of producing a catalyst for the conversion of low molecular weight hydrocarbons into high octane gasoline or aromatic hydrocarbons containing zeolite family pentasil with silicate module SiO2/Al2ABOUT3=20-80, modified zinc oxide, platinum and phosphorus oxide, the binder is alumina (U.S. Pat. RU # 2144846, 01 J 29/44, WITH 10 G 35/095, 1998).

The disadvantages of this catalyst are the use of expensive Pt-modifier and a low output to 54.2 wt.% liquid products of the reaction of conversion of NGL at 600 C.

A known method of producing a catalyst for the conversion of aliphatic hydrocarbons, C2-C6in high-octane gasoline or aromatic hydrocarbons containing zeolite family pentasil with silicate module SiO2/Al2O3=20-80, modified zinc oxide, platinum, boron oxide and phosphorus oxide, the binder is alumina (U.S. Pat. RU # 2144847, 01 J 29/44, WITH 10 G 35/095, 1998).

The disadvantages of this catalyst are the use of expensive Pt-modifier and a low output to 43.2 wt.% liquid products of the reaction of conversion of NGL at 600 C.

Known zeolite-containing catalyst for the transformation of elevationstart, containing high-silica group zeolite with a molar ratio of SiO2/Al2O3=20-80 mol/mol and a residual content of sodium oxide is not more than 0.4 wt.%, zinc oxide, gallium mixture of two or more oxides of rare earth elements selected from the group CE, La, Nd, Pr, a binder component, further comprises the oxides of iron (III) and magnesium (U.S. Pat. RU # 2172212, 29/46 01 J, 10 G 35/095, 1999). The composition of the catalyst increases the yield of liquid hydrocarbons FROM5+and the increase in the content of aromatic hydrocarbons.

The disadvantages of this method are the multi-stage cooking, the complex composition of multicomponent catalyst and not a high yield of high octane component of gasoline.

A method of obtaining high zeolites of type ZSM-5 (U.S. Pat. RU # 1527154, 01 33/28, 1987). High zeolites of type ZSM-5 with silicate module SiO2/Al2O3=30-200 get the hydrothermal crystallization of a reaction mixture at 120-180 C for 1-7 days, containing sources of silicon oxide, aluminum oxide, alkali metal oxide, hexamethylenediamine were, and water. The degree of crystallinity of the obtained product 85-100%, the catalytic stability to mechanical grinding to a particle size of 0.1 to 1.0 μm and thermoprotei processing steam at 520 C for 50 h

The disadvantage of the catalyst is not a high yield of liquid products such as high octane gasoline from aliphatic hydrocarbons2-C12.

A known catalyst for the conversion of aliphatic hydrocarbons, C2-C12in a high-octane component of gasoline or a concentrate of aromatic hydrocarbons adopted for the prototype (U.S. Pat. RU # 2165293, 01 J 29/40, WITH 10 G 35/095, 2000). The catalyst contains (wt.%): the group zeolite with a molar ratio of SiO2/Al2ABOUT3=20-150 and the residual content of sodium oxide is not more than 0.4 wt.% - 20,00-90,00; zinc oxide - 0,10-6,00 and/or gallium oxide - 0,10-3,00; mixture of two or more oxides of rare earth elements selected from the group CE, La, Nd, Pr - 0,10-5,00; iron oxide (III) - 0,01-2,00; magnesium oxide 0,01-2,00; calcium oxide - 0,01-2,00; a binder component - the rest.

The disadvantages of the catalyst, taken as a prototype, is a multi-stage cooking, the complex composition of multicomponent catalyst and not a high yield of high octane component of gasoline.

The known method of producing high octane gasoline fractions and aromatic hydrocarbons where the hydrocarbon feedstock, wikipaedia in the temperature range of the boiling point of gasoline is subjected to the including modified elements I, II, III, IV, and VIII groups (U.S. Pat. RU # 2039790, WITH 10 G 35/095, 1993). At the same time in each subsequent zone is subjected to contacting a light gasoline fraction of the previous zone, and heavy gasoline fractions zones mixed with products of last contact zone.

The disadvantages of this method are the multistage and the complexity of the process of producing high octane gasoline fractions and aromatic hydrocarbons.

The known method of producing high octane gasoline fractions and aromatic hydrocarbons (U.S. Pat. RU # 2163624, WITH 10 G 35/095, 1998). According to this method the transformation of hydrocarbons and/or oxygen-containing compounds is carried out at a temperature 280-460 C, a pressure of 0.1-4 MPa and in the presence of hydrogen-containing gas with a catalyst containing a zeolite with structure of ZSM-5 or ZSM-11, in the crystal lattice which consists of atoms of aluminum and iron, with subsequent separation of the products contacting gaseous and liquid fractions, the stage contacting is performed with a catalyst containing zeolite total empiricheskoi formula (0.02-0.09)Na2O Al2ABOUT3(0,01-1,13)Fe2ABOUT3(27-212)SiO2kH2O modified elements or compounds is otopleniya catalyst and not a high yield of high octane gasoline fractions and aromatic hydrocarbons from hydrocarbon raw materials.

The closest to the essence of the technical solution is the way transformations of aliphatic hydrocarbons2-C12in a high-octane component of gasoline or a concentrate of aromatic hydrocarbons is carried out at a temperature of 250-650 C, a pressure of 0.1-4.0 MPa and space velocity of the raw material is 0.1 to 10.0 h-1in the presence of a catalyst containing a group zeolite with a molar ratio of SiO2/Al2ABOUT3=20-150 mol/mol and with a residual content of sodium oxide is not more than 0.4 wt.%, zinc oxide and/or gallium oxide, and in any ratio of two or three oxide from the group of rare earth elements selected from the group CE, La, Nd, Pr, binder additionally contains iron oxide (III), magnesium oxide and calcium oxide (U.S. Pat. RU # 2165293, 01 J 29/40, WITH 10 G 35/095, 2000).

The disadvantages of this method are the multistage get, the complex composition of multicomponent catalyst and not a high yield of aromatic hydrocarbons from hydrocarbon raw materials.

The objective of the invention is the obtaining of an active and selective catalyst for the conversion process are aliphatic hydrocarbon, C2-C12in high-octane gasoline and/or aromatic hydrocarbons.

W2-C12in high-octane gasoline and/or aromatic hydrocarbons contains telesolutions with the structure of high zeolite ZSM-5 with silicate module SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000; as modifying component contains at least one oxide of an element selected from the group: copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium in an amount of 0.1-10.0 wt.%, as a hardening additive contains 0.1 to 5.0 wt.% oxide of boron, phosphorus, or mixtures thereof, the binder is alumina, followed by forming into pellets or tablets and the catalyst formed during the heat treatment at 500 to 600 C for 0.1 to 24 hours

The increase in catalyst activity and selectivity for the formation of aromatic hydrocarbons from hydrocarbon feedstock is achieved by obtaining zhelezohromovye with the structure of high zeolite ZSM-5 at the stage of hydrothermal synthesis. Additional introduction to telesolutions metals modifier in an amount of 0.1-10.0 wt.% allows to increase the output of high-octane gasoline and aromatic hydrocarbons from aliphatic hydrocarbons2-C12.

Telesolutions (JAS) with the giving of 0.5-7 days the reaction mixture, contains a source of cations of alkali metal, silicon oxide, aluminum oxide, iron oxide, hexamethylenediamine were (R) and water in the ratio of SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000; H2O/SiO2=20-80; R/SiO2=0,03-1,0; HE-/SiO2=0,076-0,6; Na+/SiO2=0,2-1,0 (U.S. Pat. RU # 1527154, 01 33/28, 1987) or other known methods. The degree of crystallinity obtained JAS is 85-100%, after crystallization of the zeolite is washed with distilled water, dried at 110 C for 2-12 h and calcined at 550-600 C for 4-12 h In IR-spectra obtained JAS observed absorption band at 445, 550, 810 cm-1and a broad band in the region of 1000-1300 cm-1characteristic of high zeolite ZSM. According to IR-spectroscopy and x-ray analysis of the obtained JAS identical to the zeolite ZSM-5.

The cooking process of the proposed catalyst consists of the following stages: decationization, impregnation decationizing of zhelezohromovye salts of metals-modifiers acids (boric, phosphoric, or a mixture thereof) as a hardening additives, mixing with a binder - aluminum hydroxide (boehmite) or aluminum oxide, formed into granules or pellets, drying, and catalisano processing 25% solution of NH4Cl (10 ml per 1 g of zeolite) at 90 C for 2 h, then washed with water, dried at 110 C for 4-12 h and calcined at 550-600 C for 4-12 h

Introduction metal-modifiers in dictionary telesolutions carried out by impregnation with appropriate aqueous solutions of salts of metals of modifying capacity of the zeolite. The estimated amount of the salt of the corresponding metal modifier dissolved in distilled water in the amount covering the entire volume of JAS. Impregnation JAS carried out at 40-50 C and stirring for 3-4 hours, after which the zeolite is dried at 110 C for 4-6 h

A hardening additive in the form of boron or phosphorus is introduced into the dried zeolite by impregnation with a solution of boric or phosphoric acid. The estimated amount of the acid dissolved in distilled water in the amount covering the entire volume of JAS. Impregnation of the zeolite is carried out at 20-30 C and stirring for 2-3 hours, after which the zeolite is dried at 110 C for 4-6 h

Then the estimated amount of the binder of aluminum hydroxide (boehmite) or aluminum oxide at the stage of forming pre-expose peptization of 0.1 n solution of nitric acid, then mixed with dried and is in granules or tablets, dried at 20-30 C for 2-8 h at 110 C for 2-6 h, and then calcined at 550-600 C for 4-12 h In the process of drying and calcining at a high temperature of 550-600 With zhelezohromovye structure type zeolite H-ZSM-5 and component connections of modifying metals, hardening binder and additives are modifying JAS active components, the formation and the formation of active, selective and stable catalyst.

The obtained zeolite catalysts (both before and after mixing with a binder) can be treated with water vapor (100%) at 450-550 With a bulk velocity of water flow (liquid) 1-2 h-1within 4-16 hours

The invention is illustrated by the following examples.

Example 1 (the prototype). To 200 g of water glass (29 wt.% SiO2, 9 wt.% Na2O, 62 wt.% H2A) with stirring, add 11 g of the diamine in 100 ml of N2About 1 g high zeolite as a “seed”, 14,475 g of Al(NO3)39 H2About 160 ml of N2Oh and poured a 0.1 n solution of HNO3. The resulting mixture was loaded into a stainless steel autoclave, heated to 175-180 C and maintained at this temperature for 6 days, and then cooled to room temperature. The synthesis is giving 8 hours For translation in the N-form high-silica zeolite decationized processing 25 wt.% aqueous solution of NH4Cl (10 ml per 1 g of zeolite) at 90 C for 2 h, then washed with distilled water, dried at 110 C for 4-6 h and calcined at 550 C for 6 hours Receive high-silica type zeolite H-ZSM-5 with silicate module SiO2/Al2ABOUT3=50.

The resulting catalyst has a composition, wt.%:

SiO296,6

Al2O33,3

Na2O 0,1

Example 2 (the prototype). High-silica zeolite H-ZSM-5 receive the same as in example 1, but instead 14,475 g of Al(NO3)39 H2O take 24,15 g of Al(NO3)39 H2O. Get high-silica type zeolite H-ZSM-5 with silicate module SiO2/Al2ABOUT3=30.

The resulting catalyst has a composition, wt.%:

SiO294,6

Al2ABOUT35,3

Na2O 0,1

Example 3. Telesolutions (JAS) with the structure of the high-type zeolite H-ZSM-5 receive the same as in example 1, but instead 14,475 g of Al(NO3)39 H2O take 12,07 g of Al(NO3)39 H2O and 12,08 g Fe(NO3)39 H2O. Get Telesolutions th catalyst has the composition wt.%:

SiO293,5

Al2O32,6

Fe2ABOUT33,8

Na2O 0,1

Example 4. Telesolutions (JAS) with the structure of the high-type zeolite H-ZSM-5 receive the same as in example 1, but instead 14,475 g of Al(NO3)39 H2O take 18,11 g of Al(NO3)39 H2O and 6,04 g Fe(NO3)39 H2O. Get Telesolutions type H-ZSM-5 with silicate module SiO2/Al2ABOUT3=40, SiO2/Fe2O3=130.

The resulting catalyst has a composition, wt.%:

SiO294,0

Al2ABOUT34,0

Fe2ABOUT31,9

Na2O 0,1

Example 5. JAS receive the same as in example 1, but instead 14,475 g of Al(NO3)39 H2About take 13,027 g of Al(NO3)39 H2O and 1,447 g Fe(NO3)39 H2O. Get Telesolutions type H-ZSM-5 with silicate module SiO2/Al2ABOUT3=55, SiO2/Fe2ABOUT3=540.

The resulting catalyst has a composition, wt.%:

SiO296,5

Al2ABOUT32,9

Fe2ABOUT30,5

Na2O 0,1

Example 6. 10 g decationizing JAS with silicate module SiO2The resulting catalyst has a composition, wt.%:

Telesolutions 70

IN2O31

binder (Al2ABOUT3) 29

Example 7. 10 g decationizing JAS with silicate module SiO2/Al2O3=60, SiO2/Fe2O3=65, obtained according to example 3, by impregnation put 0,868 g of cu(NO3)23H2O. For this 0,868 g of cu(NO3)23H2O was dissolved in 20 ml of distilled water, the impregnated zeolite is obtained by a solution of nitrate of copper is carried out at 40-50 C and stirring for 3-4 hours, after which the zeolite is dried at 110 C for 4-6 h

Then 0,253 g boric acid dissolved in 20 ml of distilled water, dried impregnated and treated zeolite is dried at 110 C for 4-6 h

Then 4,874 g of boehmite subjected peptization of 0.1 n nitric acid and mixed with dried and processed JAS until a homogeneous pasty mass. The resulting mass is formed into granules or pellets, dried at 20-30 C for 6-8 h, then at 110 C for 2-3 h and calcined at 600 C for 4-8 h

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

CuO 2

IN2O31

Binder (Al2ABOUT3) 27

Example 8. Zeolite-containing catalyst was prepared as in example 7, but instead 0,868 g of cu(NO3)23H2O take 1,045 g Zn(NO3)26N2O.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

ZnO 2

IN2O31

Binder (Al2ABOUT3) 27

Example 9. Zeolite-containing catalyst was prepared as in example 7, but instead 0,868 g of cu(NO3)23H2About take 0,389 g (NH4)2MoO4.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

Moo32

IN2O31

Binder (Al2ABOUT3) 27

Example 10.2O take 1,272 g GA(NO3)2N2O.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

GA2ABOUT32

IN2O31

Binder (Al2ABOUT3) 27

Example 11. Dictionary JAS with silicate module SiO2/Al2O3=40, SiO2/Fe2O3=130 receives the same way as in example 4. Zeolite-containing catalyst was prepared as in example 7, but instead 0,868 g of cu(NO3)33H2About take 0,079 g ammonium renevating NH4ReO4and instead 0,253 g of boric acid and 4,538 g of boehmite take 0,197 g H3RHO4and 4,789 g of boehmite.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

Re2O70,5

P2O51

Binder (Al2ABOUT3) 28,5

Example 12. Dictionary JAS with silicate module SiO2/Al2ABOUT3=55, SiO2/Fe2ABOUT3=540 receives the same way as in example 5. Zeolite-containing catalyst was prepared as in example 11, but instead 0,079 g NH4ReO4and 4,789 g of boehmite take 0,378 g of CE(NO3)36N2PO and 4,706 g of boehmite.

Obtained CE is UB>2O51

Binder (Al2ABOUT3) 28

Example 13. Zeolite-containing catalyst was prepared as in example 12, but instead 0,378 g of CE(NO3)36N2About take 0,380 g La(NO3)36N2O.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

La2O31

P2O51

Binder (Al2ABOUT3) 28

Example 14. Zeolite-containing catalyst was prepared as in example 12, but instead 0,378 g of CE(NO3)36N2Oh, 4,706 g of boehmite take 0,868 g of cu(NO3)23H2Oh, and 4,538 g of boehmite.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

CuO 2

P2O51

Binder (Al2ABOUT3) 27

Example 15. Zeolite-containing catalyst was prepared as in example 14, but instead 0,868 g of cu(NO3)23H2O take 1,045 g Zn(NO3)26N2O.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

ZnO 2

P2O51

Binder (Al2ABOUT3) 27

Example 16. CEO the> and 4,706 g of boehmite take 2,171 g of cu(NO3)23H2O and 4,034 g of boehmite.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

CuO 5

P2O51

Binder (Al2ABOUT3) 24

Example 17. Zeolite-containing catalyst was prepared as in example 16, but the catalyst was further treated with water vapor. For this zeolite-containing catalyst after calcination is loaded into the reactor and subjected to thermoprotei treatment with water vapor (100%) at 480 with a bulk velocity of water flow (liquid) 1 h-1within 12 hours

Example 18. Zeolite-containing catalyst was prepared as in example 12, but instead 0,378 g CE(NO3)36N2Oh and 4,706 g of boehmite take 5,221 g Zn(NO3)26N2O and 3,193 g of boehmite.

The obtained zeolite catalyst has a composition, wt.%:

Telesolutions 70

ZnO 10

P2O51

Binder (Al2ABOUT3) 19

Example 19. Zeolite-containing catalyst was prepared as in example 14, but instead 0,868 g of cu(NO3)23H2O take 0,524 g Zn(NO3)26H2O and 0,636 g GA(NO3)2ZnO 1

GA2O31

P2O51

Binder (Al2ABOUT3) 27

Example 20. Zeolite-containing catalyst was prepared as in example 19, but the catalyst was further treated with water vapor. For this zeolite-containing catalyst after calcination is loaded into the reactor and subjected to thermoprotei treatment with water vapor (100%) at 520 With a bulk velocity of water flow (liquid) 1 h-1within 4 hours

The resulting catalysts are experiencing in the process of conversion of aliphatic hydrocarbons2-C12(straight-run gasoline fraction 28-185 C) for the installation of flow-type fixed bed of the catalyst at temperatures of 350-550 C, space velocity of the raw material of 0.5 to 5.0 h-1and a pressure of 0.1 to 1.5 MPa.

In the process of conversion of a mixture of aliphatic hydrocarbons WITH2-C12(straight-run gasoline fraction 28-185 C) with increasing reaction temperature from 350 to 550 C in zhelezohromovyh with the structure of high zeolite ZSM-5 reactions proceed cracking, dehydrogenation, isomerization, dehydrocyclization and paraffin aromatization of hydrocarbons from the formation mainly in the early stages of the process, the olefinic plurisubharmonicity modifying additives from the group of copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium in an amount of 0.1-10.0 wt.% allows to considerably increase the output of high-octane gasoline and aromatic hydrocarbons from aliphatic hydrocarbons2-C12compared to the unmodified zeolite.

The table below shows examples clarify the invention without limiting it.

As can be seen from the examples of catalysts 1-20 table, the catalysts 3-20 have a higher output (60-78%) of liquid products of the reaction is high - octane gasoline from a mixture of aliphatic hydrocarbons WITH2-C12than catalysts (example 1-2) prototype Pat. RU # 2165293.

Thus, the proposed catalysts for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons on the basis of zhelezohromovye with the structure of high zeolite ZSM-5 with silicate module SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000 and modified at least one oxide from the group of copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium in an amount of 0.1-10.0 wt.% allow to increase the output of high-octane gasoline to 60-78% and aromatic hydrocarbons up to 42-44% of aliphatic oglewood of aliphatic hydrocarbons 2-C12in the presence of catalysts based zhelezohromovye with the structure of high zeolite ZSM-5 with silicate module SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000 and modified at least one oxide from the group of copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium in an amount of 0.1-10.0 wt.% allows to increase the output of high-octane gasoline and aromatic hydrocarbons from aliphatic hydrocarbons, C2-C12than in the presence of a catalyst (example 21) prototype Pat. RU # 2165293.

1. The catalyst for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons containing zeolite with structure of ZSM-5, the connecting component is aluminum oxide, the modifying component, characterized in that it contains as a zeolite telesolutions with silicate module SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000, as modifying component contains at least one oxide of an element selected from the group of copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium; optionally a hardening additive is an oxide of boron, phosphorus or SS="ptx2">Telesolutions with silicate module

SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000 is 60.0 to 90.0

The modifying component 0,1-10,0

The oxide of boron, phosphorus, or a mixture of 0,5-5,0

Alumina Rest

2. The method of producing catalyst under item 1, characterized in that telesolutions with the structure of zeolite ZSM-5 with silicate module SiO2/Al2O3=20-160, SiO2/Fe2O3=30-5000 get the hydrothermal crystallization of a reaction mixture at 120-180°C for 1-7 days, containing sources of silicon oxide, aluminum oxide, iron oxide, oxide of alkali metal, hexamethylenediamine were and water, with subsequent impregnation of zhelezohromovye compounds modifying metals, mixing with a binder, forming the catalyst mass, drying and calcining.

3. The method of producing catalyst according to p. 2, characterized in that telesolutions by impregnation cause connection of the modifying group metals copper, zinc, gallium, lanthanum, cerium, molybdenum, rhenium and compounds hardening additives.

4. The method of producing catalyst according to PP.2 and 3, characterized in that the catalyst is obtained by mixing a modified telesolutions-600C) for 0.1-24 hours

5. A method of converting aliphatic hydrocarbons2-C12in high-octane gasoline and/or aromatic hydrocarbons in the presence of a catalyst, characterized in that the used catalyst under item 1 and the conversion of aliphatic hydrocarbons2-C12in high-octane gasoline and/or aromatic hydrocarbons is carried out at 300-550°C, flow rate of 0.5 to 5.0 h-1and a pressure of 0.1 to 1.5 MPa.

 

Same patents:

The invention relates to the production of motor fuels to the one-step catalytic process for the production of high-octane gasoline and diesel fuels with low sulfur content of various hydrocarbon materials with a high content of chemically stable sulfur compounds

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons

The invention relates to the refining and petrochemical industries and is dedicated to the creation of the catalysts used in the processing of aliphatic hydrocarbons in the concentrate of aromatic hydrocarbons or high-octane component of gasoline

The invention relates to a technology for environmentally friendly high-octane gasoline and can be used in the refining and petrochemical industry to improve low-octane hydrocarbons in the presence of contact of the composition consisting of zeolite catalysts
The invention relates to the production of motor fuel, namely a catalytic process for the production of a variety of hydrocarbons of high octane gasoline and vysokochetkogo diesel fuel with a low freezing point

The invention relates to an integrated device for the production of a component of high-octane gasoline and aromatic hydrocarbons

The invention relates to methods of producing aromatic hydrocarbons from a hydrocarbon and can be used in the refining and petrochemical industry

The invention relates to methods of producing unleaded high-octane gasoline fractions with reduced benzene content and/or aromatic hydrocarbons WITH6-C10of hydrocarbons and/or oxygen-containing organic compounds

The invention relates to the field of chemistry, and in particular to methods of obtaining aromatic hydrocarbons from light hydrocarbons, including petroleum gas terminal stages of separation

The invention relates to catalysts containing on the surface of the carrier compounds of molybdenum and/or tungsten, with or without additives compounds of one or more transition metals, processes for their preparation and may find wide application in the processes of hydroperiod hydrocarbons of petroleum or coal origin

The invention relates to the field of preparation of supported catalysts and can find application in various sectors of the chemical industry

The invention relates to a catalytic element for recombination of hydrogen and/or carbon monoxide with oxygen for nuclear power plants

The invention relates to a method for producing a catalyst composition comprising bulk catalyst particles containing at least one base metal of group VIII and at least two metals of group VIB, including the integration and interaction of at least one component made of base metal of group VIII with at least two components of metals of group VIB in the presence of proton fluid, and at least one metal component remains at least partly in the solid state throughout the method, where the metals of groups VIII and VIB range from about 50 to about 100 wt.% in terms of oxides, of the total weight of the specified volume of the catalytic particles, and the solubility of the component metals of these groups, which are at least partly in the solid state during the reaction, is less than 0.05 mol/100 ml water at 18aboutWith

The invention relates to the production of hydrocarbons from synthesis gas

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons
Up!