Catalyst, method of its production (versions) and method of liquid-phase alkylation of isobutane by olefins c2-c4 in its presence

FIELD: process engineering.

SUBSTANCE: invention relates to petrochemistry, particularly, to production of zeolite-based catalyst for alkylation of isobutane by olefins and may be used in oil processing. Invention covers catalyst of alkylation of isobutane by zeolite-based olefins that contains aluminium oxide and silicon dioxide at silicon dioxide-to-aluminium oxide molar ratio equal to 2.8-7.0, sodium oxide, rare-earth element, oxides of active metals, which contains oxides of platinum and/or palladium and/or rhenium and/or ruthenium at the following ratio of components, in wt %: sodium oxide - 0.26-0.8, calcium oxide - 0.8-4.2, rare earth element oxide - 12.0-20.0,oxides of platinum and/or or palladium and/or molybdenum and/or nickel and/or cobalt - 0.02-2.0, zeolite with SiO2/Al2O3 equal to 2.8-7.0, making the rest. It covers also two versions of the method of catalyst production comprising zeolite treatment by water solutions of salts of calcium, rare earth element and ammonium at increased temperature and pressure of saturated vapors for time period required for conversion of zeolite into rare-earth calcium zeolite, its washing, drying and calcinating. In compliance with this method, first, rare-earth calcium zeolite is impregnated with unipolar water unless air escapes from zeolite pores and, then, processing is performed by impregnation with water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or molybdenum and/or nickel and/ or cobalt taken in amount that ensures said content of metal oxide in finished catalyst. It comprises also drying, calcinating, or applying on rare-earth metal calcium zeolite of water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or molybdenum and/or nickel and/or cobalt. The process includes two stages: first, cold impregnation at not over 30°C, and, second, at, at least, 70°C, and finally drying, tabletting and calcinating.

EFFECT: increase in catalyst activity approximating to 100 wt %, isotope selectivity approximating to 73.5 wt %, yield of target alkyl benzene by 10-15 wt %.

16 cl, 10 ex, 2 tbl

 

The invention relates to the field of petrochemicals, in particular the production of a catalyst based on zeolite and method of alkylation of isobutane With olefins2÷4in his presence, and can be used in the oil industry.

Due to the increased requirements to the quality of gasoline (limit of polynuclear aromatic hydrocarbons) has dramatically increased interest in the process of alkylation of isobutane by olefins. The product of the process - alkylbenzene consists almost completely of isoparaffin hydrocarbons, mainly isooctanol (Σ-C8). Alkilbenzin does not contain aromatic hydrocarbons, however, has a high octane number. The development of technology suitable for implementation in industry, primarily depends on the development of catalytic systems having a high activity, selectivity in obtaining the desired products and stability. In the present alkylation process on an industrial scale as catalysts are mineral acids - sulfuric, and hydrofluoric. However, their use raises a number of problems associated with their high toxicity and korrozionnostojkoj. As an alternative wide range of catalysts of different qualitative and quantitative composition, however, the prospects for the s catalysts based on zeolites, in which to increase activity and selectivity impose various modifiers.

The closest in technical essence and the achieved result is a catalyst based on zeolite type pajazit for alkylation of isobutane With olefins2÷4described in SU 1309383, B01J 29/12, C07B 37/00, 20.10.1996, According to known technical solution, the catalyst has the following composition, % wt.: the sodium oxide 0,26÷0.8; oxide of rare earth element to 12.0÷20,0; calcium oxide 0,8÷4,2; platinum oxide or palladium 0,02÷1,2; aluminium oxide and silicon dioxide - the rest. Test CC in the alkylation of isobutane with ethylene at 90°C, the speed of feed of 1.3 h-1and duration 7 h shows the yield of alkylate 190÷210% of the mass.

The disadvantage of the catalyst is low selectivity for the target product Σ-C8(total isooctane) - 67.4% of the mass. when the alkylation of isobutane with ethylene and butenes, and in the alkylation of isobutane with propylene at 20°C and a duration of 3 h shows a low yield of alkylate - 100 wt. -%, while the selectivity for the target product Σ-C8(total isooctane) and do is 26.8 per cent of the mass.

The objective of the proposed technical solution is the development of a catalyst having a high activity, stability and selectivity for the target product Σ-C8carried out, and the alkylation of isobutane With olefins 2÷4and also in the development of a method of producing such a catalyst.

The problem is solved in that the proposed catalyst for the alkylation of isobutane by olefins C2÷C4on the basis of a zeolite containing aluminum oxide and silicon dioxide in a molar ratio of silica: alumina, equal to 2.8÷7,0, oxides of sodium, calcium, rare earth element and the oxides of active metals, as oxides of active metals contains oxides of platinum and/or palladium, and/or molybdenum and/or Nickel and/or cobalt in the following ratio of components, wt%:

the sodium oxide0,26÷0,8
calcium oxide0,8÷4,2
the oxide of rare earth element12,0÷20,0
the oxide of platinum,
and/or palladium oxide,
and/or molybdenum oxide,
and/or Nickel oxide,
and/or cobalt oxide0,02÷2,0
zeoli the ratio
SiO2/Al2O3equal to 2,8÷7,0the rest of it.

The proposed catalyst may optionally contain a binder, preferably aluminum hydroxide bemani patterns in number 10÷50 wt%. with respect to the finished catalyst, and as it contains zeolite zeolite type pajazit a molar ratio of SiO2/Al2O3equal to 2,8÷7,0.

The problem is solved also by the fact that the method of preparation of the catalyst of the alkylation of isobutane With olefins2÷4based on zeolite, including his handling of aqueous solutions of salts of calcium, rare earth element and ammonia at elevated temperature and pressure saturated vapor for a time sufficient to convert the zeolite in rare-earth calcium zeolite, and the application to it of the oxides of active metals by impregnation with aqueous solutions of salts of active metals, then rinsing and drying, in which before application of the active metals, first carry out the impregnation of the obtained rare earth calcium zeolite unipolar water to stop coming out of the air from the pores of the zeolite, and then the application of the oxides of the active metals of platinum and/or palladium, and/or molybdenum, and/or Nickel and/or cobalt, taken in quantity is TBE, providing the specified content of the oxide of the corresponding metal in the finished catalyst, and the application of active metals is carried out in two stages: in the first stage by cold soaking at a temperature not exceeding 30°C, the second at a temperature of at least 70°C., and then drying, pelleting and calcining.

In the particular case of the proposed method, the zeolite is mixed with a binder, preferably aluminum hydroxide bemani structure and solution of a mineral or organic acid, preferably nitrogen, at a pH in the range equal to 2÷4, the resulting mixture was evaporated, formed by extrusion, the extrudates provalivajut, dried and calcined.

And as zeolite used zeolite type pajazit a molar ratio of SiO2/Al2O3equal to 2,8÷7,0, and treatment of the zeolite with aqueous solutions of salts of calcium, rare earth element and ammonia is carried out at a temperature of 140÷220°C.

As salts of the active metals used chloroplatinate ammonium or tetraamine platinum, or tetraamine palladium, or paramolybdate ammonium, or nitrate of Nickel, or cobalt nitrate.

Cold impregnation spend at least 1 hour, and hot for 0.5÷2 hours, preferably 0,75÷1.0 hour.

The problem is solved also by the fact that the second option proposed implementation of the act is both the preparation of the catalyst of the alkylation of isobutane With olefins 2÷4based on zeolite, including his handling of aqueous solutions of salts of calcium, rare earth element and ammonia at elevated temperature and pressure saturated vapor for a time sufficient to convert the zeolite in rare-earth calcium zeolite and the application to it of the oxides of active metals by impregnation with aqueous solutions of salts of active metals, then rinsing and drying, in which the application of rare earth calcium zeolite oxides of active metals - platinum and/or palladium, and/or molybdenum and/or Nickel and/or cobalt from solutions of salts of the respective metals in unipolar water, taken in an amount providing the specified content of the oxide of the corresponding metal in the finished catalyst, and the application of active metals is carried out in two stages: in the first stage by cold soaking at a temperature not exceeding 30°C, the second at a temperature of at least 70°C., and then drying, pelleting and calcining.

A special case of the method according to the second variant, when impregnated with oxides of active metals zeolite is mixed with a binder, preferably aluminum hydroxide bemani structure and solution of a mineral or organic acid, preferably nitrogen, at a pH in the range of 2÷4, the resulting mixture was evaporated, formed what Ecodom extrusion, the extrudates provalivajut, dried and calcined.

As the zeolite used zeolite type pajazit a molar ratio of SiO2/Al2O3equal to 2,8÷7,0.

Treatment of the zeolite with aqueous solutions of salts of calcium, rare earth elements and ammonia is carried out at a temperature of 140÷220°C.

As salts of the active metals used chloroplatinate ammonium or tetraamine platinum, or tetraamine palladium, or paramolybdate ammonium, or nitrate of Nickel, or cobalt nitrate.

Cold impregnation spend at least 1 hour, and hot for 0.5÷2 hours, preferably 0,75÷1.0 hour.

The problem is solved also by the fact that the method of liquid-phase alkylation of isobutane With olefins2÷4at high pressure and temperature in the presence of the above-described zeolite catalyst.

The technical result, which can be obtained from the present invention is as follows:

- increase the activity of the catalyst for the conversion of olefins, almost to 100 wt. -%;

- increase the selectivity of the catalyst in the process of liquid-phase alkylation of isobutane With olefins2÷4on target product - isooctane (ISO-C8) to 73,5% wt.;

- increase the yield of the target product (alkylbenzene) 10÷15% of the mass.

The following examples, the sludge is astronout the proposed solution, but in no way limit it.

Obtaining catalysts and carrying out the reaction liquid-phase alkylation in the presence of

Example 1

Rare earth calcium zeolite receive according to the method described in patent SU 936991, B01J 37/30, 23.06.1982, With this purpose, 40 g of powdered zeolite type pajazit a molar ratio of SiO2/Al2O3equal to 4.0, loaded into an autoclave and pour a solution of calcium chloride (concentration of 60 g/l, the amount of 260 ml). The autoclave is heated up to 160°C and incubated for 3 hours At the end of processing, the autoclave is cooled, pour the used solution, pour the solution of an industrial mixture of nitrates of rare-earth elements (concentration 30 g/l, the amount of 210 ml) and again heated to 160°C, incubated for 3 hours and cooled.

After cooling and separation of the mother liquor zeolite is washed with demineralized water (condensate). Cake zeolite is dried, pressed into pellets and calcined.

Then obtained, thus, rare-earth calcium zeolite is treated first unipolar water, which is obtained in an electrochemical reactor RAG-1 (units of type STEL) (method described in Bahir V.M. Modern technical electrochemical systems for disinfection, purification and activation of water. - M.: VNIIIMT, 1999. - 84; - Il.). Unipolar water is served with the aim of chemical mod is fitiavana surface by chemisorption of hydrogen ions (H +), the intensification and the uniformity of the process it further impregnation of the active components, removal from the pores of the zeolite air to gently moisturize and thereby preventing the cracking catalyst, washing the dust and crumbs.

Next, a portion of the rare-earth-calcium zeolite pour mixture solutions of the active metals. In this example, the solution terramicina palladium, cobalt nitrate and ammonium nitrate (concentration 0.05 g/l palladium and 6.67 g/l for cobalt), in an amount to provide full coverage of the granules.

The application of active metals in the rare earth calcium zeolite is carried out in two stages: on the first carrying cold impregnation with solutions of active metals with stirring for 1 hour at 25°C. After holding the cold impregnation in the second stage impregnating solution is heated to a temperature of 75°C and are impregnated rare earth calcium zeolite a further 1 hour.

Then in the impregnating solution was added 0.02 g of oxalic acid in aqueous solution with a concentration of 50 g/DM3and 0.02 g of 30%aqueous solution. Processing continues 0.25 hours under stirring, then the solution is drained, the catalyst is dried and calcined.

Then the solution containing no active metal is poured, tablets washed with condensate, dried and calcined.

Get cat is the lyst following chemical composition, % mass.:

Na2O - 0,5; La2O3- 20,0; CaO - 1,4; PdO - 0,01; CoO - 1,5; Al2O3+SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction of liquid-phase alkylation of isobutane (isobutane fraction containing isobutane - to 99.5 wt. -%, the rest n-butane) an ethylene concentration of 99.5 wt.% primary substance at a ratio of ISO-C4:C2"=17:1, a temperature of 90°C, flow rate of feed of 1.3 h-1and duration of the catalyst 7 h in laboratory flow-through installation.

The catalyst loaded into the reactor in such a way that over and under it layer is crushed quartz (fraction of particle sizes substantially higher fraction of catalyst)serving as a device for preventing removal of the catalyst stream. The top layer of quartz also promotes uniform distribution of the flow of raw materials on the catalyst surface, and tests the alkylation unit for leaks with nitrogen at P=1,5÷2,0 MPa.

After checking the leak tightness test of the catalyst in the alkylation of isobutane by olefins C2÷C4.

The only contact alkylating component ethylene with a catalyst leads to the flow of its oligomerization on the surface of the catalyst and rapid deactivation of the latter. To avoid oligomerizes and, the reactor, with ready-to-use catalyst, pre-filled with isobutane.

After filling the system with isobutane close the valve on isobutane tank and use the pump to start the flow in the reactor, the raw material mixture of raw capacity. As a result of interaction alkilirutego and alkylating components in the presence of a catalyst to form a liquid reaction products and unreacted excess isobutane, which is taken at the outlet of the reactor in a cooled trap.

Liquid product alkylate is subjected to stabilize, and then analyze the chromatograph "Crystallux-4000M using getaccountinfo chromatography on a column of SE-30. The work was used the program "NetChrom intended for automation chromatograph "Crystallux-4000M". This program provides treatment of the chromatographic signals.

Determine the full composition of the alkylate - it is a mixture of isomers paraffin hydrocarbon, C5÷C9and its estimated octane number.

The resulting gaseous products of stabilization is mainly unreacted excess isobutane, also analyzed by getaccountinfo chromatography: column of alumina.

The output of the reaction products - alkylate calculated by the following equation of reaction is AI:

2 Ethylene + Isobutane → 2,2,4-Trimethylpentane

(100 octane number research method - EYES)

Conversion of olefin characterizes the completeness of the use of raw materials in this process and is the ratio of the number of converted olefins (OL) taken, expressed in %, and is calculated by the formula:

X(OL) - conversion OL, wt. -%;

(OL)raw concentration OL in raw materials, wt. -%;

m(raw) - the mass of the raw material, g;

(OL)cont. the concentration of AL in the product, wt. -%;

m(product - weight of the product,

The output of alkylbenzene on the olefins in the feedstock (exit AB taken on OL), expressed in percent, is determined by the formula:

η(AB) - output AB, wt. -%;

m(product) - product mass, g;

(OL)raw concentration OL in raw materials, wt. -%;

m(raw) - weight raw materials,

The selectivity of the process is judged by the content isooctanol fraction in the mixture of the products of alkylbenzene as the most valuable component of gasoline obtained by mixing isooctanol gasoline catalytic cracking of vacuum gas oil and reforming low-octane gasoline.

The selectivity of the reaction is the relative concentration isooctanol fraction of the reaction products, calculated according to the formula:

δ(AB) - selectivity re the functions, wt. -%;

C(ΣC8- concentration isooctanol fraction in product, wt. -%;

(Cont.) - the total concentration of the reaction products, % of the mass.

In accordance with the submitted calculations yield alkylbenzene on olefins in missed raw material in this example is 196% of the mass. (1.2 more than in the prototype).

The selectivity of the process is to 69.7% of the mass.

The results are given in table 2.

Example 2.

The catalyst prepared according to example 1, only for the purpose of varying the composition of the processing of a mixture of nitrates of rare-earth elements and ammonium are for 4 h at 200°C, the concentration of the mixture of solutions terramicina palladium and ammonium nitrate 0.68 g/l palladium, and the mixture is injected solution of Nickel nitrate is 0.22 g/l of Nickel.

The catalyst has the following chemical composition, % wt.:

Na2O - 0,26; La2O3- 17,4; CaO - 0,8; PdO - 0,11; NiO - 0,05; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction of liquid-phase alkylation of isobutane with butylenes in the ratio of ISO-C4:C4"=27:1, a temperature of 90°C, flow rate of 1.2 h-1, the duration of the catalyst 7 h according to the method described in example 1, but as the alkylating component use a butane-butylene fraction obtained from the catalytic cracking (B is f), hydrocarbon composition of which is determined by the method getaccountinfo chromatography (GC "Crystallux-4000M with a flame ionization detector) and are presented in table 1.

Table 1
Characteristics of the butane-butylene fraction
HydrocarbonsConcentration, % mass.
isobutane30,280
n-butane8,076
TRANS-butylene18,228
butylene13,003
isobutylene15,283
CIS-butylene13,876
isopentane1,316

The reaction product yield of alkylate are calculated according to the following reaction equations:

The output of alkylbenzene on the olefin selectivity calculated, as shown in example 1.

The results are presented in table 2.

Example 3.

40 g of powdered zeolite type with mo the popular attitude SiO 2/Al2O3equal to 5, is subjected to all the operations of example 1, only the processing take 180 ml of a mixture of nitrates of rare-earth elements and ammonium, and the concentration of the mixture of solutions terramicina palladium and ammonium nitrate is 5,04 g/l palladium, and the mixture injected a solution of ammonium molybdate (paramolybdate ammonium) of 0.038 g/l for molybdenum.

The catalyst has the following chemical composition, % wt.:

Na2O - 0,48; La2O3- 18,1; CaO - 1,4; PdO - 1,2; MoO3- 0,01; Al2O3+ SiO2- the rest (SiO2/Al2O3=5).

The catalyst was tested under the conditions of example 1.

The output of alkylbenzene on the olefin selectivity calculated, as shown in example 1.

The results are presented in table 2.

Example 4.

100 g of granulated zeolite of type X with a molar ratio of SiO2/Al2O3equal to 2.8, loaded into an autoclave and pour a solution of calcium chloride (concentration 40 g/l, the amount of solution 1020 ml). The autoclave is heated to 150°C, incubated 3 h and cooled. The spent solution is drained and operation repeat, processing the sample to 450 ml of a mixture of solutions of nitrate of rare earth elements and ammonium (concentration 15 g/l in La2O3). Then, the zeolite is washed with demineralized water and filtered to obtain a wet cake.

To implement the AI of the second variant of the method of preparation of the catalyst sample (10 g dry) pellet rare earth-calcium zeolite pour 20 ml of chloroplatinate ammonium (concentration of 0.25 g/l for Pt), of Nickel nitrate (concentration to 6.67 g/l as Ni) and unipolar with water to cover the mixture. The mixture was incubated at room temperature with periodic mixing until a uniform distribution of metal throughout the volume.

Application of active metals in the rare earth calcium zeolite is carried out in two stages: first, carrying cold soaking for 1 hour at a temperature of 25°C, and then 1 hour at a temperature of 85°C.

In the second stage in the impregnating solution in 0.75 hour add 0.005 g of oxalic acid in aqueous solution with a concentration of 50 g/DM3and 0.025 g of hydrogen peroxide in the form of a 30%aqueous solution, and processing continues 0.25 hours under stirring.

Then the mass is filtered off, washed, dried, tabletirujut and calcined.

The catalyst has the following chemical composition, % wt.: Na2O - 0,8; La2O3- 15,5; CaO - 2,4; PtO - 0,06; NiO - 1,5; Al2O3+ SiO2- the rest (SiO2/Al2O3=2,8).

The catalyst was tested under the conditions of example 1.

The output of alkylbenzene on the olefin selectivity calculated, as shown in example 1.

The test results are shown in table 2.

Example 5.

Rare earth calcium zeolite prepared as in example 4, only a portion (10 g dry) pellet rare earth-calcium zeolite is mixed with a binder - GI is roxicam aluminum bemani structure and solution of nitric acid, at a pH in the range of 2÷4, the resulting mixture was evaporated, formed by extrusion, the extrudates provalivajut, dried and calcined. Then thus obtained rare-earth calcium zeolite treated unipolar water, soaked in a mixture solution of ammonium nitrate, terramicina platinum (with a concentration of 2.4 g/l for Pt), cobalt nitrate (concentration 0,044 g/l as Co) and paramolybdate ammonium concentration is 0.22 g/l as Mo) in two stages: first for 1 hour at a temperature of 25°C, and then 1 hour at a temperature of 85°C. In the second stage in the impregnating solution in 0.75 hour add 0.005 g of oxalic acid in aqueous solution with a concentration of 50 g/DM3and 0.025 g of hydrogen peroxide in the form of a 30%aqueous solution, and processing continues 0.25 hours under stirring. The extrudates provalivajut, dried and calcined.

The catalyst has the following chemical composition, % wt.:

Na2O - 0,6; La2O3- 15,1; CaO - 2,0; PtO - 0,55; CoO - 0,01; NGO3- 0,06; Al2O3+ SiO2- the rest (SiO2/Al2O3=2,8).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 2.

The results are given in table 2.

Example 6.

40 g of powder-type zeolite with a molar ratio of SiO2/Al2O3equal to 5, is loaded into the autoclave and pour the solution floridakellie (concentration of 60 g/l, the number 3320 ml). The autoclave is heated up to 160°C and incubated for 3 hours At the end of processing, the autoclave is cooled, pour the used solution, pour the solution of an industrial mixture of nitrates of rare-earth elements (concentration 30 g/l, number 190 ml) and again heated to 160°C, incubated for 3 hours and cooled.

After cooling and separation of the mother liquor zeolite is washed with demineralized water (condensate) and filtered to obtain a wet cake. Further, as described in example 4 is applied in two stages active metal by treatment with a solution of ammonium nitrate and terramicina platinum concentration of 7.2 g/l in platinum.

Then the obtained rare earth calcium zeolite with an active metal is mixed with a binder is aluminum hydroxide bemani structure and solution of nitric acid, at a pH in the range of 2÷4, the resulting mixture was evaporated, formed by extrusion, the extrudates provalivajut, dried and calcined.

The catalyst has the following chemical composition, % wt.:

Na2O - 0,5; La2O3- 14,8; CaO - 1,2; PtO - 0,02; Al2O3+ SiO2- the rest (SiO2/Al2O3=5).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 1.

The results are shown in table 2.

Example 7.

The catalyst prepared according to example 1, but with double the number of the om treatment with a solution of calcium chloride and processing take 140 ml of a mixture of nitrates of rare-earth elements and ammonium. Next, a portion of the obtained rare earth-calcium zeolite is treated in two stages, as described in example 4, a solution of ammonium nitrate and paramolybdate ammonium (with a concentration of 7.5 g/l as Mo).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,6; La2O3- 12,1; CaO - 3,0; NGO3- 2,0; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction of liquid-phase alkylation of isobutane with propylene, with the concentration of 99.5% of the mass. primary substance at a ratio of ISO-C4:C3"=8:1, 20°C and the duration of operation of the catalyst 3 o'clock

The reaction product yield of alkylate are calculated according to the following reaction equations:

Calculating the yield of the reaction products and the selectivity of the process, as shown in example 1.

The results are shown in table 2.

Example 8.

Dealumination sodium form of type zeolite with a molar ratio of SiO2/Al2O3equal to 5.1, is carried out by treatment with a mixture of hydrochloric acid solutions and trylon B at 95°C until the molar ratio of SiO2/Al2O3=7,0. Then rare earth-calcium form of the catalyst prepared according to example 1, except that the treatment with a mixture of nitrates of rare-earth elements and ammonium are for 3 h at 140°C. Dalnas the processing of the received sample lead by example 4 in two stages with a mixture of solutions of chloroplatinate platinum, ammonium nitrate and cobalt nitrate (concentration of 0.58 g/l for Pt and 0.45 g/l Co).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,5; La2O3- 15,4; CaO - 0,8; PtO - 0,11; CoO - 0,1; Al2O3+ SiO2- the rest (SiO2/Al2O3=7).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 1.

The results are shown in table 2.

Example 9.

The catalyst prepared according to example 1, except that the treatment with a mixture of nitrates of rare-earth elements and ammonium are for 3 h at 150°C, and the resulting rare earth-calcium zeolite is treated according to example 4 in two stages with a mixture of solutions of ammonium nitrate, Nickel nitrate and paramolybdate ammonium concentration 0,044 g/l of Nickel and 4.5 g/l as Mo).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,5; La2O3- 16,0; CaO - 0,4; NGO3- 1,2; NiO - 0,01; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 1.

The results are shown in table 2.

Example 10.

The catalyst prepared according to example 7, only the processing solution of calcium chloride is carried out at 200°C, and the resulting rare earth-calcium zeolite is treated according to example 4 in two stages with a mixture of solutions of ammonium nitrate, tetramic is the palladium, terramicina platinum, Nickel nitrate, paramolybdate ammonium and nitrate cobalt (with a concentration of 0.05 g/l palladium, 0.05 g/l for platinum, 0,44 g/l of Nickel, 0.75 g/l for Mo, 0.27 g/l Co) and unipolar water.

The catalyst has the following chemical composition, % wt.:

Na2O - 0,7; La2O3- 10,1; CaO - 6,0; PtO - 0,01, PdO - 0,01; NGO3- 0,2; NiO - 0,1; Soo - 0,06; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 1.

The results are shown in table 2.

Example 11.

The catalyst prepared according to example 7, only a portion of the obtained rare earth-calcium zeolite is treated in two stages, as described in example 4, a solution of ammonium nitrate and Nickel nitrate (with a concentration of 8.8 g/l for Ni).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,6; La2O3- 12,1; CaO - 3,0; NiO - 2,0; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction of liquid-phase alkylation of isobutane with propylene as described in example 7.

Calculating the yield of the reaction products and the selectivity of the process, as shown in example 1.

The results are shown in table 2.

Example 12.

The catalyst prepared according to example 7, only a portion of the obtained rare earth-calcium zeolite is srabatyvayut in two stages, as described in example 4, a solution of ammonium nitrate and cobalt nitrate (concentration of 8.8 g/l Co).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,6; La2O3- 12,1; CaO - 3,0; CoO - 2,0; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction of liquid-phase alkylation of isobutane with propylene as described in example 7.

Calculating the yield of the reaction products and the selectivity of the process, as shown in example 1.

The results are shown in table 2.

Example 13.

The catalyst is prepared for all operations example 1, except that the impregnation of the active metals take a mixture of solutions of ammonium nitrate, Nickel nitrate and cobalt nitrate (concentration 2,22 g/l of Nickel and 2,22 g/l Co).

The catalyst has the following chemical composition, % wt.:

Na2O - 0,5; La2O3- 16,0; CaO - 0,4; COO3- 0,5; NiO - 0,5; Al2O3+ SiO2- the rest (SiO2/Al2O3=4).

The catalyst was tested in the reaction liquid phase alkylation in the conditions of example 1.

The results are shown in table 2.

Thus, the proposed solution allows to increase the activity for the conversion of olefins to almost 100% of the mass, the product yield (alkylbenzene) 10÷15% of the mass. and the selectivity of the alkylation of isobutane by olefins C2 ÷C4on target product - isooctane (ISO-C8and thereby improve the quality of alkylbenzene to 73,5% of the mass. compared with 67.4% of the mass. the prototype, in the case of use as alkylating component etileno or butylenes, and to 60.3% of the mass, compared to 26.8% of the mass. for prototype, if the alkylating component used propylene.

Table 2
The results of the tests of the catalysts in the reaction of liquid-phase alkylation
IndicatorsExamples
12345678910111213
Na2O0,50,260,480,80,60,5 0,60,50,50,70,60,60,48
REE20,017,418,115,515,114,812,115,416,0the 10.112,112,118,1
CaO1,40,81,42,42,01,23,00,80,46,03,03,01,4
PtO---0,060,550,02-0,11- 0,01---
PdO0,010,111,2------0,01---
Moo3--0,01-0,06-2,0-1,20,2--
NiO-0,05-1,5----0,010,12,0-0,5
Soo1,5---0,01--0,1-0,06-2,00,5
Conversion of olefins, wt.%9810010097100100100100100100100100100
The product yield, wt.%196211205197204199172192179202175178196
Selectivity for su the IU ISO-C 869,771,369,270,473,567,459,165,763,272,360,360,170,5

1. The catalyst for the alkylation of isobutane With olefins2-C4on the basis of a zeolite containing aluminum oxide and silicon dioxide in a molar ratio of silica : alumina, equal to 2.8-7,0, oxides of sodium, calcium, rare earth element and the oxides of active metals, characterized in that as the oxides of active metals it contains oxides of platinum and/or palladium, and/or molybdenum and/or Nickel and/or cobalt in the following ratio, wt.%:

the sodium oxide0,26-0,8
calcium oxidethe 0.8-4.2V
the oxide of rare earth element12,0-20,0
the oxide of platinum, and/or
the oxide of palladium, and/or
molybdenum oxide, and/or
Nickel oxide, and/or
the cobalt oxideof 0.02 to 2.0
zeolite with a ratio of SiO2/Al2O3equal to a 2.8-7,0,rest

2. The catalyst according to claim 1, characterized in that it further comprises a binder, preferably aluminum hydroxide bemani patterns, in the amount of 10-50 wt.% with respect to the finished catalyst.

3. The catalyst according to claim 1, characterized in that it contains zeolite zeolite type pajazit a molar ratio of SiO2/Al2O3equal to a 2.8-7,0.

4. The method of preparation of the catalyst according to claim 1, comprising processing a zeolite with aqueous solutions of salts of calcium, rare earth element and ammonia at elevated temperature and pressure saturated vapor for a time sufficient to convert the zeolite in rare-earth calcium zeolite, and the application to it of the oxides of active metals by impregnation with aqueous solutions of salts of active metals, then rinsing and drying, characterized in that before applying the active metals first carry out the impregnation of the obtained rare earth calcium zeolite UNIP is popular with water to stop coming out of the air from the pores of the zeolite, and then the deposition of oxides of active metals - platinum and/or palladium, and/or molybdenum and/or Nickel and/or cobalt, taken in an amount to provide the specified content of the oxide of the corresponding metal in the finished catalyst, and the application of active metals is carried out in two stages: in the first stage by cold soaking at a temperature not exceeding 30°C, the second at a temperature of at least 70°C., and then drying, pelleting and calcining.

5. The method according to claim 4, characterized in that the zeolite is mixed with a binder, preferably aluminum hydroxide bemani patterns, and the solution of a mineral or organic acid, preferably nitrogen, at a pH in the range equal to 2-4, the mixture was evaporated, formed by extrusion, the extrudates provalivajut, dried and calcined.

6. The method according to claim 4, characterized in that the zeolite used zeolite type pajazit a molar ratio of SiO2/Al2O3equal to a 2.8-7,0.

7. The method according to claim 4, characterized in that the treatment of the zeolite with aqueous solutions of salts of calcium, rare earth element and ammonia is carried out at a temperature of 140-220°C.

8. The method according to claim 4, characterized in that salts of the active metals used chloroplatinate ammonium, or tetraamine platinum, or tetraamine palladium, or paramolybdate ammonium, or NITR the t of Nickel, or nitrate of cobalt.

9. The method according to claim 4, characterized in that the cold impregnation is conducted for at least 1 h, and hot for 0.5 to 2 h, preferably 0.75 to 1.0 hours

10. The method of preparation of the catalyst according to claim 1, including the processing of aqueous solutions of salts of calcium, rare earth element and ammonia at elevated temperature and pressure saturated vapor for a time sufficient to convert the zeolite in rare-earth calcium zeolite, and the application to it of the oxides of active metals by impregnation with aqueous solutions of salts of active metals, then rinsing and drying, characterized in that exercise drawing on rare earth calcium zeolite oxides of active metals - platinum and/or palladium, and/or molybdenum and/or Nickel and/or cobalt from solutions of salts of the respective metals in unipolar water, taken in an amount to provide the specified content of the oxide of the corresponding metal in the finished catalyst, and the application of active metals is carried out in two stages: in the first stage by cold soaking at a temperature not exceeding 30°C, the second at a temperature of at least 70°C., and then drying, pelleting and calcining.

11. The method according to claim 10, characterized in that the impregnated oxides of the active metals zeolite is mixed with a binder, preferably aluminum hydroxide bemani is tructure, and the solution of a mineral or organic acid, preferably nitrogen, at a pH in the range equal to 2-4, the mixture was evaporated, formed by extrusion, the extrudates provalivajut, dried and calcined.

12. The method according to claim 10, characterized in that the zeolite used zeolite type pajazit a molar ratio of SiO2/Al2O3equal to a 2.8-7,0.

13. The method according to claim 10, characterized in that the treatment of the zeolite with aqueous solutions of salts of calcium, rare earth elements and ammonia is carried out at a temperature of 140-220°C.

14. The method according to claim 10, characterized in that salts of the active metals used chloroplatinate ammonium, or tetraamine platinum, or tetraamine palladium, or paramolybdate ammonium, or nitrate of Nickel, or cobalt nitrate.

15. The method according to claim 10, characterized in that the cold impregnation is conducted for at least 1 h, and hot for 0.5 to 2 h, preferably 0.75 to 1.0 hours

16. The method of liquid-phase alkylation of isobutane With olefins2-C4at high pressure and temperature in the presence of a zeolite catalyst, wherein the process is conducted in the presence of a catalyst according to any one of claims 1 to 3.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to a method of isomerising vitamin D analogues such as compounds used in synthesis of calcipotriol using a flow-type photoreactor or a photoreactor with continuous flow for preparing said vitamin D analogues. The invention also relates to use of intermediates produced using said method to produce calcipotriol or monohydrate of calcipotrol or its pharmaceutical medicinal forms.

EFFECT: improved properties of compounds.

21 cl, 4 ex, 1 tbl

FIELD: organic synthesis and catalysts.

SUBSTANCE: invention relates to improved method of telomerization of diene with conjugated double bonds, wherein said diene interacts with a compound having active hydrogen atom and selected from group, consisting of alkanols, hydroxyaromatic compounds, carboxylic acids, and water, in presence of telomerization catalyst based on VIII group metal source and bidentate ligand. The latter is depicted by general formula (I): R1R2M1-R-M2R3R4, wherein M1 and M2 independently represent P; R1, R2, R3, and R4 independently represent monovalent aliphatic group or R1, R2, and M1 jointly and/or R3, R4, and M2 jointly independently represent cycloaliphatic group with 5-12 carbon atoms in cycle, wherefrom one atom is M1 or M2; and R represents (i) bivalent organic bridge group, which is unsubstituted alkylene group or alkylene group substituted by lower alkyl groups optionally incorporating oxygen as heteroatom, or (ii) group containing two benzene rings bound to each other or to alkylene groups, which in turn are linked to M1 and M2. Invention also relates to novel bidentate ligands, which can be utilized in the method of invention and having following general formulas: R1R2M1-V-M2R3R4 (II) and Q1Q2M1-Q5-Ar1-Q6-M2Q3Q4 (III). Invention further relates to improved method for production of 1-octene involving 1,3-butadiene telomerization step to form 1-substituted 2,7-octadiene.

EFFECT: expanded synthetic possibilities in conjugated dienes area.

10 cl, 1 dwg, 1 tbl, 10 ex

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention concerns catalytic process for obtaining isooctane fractions via alkylation of isobutane with butylene fractions. Process involves catalytic complex having following composition: MexOy*aAn-*bCnClmH2n+2-m, wherein Me represents group III-IV metal, x=1-2, y=2-3, and An- anion of oxygen-containing acid selected from sulfuric, phosphoric, molybdenic, and tungstenic acid, or mixture thereof in any proportions; a=0.01-0,2, b=0.01-0.1; bCnClmH2n+2-m is polychlorine-substituted hydrocarbon with n=1-10 and m=1-22, dispersed on porous support and containing hydrogenation component. Alkylation process is carried out at temperature not exceeding 150°C, mass flow rate of starting mixture not higher than 3 g/g cat*h, pressure not higher than 40 atm, and in presence of 10 mol % hydrogen.

EFFECT: increased catalyst stability and selectivity.

5 cl, 3 tbl, 20 ex

FIELD: heterogeneous catalysts.

SUBSTANCE: catalyst contains porous carrier, buffer layer, interphase layer, and catalytically active layer on the surface wherein carrier has average pore size from 1 to 1000 μm and is selected from foam, felt, and combination thereof. Buffer layer is located between carrier and interphase layer and the latter between catalytically active layer and buffer layer. Catalyst preparation process comprises precipitation of buffer layer from vapor phase onto porous carrier and precipitation of interphase layer onto buffer layer. Catalytic processes involving the catalyst and relevant apparatus are also described.

EFFECT: improved heat expansion coefficients, resistance to temperature variation, and reduced side reactions such as coking.

55 cl, 4 dwg

The invention relates to new phosphorus ylides F.-ly (I)

< / BR>
in which R1, R2and R3represent the amino group R R N, where R' and R" are C1-C6alkyl; R4- H, Me; R5polymer media polystyrene type f crystals of (S)

< / BR>
where n, n' and m are integers greater than or equal to 1

FIELD: petrochemistry.

SUBSTANCE: invention relates to hydrocarbons cracking catalysts; the method describes modification of zeolitealuminumsilica-base catalyst for hydrocarbons cracking by means of soaking of the catalyst in the organisticmetallosiloxane solution amid cavitation processing with the intensively of the interval rate of injection 0.2-0.5 W/m followed by maturing at the ambient temperature, solvent distilling and high-temperature processing.

EFFECT: cracking catalyst which has high cracking intensity and selectivity was received.

3 cl, 9 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to the method of production of purification catalysts of internal combustion engines exhaust gases; the method of preparation of purification catalysts of internal combustion engines exhaust gases is described herein, the method is characterized by application of cordierite carriers of the cellular structure, formation of the inert layer of aluminum and silicon hydrate on the carrier by means of processing with the caustic soda water solution at the ambient temperature followed by soaking the carrier in the reactor with the inert layer with the cerium salt water solutions and precursor that is represented by perchlorate palladium (II) received directly during the solution of perchlorate palladium (II) in the water in the presence of perchloric acid; thereafter the reduction of palladium by means of hydrogen on the surface of the catalyst is conducted in the above reactor at the atmospheric pressure and ambient temperature.

EFFECT: precipitation and facilitation of the catalysts preparation technology.

1 dwg, 1 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: invention relates to petrochemical and chemical industry, particularly a method of preparing moulded catalysts for conversion of methane into aromatic hydrocarbons and hydrogen in nonoxidative conditions. The invention describes a catalyst for a nonoxidative methane conversion process, containing high-silica zeolite H-ZSM-5, a binding additive - calcium form of montmorillonite, modifying elements - molybdenum and cobalt, where content of the binding additive in the catalyst is not more than 40.0 wt %, while content of molybdenum and cobalt is not more than 3.0 wt % and 1.0 wt %, respectively. Described is a method of preparing a catalyst, involving modification of zeolite with promoting elements through successive wetness impregnation of zeolite H-ZSM-5 with molybdenum and cobalt salt solutions, followed by calcination, and then mixing the zeolite modified with metals with a binding additive suspension in a given proportion to obtain a moulding mass and moulding said mass into granules in a moulding device. The invention also describes a method for nonoxidative conversion of methane in the presence of the catalyst described above.

EFFECT: high efficiency of the nonoxidative methane conversion process owing to high activity and stability of the catalyst.

4 cl, 7 ex, 1 tbl

FIELD: process engineering.

SUBSTANCE: invention relates to catalytic filters for cleaning diesel engine exhaust gases. Proposed filter comprises inlet and outlet and axial length coated by first catalyst comprising platinum group metals on carrier materials and differs from known designs in that said carrier materials are selected from the group including aluminium oxide, silicon dioxide, titanium dioxide, zirconium dioxide, cerium dioxide and mixes thereof, or mixed oxides. Note here that first catalyst additionally comprises at least one zeolite to accumulate hydrocarbons starting from filter inlet. Note also that section of said filter length is coated by second catalyst that contains no zeolite. Invention covers the method of fabricating said filter wherein both catalyst are applied on said filter as suspension coat. Besides it covers application of said filter for decreasing the content of carbon, hydrocarbon and ash particles in diesel engine exhaust gases.

EFFECT: improved conversion of hydrocarbons into carbon oxide.

10 cl, 2 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing ethylene on modified aluminium oxide catalysts during dehydration of ethanol. Described is a catalyst for producing ethylene during dehydration of ethanol, containing aluminium oxide and chlorine in amount of 1.0-4.0 wt %. Described is a method of producing the catalyst by saturating aluminium oxide with hydrochloric acid, followed by drying and calcination, thereby obtaining a catalyst containing aluminium oxide and chlorine in amount of 1.0-4.0 wt % with specific surface of 150-300 m2/g and pore size distribution of 3-30 nm. Described is a method of producing ethylene via dehydration of ethanol using the catalyst described above at 350-400°C and contact time of 0.3-1 s.

EFFECT: high activity and selectivity of producing ethylene from ethanol.

11 cl, 10 ex, 3 tbl

FIELD: technological processes.

SUBSTANCE: present invention relates to a catalyst for hydrocarbon production from synthesis gas, to method of its production, method of such catalyst regeneration and method of hydrocarbon production with application of such catalyst. A catalyst is described to produce hydrocarbon from synthesis gas, in which metal cobalt or metal cobalt and cobalt oxides; and zirconium oxides are applied onto a catalyst substrate, which mainly consists of a silicon dioxide. This catalyst is characterised by the fact that content of admixtures in the catalyst makes less or is equal to 15 wt %. Versions of the method are described to produce such catalyst, where the catalyst is produced by simultaneous or separate application of cobalt and zirconium compounds onto a catalyst substrate by impregnation method, impregnation method by moisture capacity, by method of deposition or method of ion exchange and performance of restoration treatment or baking and restoration treatment. Versions are described to regenerate such catalyst, where the catalyst with reduced activity is treated with a regenerating gas, containing hydrogen, or regenerating gas is supplied into a reactor, or regenerating gas is supplied into any part of the outer circulation system, and the catalyst and the regenerating gas contact with each other. Versions of the method to produce hydrocarbon from synthesis gas with application of such catalyst are described, where the method is carried out with performance of reaction in a liquid phase using a reactor with a layer of suspended residue or a layer of suspended residue with an external circulation system.

EFFECT: production of catalyst having high activity, durable service life and high resistance to water without loss of strength and wear resistance.

31 cl, 3 tbl, 2 dwg, 21 ex

FIELD: technological processes.

SUBSTANCE: invention relates to a technology of catalysts preparation for conversion of natural gas and may be used in chemical industry, for instance, to produce technical hydrogen. The method is described to prepare a catalyst for natural gas conversion, including treatment of aluminium oxide in presence of potassium hydroxide, production of a homogeneous paste, forming granules from it, their curing, drying and baking, impregnation of the produced carrier in solutions of nickel and aluminium nitrates with subsequent drying and curing, at the same time combined grinding and mixing pf aluminium oxide is carried out with solid potassium hydroxide for 45-60 min with subsequent addition of water to the mixture, baking of granules prior to carrier impregnation is carried out at the temperature of 1200-1250°C for 4-6 hrs, and potassium hydroxide is used in amount of 2-5% from the initial raw materials weight.

EFFECT: reduced energy intensity of the method and increased activity of the finished catalyst at temperature that corresponds to the start of the steam conversion process.

1 tbl, 2 ex

FIELD: technological processes.

SUBSTANCE: invention relates to a technology to prepare catalysts for conversion of hydrocarbons and may be used in chemical industry, for instance, to produce technical hydrogen from natural gas and processes gases required for synthesis of ammonia and methanol. The method is described to prepare a catalyst for conversion of hydrocarbons, including mixing of alumina with a functional additive and 20% nitric acid to produce a homogeneous plastic paste, its moulding, curing, drying and baking, double impregnation of the produced carrier in solutions of nickel and aluminium nitrates with subsequent drying and baking, at the same time mixing of alumina and functional additive is combined with grinding and mechanical-chemical activation for 45-60 min, afterwards the nitric acid is added in amount of 0.18-0.20 l/kg of material, the plastic paste produced during subsequent mixing is formed into blocks of cellular structure, baking prior impregnation of the carrier is carried out at the temperature of 1200-1250°C for 4-6 hrs, and the functional additive is 3-7 wt % of paraffin.

EFFECT: increased external active surface of the catalyst and reduction of its hydraulic resistance.

1 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: invention relates to petrochemisry, gas chemistry, coal chemistry and a catalyst for synthesis of hydrocarbons containing 5 or more carbon atoms from CO and H2 (Fischer-Tropsch synthesis), a method for synthesis of C5+ hydrocarbons using said catalyst and a method of producing said catalyst. Described is a catalyst for synthesis of C5+ hydrocarbons containing a support in form of fluorinated γ-aluminium oxide, 30 wt % cobalt and 0.5 wt % rhenium. Described is a method of producing said catalyst, involving preliminary thermal treatment of the γ-aluminium oxide-based support and then adding cobalt and rhenium via step-by-step saturation with aqueous solutions of cobalt nitrate and ammonium perrhenate and step-by-step thermal treatment, wherein the support used is fluorinated γ-aluminium oxide. The invention also describes a method of producing C5+ hydrocarbons via catalytic conversion of CO and H2 using said catalyst.

EFFECT: high selectivity with respect to formation of desired hydrocarbon products (over 90%) and low selectivity with respect to formation of by-product - methane (less than 4%), wherein the relationship between the output of the desired products and the conversion of carbon oxide (output C5+-Kco) is linear in the conversion interval from 0 to 80-90%.

4 cl, 4 ex, 1 tbl, 6 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to production of zeolite catalysts, catalysts thus produced and method of producing synthetic fuel using produced catalyst. Proposed methods comprises zeolite two-step loading, impregnating zeolite with cobalt compound in solution and drying in air flow after every loading. Invention covers also catalysts produced by said methods. It covers also the method of producing synthetic fuel using produced catalyst, its activation and synthesis of hydrocarbons, particular, aliphatic hydrocarbons C5-C10 from synthesis gas that represents CO and H2.

EFFECT: higher activity and isomeric selectivity.

36 cl, 2 tbl, 13 ex

FIELD: oil and gas production.

SUBSTANCE: invention refers to certain catalytic compositions and processes used for decreasing of sulphur derivatives, usually found in a petrol fraction of liquid-phase catalytic cracking processes. The invention represents a cracking catalyst composition containing zeolite or a component containing zeolite, containing Na2O in amount 0.3 wt % or less combined with a component containing Lewis acid, and a cracking catalyst composition contains Na2O in number of 0.2 % or less, and a component containing Lewis acid within 3 to 75 wt %. Besides the invention involves an advanced method of catalytic cracking of raw hydrocarbons containing organic sulphur derivatives, involves a method for decreasing of sulphur content in gasoline and a method for preparing the cracking catalytic composition.

EFFECT: it is established that amount of sulphur compounds in hydrocarbon supplied at the stage of liquid-phase catalytic cracking can be decreased by at least 15% in comparison with effect of the same composition not containing a component comprising.

59 cl, 14 tbl, 8 dwg, 5 ex

FIELD: chemistry.

SUBSTANCE: unsupported catalyst composition for hydrocracking contains one or more group VIb metals, one or more group VIII base metals, one or more zeolites and optionally heat-resistant oxide material. The said composition is obtained through deposition of group VIb metals, group VIII base metals and optionally heat-resistant oxide material in the presence of a zeolite. The method of preparing the said catalyst composition, in which one or more compounds of group VIb metals are combined with one or more compounds of group VIII base metals, and with zeolite, in the presence of a proton-containing liquid and an alkaline compound, and the catalyst composition is extracted after deposition.

EFFECT: obtaining a catalyst composition with very high activity during hydrogenation of monoaromatic compounds, significantly better selectivity towards middle distillate products.

15 cl, 13 ex, 4 tbl

FIELD: petroleum processing.

SUBSTANCE: petroleum feedstock hydrocracking catalyst is prepared by compounding zeolite Y with aluminonickel(cobalt)-molybdenum(tungsten) oxide system. Specifically, low-alkalinity zeolite Y having silicate modulus 5.5-7.0 and crystallinity at least 70% is mixed with aluminum hydroxide having pseudoboehmite structure in proportion (1-9):1. Thus obtained mix is molded, dried, and calcined under water steam atmosphere to give molded thermally treated zeolite. The latter is impregnated with aqueous Ni(Co) and Mo(W) salt solutions or ground and compounded with aluminonickel(cobalt)-molybdenum(tungsten) oxide system by mixing with aluminum hydroxide and Ni(Co) and Mo(W) salts, after which follow molding and impregnation with aqueous Ni(Co) and Mo(W) salt solutions.

EFFECT: expanded catalyst preparation possibilities.

2 cl, 5 tbl, 4 ex

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