Catalyst for dehydrogenation of paraffin hydrocarbons

 

(57) Abstract:

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons. Offered the catalyst for dehydrogenation of paraffin hydrocarbons comprising chromium oxide and alumina media. As a carrier, the catalyst contains aluminium spinel and has the following content of components in terms of oxides, wt.%: Cr2O310,0-30,0, ZnO 30,0-45,0, Al2O3the rest of it. Effect: this catalyst allows to reduce coke formation, reduce the proportion of adverse reactions increases the efficiency of the process of dehydrogenation of paraffin hydrocarbons. table 1.

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons.

Known catalyst for dehydrogenation of paraffin hydrocarbons containing, wt.%:

Cr2O3- 12,2

TO2ON - 1,4

SiO2- 2,0

Al2O3- Rest

(U.S. Pat. RF 1366200, publ. BI 2 - 15.01.1988 year).

Closest to the present invention is a catalyst for dehydrogenation of paraffin hydrocarbons, comprising, by wt.%:

Cr2 where Me is an alkaline metal.

(U.S. Pat. RF 2127242, publ. BI 7 - 10.03.1999 year).

Both of these catalysts have low activity and selectivity in the process of dehydrogenation of paraffin hydrocarbons.

The present invention is to increase the efficiency of the catalyst.

Offered the catalyst for dehydrogenation of paraffin hydrocarbons comprising chromium oxide and, as a carrier, aluminium spinel in the following components in terms of oxides, wt.%:

Cr2O3- 10,0-30,0

ZnO - 30,0-45,0

Al2O3- Rest

Distinct new catalyst from the prototype is the content as a carrier aluminium spinel at the specified content component.

The use of the catalyst of the inventive combination of components in a given volume can reduce the coke formation, promotes more rapid and complete oxidation-reduction reactions. This reduces the proportion of adverse reactions, increasing the efficiency of the catalyst.

The process of obtaining a new catalytic system consists in dispersing joint of the catalyst can be carried out, for example, impregnation of the specified carrier with a solution containing precursors of chromium oxide with subsequent formation of microspheres by spray-drying the resulting suspension in the column of spray drying. The sample calcined catalyst in the activator when 680-850oC for 2-5 hours.

Example 1.

Aluminium spinel derived from zinc aluminate by calcination at 1000oC for 4 hours in air flow. Microspheric lomography the catalyst having a particle diameter of from 5 to 250 microns, produced by the method of spray-drying the suspension obtained from 173 g of aluminium spinel, 40,75 g of chromium trioxide and 450 ml of water in a bead mill with stirring for 5 hours at 20oC. a Sample of the catalyst is subjected to heat treatment consisting of annealing at 680oC for 5 hours in air flow. The resulting product has the following composition, wt.%:

Cr2O3- 15,2

ZnO - 37,6

Al2O3- 47,2

The resulting catalyst was tested in the process of dehydrogenation of isobutane and propane, carried out 550-610oC, space velocity of the raw material 400-600 l reagent / l catalizadores in laboratory quartz reactor. Catalitic the hydrocarbons are served within 30 minutes; phase blowdown, when nitrogen is passed for 10 minutes to release the catalyst from the adsorbed reaction products of dehydrogenation; regeneration phase, when in the regenerator the gas is fed to the regeneration air for 30 minutes (in these experiments), and again the blowdown phase when nitrogen is passed for 10 minutes to release the catalyst from the adsorbed reaction products of regeneration. Specifications industrial process dehydrogenation in a fluidized bed of catalyst require regeneration at temperatures above the temperature of reaction: in this case, regeneration and restoration is carried out at 650oSecond, whereas the dehydration - when 550-610oC. the results are shown in the table.

Example 2.

Microspheric lomography the catalyst having a particle diameter of from 5 to 250 microns, produced by the method of spray-drying the suspension obtained from 173 g of aluminium spinels synthesized as described in example 1, 57 g of chromium trioxide and 500 ml of water in a bead mill with stirring for 4 hours at 30oC. a Sample of the catalyst is subjected to heat treatment consisting of annealing at 720oWith over 4 is BR>
Al2O3- 44,5

The resulting catalyst was tested in the process of dehydrogenation of isobutane and propane, as described in example 1. The results are shown in the table.

Example 3.

Microspheric lomography the catalyst having a particle diameter of from 5 to 250 microns, produced by the method of spray-drying the suspension obtained from 173 g of aluminium spinels synthesized as described in example 1, 75 g of chromium trioxide and 550 ml of water in a bead mill with stirring for 3 hours at 40oC. a Sample of the catalyst is subjected to heat treatment consisting of annealing at 800oC for 3 hours in air flow. The resulting product has the following composition, wt.%:

Cr2O3- 24,8

ZnO - 33,3

Al2O3- 41,9

The resulting catalyst was tested in the process of dehydrogenation of isobutane and propane, as described in example 1. The results are shown in the table.

Example 4.

Microspheric lomography the catalyst having a particle diameter of from 5 to 250 microns, produced by the method of spray-drying the suspension obtained from 173 g of aluminium spinels synthesized as described in example 1, 97 g of chromium trioxide and 550 ml of water in beaded Eastasia of annealing at 780oC for 3 hours in air flow. The resulting product has the following composition, wt.% :

Cr2O3- 29,9

ZnO - 31,1

Al2O3- 39,0

The resulting catalyst was tested in the process of dehydrogenation of isobutane and propane, as described in example 1. The results are shown in the table.

Example 5.

Microspheric lomography the catalyst having a particle diameter of from 5 to 250 microns, produced by the method of spray-drying the suspension obtained from 173 g of aluminium spinels synthesized as described in example 1 of 25.5 g of chromium trioxide and 400 ml of water in a bead mill with stirring for 3 hours at 50oC. a Sample of the catalyst is subjected to heat treatment consisting of annealing at 850oC for 2 hours in air flow. The resulting product has the following composition, wt.%:

Cr2O3- 10

ZnO - 39,9

Al2O3- 50,1

The resulting catalyst was tested in the process of dehydrogenation of isobutane and propane, as described in example 1. The results are shown in the table.

Catalyst for dehydrogenation of paraffin hydrocarbons comprising chromium oxide and alumina carrier, characterized in that as the carrier Ref.%:

CR2O3- 10,0 - 30,0

ZnO - 30,0 - 45,0

Al2O3- Ostalnoe

 

Same patents:

The invention relates to a device for the catalytic dehydrogenation of hydrocarbons, in particular for radial flow reactors, and can be used in the chemical and petrochemical industry

The invention relates to a device for the catalytic dehydrogenation of hydrocarbons and can be used in the petrochemical industry

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons, the catalyst comprises chromium oxide, aluminum oxide and tin oxide, in addition it contains zinc oxide and platinum at the following content, wt.%: CR2ABOUT310,0-30,0, ZnO 30,0-45,0, SnO20,1-3,0, Pt Of 0.005 To 0.2, Al2ABOUT3the rest

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons

The invention relates to the production of vinylaromatic hydrocarbons, such as styrene, alfamethylstyrene, divinylbenzene, etc. and can be used in the petrochemical industry

The invention relates to a method for catalytic dehydrogenation legitimacy hydrocarbons in the reaction system containing steel part

The invention relates to the extraction and removal of by-products, representing a multi-core aromatic organic compounds from a stream of steam flowing from the reaction zone dehydrogenization normally gaseous hydrocarbon

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons, the catalyst comprises chromium oxide, aluminum oxide and tin oxide, in addition it contains zinc oxide and platinum at the following content, wt.%: CR2ABOUT310,0-30,0, ZnO 30,0-45,0, SnO20,1-3,0, Pt Of 0.005 To 0.2, Al2ABOUT3the rest

The invention relates to the production of catalysts for the synthesis of organofluorine compounds (penthaleidae General formula C2HClxF5-xwhere x varies from 0 to 4), in particular, to obtain trichotillomania, tetrafluorochloroethane and Pentafluoroethane (freon 123, 124 and 125, respectively)

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons

The invention relates to the production of catalysts for dehydrogenation of paraffin hydrocarbons

The invention relates to the field of catalysts for dehydrogenation of paraffin hydrocarbons

The invention relates to catalysts for dehydrogenation of paraffin hydrocarbons
The invention relates to the production of cycloalkanones C8-C12promising intermediates in the synthesis of lactams, aliphatic dicarboxylic acids, Daminov - monomers for the production of polyamide fibers, plastics and plasticizers new types and other valuable materials

The invention relates to methods for preparing catalysts for dehydrogenation of paraffin hydrocarbons, in particular for the dehydrogenation of C2-C5paraffins to the corresponding olefins

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention relates to production of olefin or diolefin hydrocarbons via dehydrogenation of corresponding paraffinic C3-C5-hydrocarbons carried out in presence of catalyst comprising chromium oxide and alkali metal deposited on composite material including alumina and aluminum wherein percentage of pores larger than 0.1 μm is 10.0-88.5% based on the total volume of open pores equal to 0.10-0.88 cm3/g. Preparation of catalyst involves treatment of carrier with chromium compound solution and solution of modifying metal, preferably sodium or sodium and cerium. Carrier is prepared by from product resulting from thermochemical activation of amorphous hydrargillite depicted by formula Al2O3·nH2O, where 0.25<n<2.0, added to homogenous mass in amount 1.0 to 99.0% using, as additional material, powdered aluminum metal, which is partly oxidized in hydrothermal treatment and calcination stages. Hydrocarbon dehydrogenation process in presence of the above-defined catalyst is also described.

EFFECT: increased activity and selectivity of catalyst.

3 cl, 2 dwg, 4 tbl, 7 ex

Up!