Catalyst for conversion of methanol into olefin hydrocarbons, process of preparation thereof, and a process of conversion of methanol into olefin hydrocarbons

FIELD: petrochemical processes.

SUBSTANCE: catalyst, containing high-silica zeolite of the H-ZSM-5 type having silica modulus SiO2/Al2O3 = 20 to 160 in amount 60.0-90.0%, contains (i) as modifying component at least one oxide of element selected from group: boron, phosphorus, magnesium, calcium, or combination thereof in amount 0.1-10.0 wt %; and (ii) binding agent: alumina. Catalyst is formed in the course of mechanochemical and high-temperature treatments. Described is also a catalyst preparation process comprising impregnation of decationized high-silica zeolite with compounds of modifying elements, dry mixing with binder (aluminum compound), followed by mechanochemical treatment of catalyst paste, shaping, drying, and h-temperature calcination. Conversion of methanol into olefin hydrocarbons is carried out in presence of above-defined catalyst at 300-550°C, methanol supply space velocity 1.0-5.0 h-1, and pressure 0.1-1.5 mPa.

EFFECT: increased yield of olefin hydrocarbons.

3 cl, 1 tbl, 15 ex

 

The invention relates to the petrochemical industry, to methods of preparation of the catalyst for conversion of methanol to olefin hydrocarbons.

The main industrial process to obtain olefinic hydrocarbon is a thermal pyrolysis of different types of hydrocarbons, which is carried out at a temperature of 780-850°C in the presence of water vapor. Disadvantages of the process of thermal pyrolysis of hydrocarbons are very harsh process conditions, high consumption of water vapor, hydrocarbons and low yield of lower olefins With2-C3- no more 42-44%.

Known catalyst and method of catalytic conversion of methanol to olefins on the crystalline aluminosilicate catalyst (U.S. Pat. USA N 4433189, C 07 C 1/20, 1984). A mixture of hydrocarbons containing lower olefins, obtained by passing etanolsoderjasimi raw materials, possibly mixed with water in the amount of 1-10 mol/mol of methanol, at temperatures between 20 and 500°C and a pressure of 0.35-35 at over a catalyst consisting of a bound or unbound crystalline aluminosilicate zeolite ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-48, ZSM-5, with an index of permeability 1-12, a molar ratio of SiO2:Al2O3≥12, or over a catalyst consisting of amorphous SiO2modified bound or unbound crystalline alumosilicate the m zeolite with an index of permeability 1-12 and the ratio of SiO 2:Al2O3≥12, treated with silicone or silane. Together with etanolsoderjasimi raw material in the reaction zone, introducing a diluent (air, inert gas) with a bulk velocity of 10-610 h-1to maintain the ratio O2:MeOH=from 0.01 to 0.25:1. When using as a catalyst of zeolite HZSM-5 modified SiO2the selectivity for the amount of olefins With2-C4is 69%.

The disadvantages are the complexity of the preparation of the catalyst and the use of diluent (air, inert gas) in the conversion of methanol, which creates additional difficulties for subsequent isolation of pure olefins With2-C4.

A method of obtaining high zeolites of type ZSM-5 (U.S. Pat. EN N 1527154, C 01 B 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 in the conversion of methanol is 460-1100 hours To improve the stability of high zeolites in the H form is subjected to mechanical grinding to a particle size of 0.1 to 1.0 μm and thermoprotei processing water is arene at 520° With over 50 hours

The disadvantage of the catalyst is not sufficiently high selectivity in the formation of lower olefins With2-C4from methanol.

Known catalyst and method of turning organic materials: alcohols, ethers, or their mixtures, for example of methanol to hydrocarbons at a temperature 275-600°C, a pressure of 0.5 to 50 ATM and a flow rate of 0.5-100 h-1catalyst consisting of a zeolite with an initial molar ratio of SiO2:Al2O3≥100:1 (500:1), obtained by crystallization in the presence of Quaternary niewyk ions, calcined at 200-600°C and treated with 100-600°C pairs AlCl3c followed by hydrolysis and calcination (U.S. Pat. USA N 4568787, C 07 C 1/00, C 07 C 1/20, 1986). For the preparation of the catalyst used zeolite ZSM-5, ZSM-11, mixed phase, ZSM-12, ZSM-38, ZSM-23 or ZSM-48. As a binder for the catalyst used Al2O3. Conversion of methanol reaches 78% with selectivity2H433.6% and C3H625%.

The disadvantages of catalyst and method are the complexity of the preparation of the catalyst and not enough high activity and selectivity in the formation of olefins With2-C3from methanol.

Closest to the claimed are the catalyst based on zeolite HZSM-5, a method of converting methanol to olefins on coarse-grained catalyst Pat. USA N 4550217, C 07 C 1/20, 1985). The conversion of aliphatic alcohols With1-C3possibly, their mixtures, their aqueous solutions or corresponding ethers, better than methanol or dimethyl ether to a product containing olefins, in the presence of the crystalline type zeolite HZSM-5, which is to control the activity of the catalyst change its grain, and activity increase corresponds to the increase in the grain size and the average conversion of 50% of the used catalyst with an average grain size ≥3,2 mm

The main disadvantages of this catalyst and the method adopted for the prototype, are the complexity of the preparation of the catalyst and is not sufficiently high selectivity of the formation of olefins from methanol (25,9-26,6%2H4and 22.5 and 22.8% With3H6).

The objective of the invention is the obtaining of an active and selective catalyst for the conversion of methanol to olefins, and the development of a method of producing olefinic hydrocarbons from methanol.

The technical result is achieved by the fact that the proposed catalyst for conversion of methanol to olefin hydrocarbons contains high-silica type zeolite H-ZSM-5 c silicate module SiO2/Al2O3=20÷160 in number 60,0÷to 90.0 wt.%, as the modifying component contains at least one oxide of an element selected from the group of elements: the PRS, phosphorus, magnesium, calcium or a mixture thereof in an amount of 0.1÷10.0 wt.%, the binder is alumina, and the catalyst is formed by mechanochemical process and high temperature treatments.

The cooking process of the proposed catalyst comprises the following steps: mixing the raw materials and crystallization of the reaction mixture under hydrothermal conditions, decationization, impregnation decationizing high zeolite compounds of elements modifiers, dry mixing with a binder is a compound of aluminum, subsequent mechanical processing of the catalyst mass, forming, drying and calcining at a high temperature.

High zeolites (VCC) ZSM-5 get the hydrothermal crystallization at 120÷180°C for 1÷6 days the reaction mixture containing a source of cations of alkali metal, silicon oxide, aluminum oxide, hexamethylenediamine were and water in the ratio of SiO2/Al2O3=20÷160, H2O/SiO2=20÷80; R/SiO2=0,03÷1,0; OH-/ SiO2=0,076÷0,6; Na+/SiO2=0,2÷and 1.0.

After crystallization of the zeolite is washed with distilled water, dried at 110°C 2÷12 h and calcined at 550÷600°C for 4÷12 o'clock

According to IR-spectroscopy and x-ray analysis of the obtained VCC identical to the zeolite ZSM-5, with Epen crystallinity obtained VCC 85÷ 100%.

For translation in the N-form VCC decationized processing 25% solution of NH4Cl (10 ml per 1 g of zeolite) at 90°C 2 h, then washed with water, dried at 110°C 4÷12 h and calcined at 550÷600°C 4÷12 o'clock

Next, N-VCC with silicate module SiO2/Al2O3=20÷160 and the structure of zeolite ZSM-5 is impregnated with the modifying component - one compound from the group of elements: boron, phosphorus, magnesium, calcium or mixtures thereof in an amount of 0.1÷10.0 wt.%, dried at 110°C for 4÷6 o'clock Processed and dried zeolite is mixed with the calculated amount of the binder is a compound of aluminum: aluminum hydroxide or aluminum oxide.

The resulting mixture is subjected to mechanochemical treatment in a vibrating mill for 1÷72 h, the catalyst mass is molded, dried at 20÷25°C for 1÷16 h, then at 110°C for 1-24 h and calcined at a temperature of 550÷600°C for 1÷24 hours

Under the action of mechanical and high-temperature treatments of the mixture: type zeolite H-ZSM-5, components, compounds modifying metals and binder additives is the modification of the zeolite active components, formation and education of highly disperse, active, selective and durable catalyst.

The obtained zeolite catalysts (both before and after smashin the I 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 1-24 hours

The conversion of methanol to olefin hydrocarbons is carried out in the presence of a zeolite catalyst at a temperature of 300-550°C, space velocity of methanol 1,0-5,0 h-1and a pressure of 0.1 to 1.5 MPa.

The invention is illustrated by the following examples.

Example 1. To 400 g of water glass (29% SiO2, 9% Na2O 62% H2O) was added with stirring to 23.6 g of diamine (R) in 200 ml of H2O, 48.10 per g of Al(NO3)3· 9H2O in 320 ml of H2O, 1 g "seed" high zeolite and poured 0.1 N. the solution of HNO3.

The resulting mixture was loaded into an autoclave of stainless steel, is heated to 175°C and incubated for 6 days and then cooled. The synthesized product is washed with water, dried and calcined at 540° (C 12 h of crystallinity of the product is 96%.

For translation in H-form zeolites decationized processing 25% solution of NH4Cl (10 ml per 1 g of zeolite) at 90°C 2 h, then washed with water, dried at 110°C and calcined at 540°C 6 o'clock Get H-ZSM-5 with silicate module SiO2/Al2O3=30.

Example 2. H-ZSM-5 with silicate module SiO2/Al2O3=50 receives the same way as in example 1, but instead 48.10 per g of Al(NO3)3· 9H2O take 29,0 g of Al(NO3)3· 9H2 O Get H-ZSM-5 with silicate module SiO2/Al2O3=50.

Example 3. H-ZSM-5 with silicate module SiO2/Al2O3=90 receives the same way as in example 1, but instead 48.10 per g of Al(NO3)3· 9H2O take 16,10 g of Al(NO3)3· 9H2O Get H-ZSM-5 with silicate module SiO2/Al2O3=90.

Example 4. H-ZSM-5 with silicate module SiO2/Al2O3=160 receives the same way as in example 1, but instead 48.10 per g of Al(NO3)3· 9H2O take 16,10 g of Al(NO3)3· 9H2O Get H-ZSM-5 with silicate module SiO2/Al2O3=160.

Example 5. 5 g decationizing H-ZSM-5 with silicate module SiO2/Al2O3=30, obtained in example 1, by impregnation put 0,064 g of boric acid. 0,064 g boric acid dissolved in 10 ml of distilled water and impregnated with this solution the whole volume of the zeolite under stirring at 40-50°C for 3-4 h, after which the zeolite is dried at 110°C for 4-6 hours Then 2,479 g of boehmite AlO(OH) is mixed with dried and treated H-ZSM-5 and is subjected to mechanochemical treatment in a vibrating mill for 72 hours the resulting mass is molded, dried at 20-30°C for 6-8 h, then at 1100C for 2-3 h and calcined at 600°C for 12-14 hours

The resulting catalyst has a composition, wt.%:

H-ZSM-5 (SiO2/Al2O3=30)70,0
B2O30,5
binder (Al2O3)29,5

Example 6. 5 g decationizing H-ZSM-5 with silicate module SiO2/Al2O3=30, obtained in example 1, by impregnation put 1,503 g Ca(NO3)2· 4H2O. For this 1,503 g Ca(NO3)2· 4H2O dissolved in 10 ml of distilled water and impregnated with this solution the whole volume of the zeolite under stirring at 40-50°C for 3-4 h, after which the zeolite is dried at 110°C for 4-6 hours Then 2,101 g AlO(OH) is mixed with dried and treated H-ZSM-5 and is subjected to mechanochemical treatment in a vibrating mill for 12 hours resulting mass is molded, dried at 20-30°C for 14-16 h, then at 110°C for 10-12 h and calcined at 600°C for 10-12 hours

The resulting catalyst has a composition, wt.%:

H-ZSM-5 (SiO2/Al2O3=30)70,0
CaO5,0
binder (Al2O3)25,0

Example 7. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 0,325 g of Mg(NO3)2·2H 2O and 2,436 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=30)70,0
MgO1,0
binder (Al2O3)29,0

Example 8. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 1,633 g of Mg(NO3)2·2H2O and 2,101 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=30)70,0
MgO5,0
binder (Al2O3)25,0

Example 9. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 3,800 g of Mg(NO3)2·2H2O and 2,941 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=30)60,0
MgO10,0
binder (Al2O3)30,0

Example 10. Zeolite-containing catalyst was prepared that the same as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 0,106 g H3PO4and 3,077 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=30)65,0
P2O51,0
binder (Al2O3)34,0

Example 11. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 1,024 g of Mg(NO3)2·2H2O, 0,103 g H3PO4and 2,546 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=30)67,0
P2O51,0
MgO3,0
binder (Al2O3)29,0

Example 12. H-ZSM-5 with silicate module SiO2/Al2O3=50 receive the same as in example 2. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 0,325 g of Mg(NO3)2·2H2O and 2,436 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=50)70,0
MgO1,0
binder (Al2O3)29,0

Example 13. H-ZSM-5 with silicate module SiO2/Al2O3=50 receive the same as in example 2. Zeolite-containing catalyst was prepared as in example 6, but instead 1,503 g Ca(NO3)2·4H2O and 2,101 g AlO(OH) take 1,759 g of Mg(NO3)2·2H2O and 2,715 g AlO(OH).

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

H-ZSM-5 (SiO2/Al2O3=50)65,0
MgO5,0
binder (Al2O3)30,0

Example 14. Zeolite-containing catalyst was prepared as in example 7, 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%) in 480°With a bulk velocity of water flow (liquid) 1 h-1within 12 hours

Example 15. Zeolite-containing catalyst was prepared as in example 8, but the catalyst was further treated with water vapor. For this zeolite-containing catalyst after calcination is loaded into the reactor and subjected to the Ute 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 reforming of methanol on installing a flow-type fixed bed of the catalyst at a temperature of 350-550°C, space velocity of the raw materials 1,0-5,0 h-1and a pressure of 0.1 to 1.5 MPa.

In the process of reforming of methanol with increasing reaction temperature from 350 to 550°With over zeolite catalysts based on high-type zeolite H-ZSM-5 reactions proceed cracking, dehydrogenation, isomerization, dehydrocyclization and aromatization of hydrocarbons from the formation mainly in the first stages of the process of olefinic hydrocarbons, which later turn into isoparaffin and alkylaromatic hydrocarbons. Introduction to high-silica zeolite modifying additives from the group of elements: boron, phosphorus, magnesium, calcium or mixtures thereof in an amount of 0.1-10.0 wt.% (examples 5-15) can significantly increase the yield of olefinic hydrocarbons from methanol, compared with non-modified zeolite (examples 1-4).

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

As can be seen from the examples of catalysts 1-16 table, the catalysts (examples 5-15) have a higher yield of olefinic hydrocarbons (up to 72-73%) of methanol than the prototype Pat. USA N 4550217 (example 6).

Preliminary mechanical activation of a mixture of the starting components can significantly reduce the temperature of formation of the active components and to obtain highly dispersed, active and selective catalyst. Introduction metals modifier in an amount of 0.1-10.0 wt.% allows you to increase the selectivity of the formation of olefinic hydrocarbons from methanol.

Thus, the proposed catalysts for the conversion of methanol on the basis of high-type zeolite H-ZSM-5 c silicate module SiO2/Al2O3=20-160 and modified at least one oxide of elements from the group of boron, phosphorus, magnesium, calcium or mixtures thereof in an amount of 0.1-10.0 wt.% allow to increase the yield of olefinic hydrocarbons to 70-72%.

The way to obtain olefinic hydrocarbons from methanol in the presence of catalysts based on high type zeolites H-ZSM-5 and modified at least one of the oxides of group elements: boron, phosphorus, magnesium, calcium or mixtures thereof in an amount of 0.1-10.0 wt.% allows great output and selectivity to obtain olefinic hydrocarbons than the catalyst (prototype) Pat. USA N 4550217 (example 16).

1. Catalyst for conversion of methanol to olefin hydrocarbons containing zeolite with structure shall uroy ZSM-5, the binder component is aluminum oxide, the modifying component, characterized in that it contains a high-silica type zeolite H-ZSM-5 with silicate module SiO2:Al2About3=20-160; as modifying component contains at least one oxide of element selected from the group of boron, phosphorus, magnesium, calcium or a mixture thereof; the catalyst is formed in the process of mechanochemical and thermal treatment and has the following composition, wt.% in terms of the oxide:

High-silica type zeolite H-ZSM-5
with silicate module SiO2/Al2About3=20-160by 60.0 to 90.0
The modifying component0,1-10,0
BinderRest

2. The method of preparation of the catalyst according to claim 1, characterized in that the high-silica type zeolite H-ZSM-5 with silicate module SiO2:Al2About3=20-160 get hydrothermal crystallization at 120-180°C for 1-6 days. the reaction mixture containing sources of silicon oxide, aluminum oxide, oxide of alkali metal, and water hexamethylenediamine were further impregnated high zeolite compounds modifying elements from the group of boron, phosphorus, magnesium, calcium or mixtures thereof, mixed with the tie shall provide for - the connection of aluminum, followed by mechanochemical processing in a vibrating mill for 1-72 h, forming the catalyst mass, drying at 110°C for 1-24 h and calcining at 550-600°C for 1-24 hours

3. A method of converting methanol to olefin hydrocarbons in the presence of a zeolite catalyst comprising heating and passing methanol over zeolite catalyst, characterized in that methanol is passed through the layer of zeolite-containing catalyst according to claim 1, heated to a temperature of 300-550°With, at the space velocity of methanol 1,0-5,0 h-1and a pressure of 0.1 to 1.5 MPa.



 

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EFFECT: enhanced efficiency.

FIELD: chemical industry; petrochemical industry; methods of production of the catalysts and hydrocarbons with their use.

SUBSTANCE: the invention is pertaining to the method of production of the catalyst for production of hydrocarbons and to the method for production of hydrocarbons at the presence of the catalyst on the basis of the metal of VIII group on the carrier - the refractory oxide. The presented method of production of the catalyst for production of hydrocarbons on the basis of the metal of VIII group on the carrier - the refractory oxide provides for mixing of the refractory oxide with the surface area of no less than 0.5 m2 /g with the solution of the precursor of this refractory oxide and with the metal or with the precursor of this metal till production of the suspension, drying of the suspension and its calcination. The invention also presents the method of production of the hydrocarbons providing for contacting of the mixture of the hydrocarbon monoxide with hydrogen at the heightened temperature and pressure at presence of the catalyst produced by the method described above. The technical result is production of the catalyst with higher activity in the synthesis of the hydrocarbons at conservation of high selectivity.

EFFECT: the invention ensures production of the catalyst with the higher activity in the synthesis of the hydrocarbons at conservation of the high selectivity.

8 cl, 1 tbl, 1 ex

FIELD: petrochemical industry; methods of production of the cracking bead catalyst.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to the method of production of the cracking zeolite-containing catalysts (ZCCs). The bead catalyst is produced by mixing of the water solutions of the sodium silicate, aluminum sulfate and suspensions of NaY-type zeolite and alumina, molding of the hydrogel granules in the oil column, treatment with the solution of sodium sulfate and the following activation by the solution of ammonium sulfate or ammonium nitrate with the mixture of the rare-earth elements (REE), by the solution of the platonic-chloro-hydrogen acid, the drying and calcination in the steam aerosphere. At that the aluminum sulfate solution has the concentration of 0.5-7.0 kg/m3, and the calcinations is conducted at the steam concentration above 40 vol.%. The technical result of the invention is the controlled raise of the loose mass in the range of 650-850 kg/m3, the increase of activity and improvement of the mechanical properties of the bead catalyst.

EFFECT: the invention ensures the controlled raise of the loose mass in the given above range, the increase of activity and improvement of the mechanical properties of the bead catalyst.

6 ex, 1 tbl, 1 dwg

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to improved method for preparing double metal cyanide catalysts effective to catalyze synthesis of polyetherpolyols via polyaddition of alkylene oxides to starting compounds containing active hydrogen atoms. Method is characterized by that aqueous solutions of metal salt and metal cyanide salt are first brought to react in presence of organic complex ligands and, if necessary, one or several other complexing components to form dispersion of double metal cyanide catalyst, which is filtered to give filtration precipitates. The latter are washed with one or several aqueous or nonaqueous solution of organic complex ligands in flowing washing mode and, if necessary, one or several other complexing components, after which washed filtration precipitates are dried after optional squeezing and mechanical removal of moisture. Washing and drying stages are performed on the same filter.

EFFECT: significantly simplified process due to avoided repetitive redispersing of catalyst followed by transferring filtration precipitate to another equipment.

9 cl, 13 ex

FIELD: various-destination catalysts.

SUBSTANCE: invention relates to production of copper-zinc-aluminum catalysts appropriate for low-temperature steam conversion of carbon monoxide, low-temperature methanol synthesis, and hydrogenation-dehydrogenation of various organic compounds. Catalyst preparation process comprises preparing ammonia-carbonate solutions of copper and zinc, treating aluminum-containing raw material with ammonia-carbonate solution of zinc, mixing thus treated or its mixture with untreated aluminum-containing raw material with copper and zinc compounds, holding resulting suspension in reactor at elevated temperature and stirring, separating formed catalyst mass from solution, drying, calcination, and granulation. Specifically, treatment of aluminum-containing raw material with ammonia-carbonate solution of zinc is carried out at 75-90°C and is followed by ageing at stirring until ammonia-carbonate solution of zinc is decomposed and mixing of copper, zinc, and aluminum-containing raw material is conducted in dosed manner while maintaining reactor temperature 75-90°C and specified copper-to-zinc ratio in liquid phase of suspension. Moreover, zinc compounds are introduced into reactor in the form of ammonia-carbonate solution or oxide, or basic carbonate and copper compound in the form of ammonia-carbonate solution so that copper-to-zinc atomic ratio in finished catalyst is (0.55-2.2):1 and atomic content of aluminum ranges from 2.6 to 10.6.

EFFECT: simplified catalyst preparation technology, avoided noxious effluents and gas emissions, and assured preparation of high-activity, stable, and strong catalysts.

3 cl, 1 tbl, 16 ex

FIELD: technical chemistry; catalyst carriers for various heterogeneous processes in chemical industry.

SUBSTANCE: proposed carrier has metal base made from chromium and aluminum alloy and/or metallic chromium and coat made from chromium of aluminum oxides or oxides of chromium, aluminum, rare-earth elements or mixture of them. Method of preparation of carrier includes forming of metal powder containing aluminum and other powder-like components and calcination of carrier at solid phase sintering point; used as additional component of metal powder is powder-like chromium; mixture thus obtained is subjected to mechanical activation and is placed in mold accessible for water vapor, after which it is subjected to hydro-thermal treatment and molded product is withdrawn from mold, dried and calcined at respective temperature; then additional layer of aluminum and rare-earth elements oxides or mixture of solutions and suspensions is applied on calcined product followed by drying and calcination.

EFFECT: increased specific surface; enhanced heat resistance of carrier.

8 cl, 1 tbl, 5 ex

FIELD: production of catalysts on base of compounds of copper, zinc and aluminum for low-temperature conversion of carbon oxide with water steam; chemical, and petrochemical industries; production of ammonia and hydrogen.

SUBSTANCE: proposed method consists in mixing the solution of ammonia-carbonate complex of copper with solution of ammonia-carbonate complex of zinc and with oxide or hydroxide of aluminum; suspension thus obtained is heated to 40-50°C, then it is subjected to stirring continued for 1-2 h, after which temperature is raised to 85-97°C and purge gas is introduced, for example nitrogen or carbon dioxide and suspension is mixed at solid-to-liquid ratio of 1:(2.0-4.0); sediment is removed; mixture is dried, calcined and liquid stabilizing additives are introduced into calcined mass at solid-to-liquid ratio of 1: (0.2-1.0) and 1-1.5 mass-% of graphite is added; mixture is stirred, granulated and pelletized. Used as stabilizing additives are chromic, nitric or oxalic acids, or their salts, or carbamide.

EFFECT: enhanced activity and thermal stability.

2 cl, 1 tbl, 20 ex

FIELD: petroleum processing and catalysts.

SUBSTANCE: invention relates to catalyst for steam cracking of hydrocarbons, which catalyst contains KMgPO4 as catalyst component. Catalyst is prepared by dissolving KMgPO4 precursor in water and impregnating a support with resulting aqueous solution of KMgPO4 precursor or mixing KMgPO4 powder or its precursor with a metal oxide followed by caking resulting mixture. Described is also a light olefin production involving steam cracking of hydrocarbons.

EFFECT: increased yield of olefins, reduced amount of coke deposited on catalyst, and stabilized catalyst activity.

21 cl, 4 tbl, 14 cl

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