Polymetallic catalyst with strong inter-metal interaction

FIELD: chemistry.

SUBSTANCE: invention relates to the field of hydrocarbon conversion. Claimed is a catalyst for catalytic reforming of a hydrocarbon raw material, which contains at least one metal M of a group of platinum, tin, a phosphorus promoter, a halogen-containing compound, a porous substrate and at least one promoter X1, selected from the group, consisting of gallium and indium. The said catalyst in a reduced form demonstrates, in accordance with Mossbauer spectroscopy 119Sn, a signal, which has a value of quadrupole splitting from 0 to 0.45 mm/s and a chemical shift IS from 1.5 to 2.4 mm/s relative to CaSnO3, with an area of the said signal constituting from 1 to 30% of the total surface of signals. The catalyst is obtained by a method, including the introduction of the said promoter X1 and phosphorus at the stage of the substrate preparation.

EFFECT: increase of selectivity with respect to C5+ compounds and reduction of coke formation.

10 cl, 2 tbl, 11 ex

 

The technical field to which the invention relates

The present invention relates to the field of conversion of hydrocarbons, more specifically, to the reforming of hydrocarbons in the presence of a catalyst to obtain gasoline fractions. The invention relates also to an improved catalytic composition based on at least one platinum group metal, suitable for this conversion, as well as the way they are received.

The level of technology

Many patent documents describe the addition of promoters to the catalyst based on platinum, in order to improve their performance in the reforming of hydrocarbons. Thus, the patent US 2814599 describes the addition of such promoters as gallium, indium, scandium, yttrium, lanthanum, thallium or anemone, catalysts based on platinum or palladium.

Patent US 4522935 describes deposited on a substrate reforming catalysts containing platinum, tin, indium and halogen-containing compound in which the atomic ratio of indium/platinum exceeds 1,14.

Patent FR 2840548 describes the catalyst in the form of a uniform layer of particles containing amorphous matrix, at least one noble metal, at least one halogen and at least one additional metal. This additional metal is preferably selected from the group consisting of tin, germanium,lead, gallium, indium, thallium, rhenium, manganese, chromium, molybdenum and tungsten.

Phosphorus is known, moreover, that its addition increases the yield of hydrocarbon compounds with the number of carbon atoms is strictly larger than 4 (C5+) and, in particular, aromatic products. This feature is patented in the US patents 2890167, US 3706815, US 4367137, US 4416804, US 4426279 and US 4463104. Later in the patent US 2007/0215523 has been described that the addition of small amounts of phosphorus, less than 1 wt.%, stabilizes the substrate, allowing better to keep the specific surface and chlorine when it is used in catalytic reforming process.

Patents US 6864212 and US 6667270 describe substrate containing bismuth and phosphorus, evenly distributed, and used for preparation of the catalyst catalytic reforming of hydrotreated naphtha. According to these patents add only one of bismuth in the substrate reduces the formation of coke and prevent the fall activity, but with reduced output C5+, while adding only one phosphorus increases the yield of this fraction without improving the stability of the catalyst. The combination of these two elements can further reduce the formation of coke, simultaneously giving the best selectivity when the amount of Bi in the range from 0.10 to 0.06 wt.% and the number P of 0.3 wt.%. These two patents do not disclose the use of other e the cops.

In addition, in patent EP1656991 catalyst containing platinum, tin, a substrate of high density, consisting of at least one inorganic oxide including alumina, phosphate and possibly other element selected from germanium, gallium, rhenium, phosphorus, indium or mixtures thereof, characterized in that at least 33 wt.% tin connected with platinum in the form of a special cluster Pt-Sn, which can be detected Mössbauer spectroscopy. The interest in this catalyst due to its high stability and minimizing the formation of coke when it is used, as compared with the known catalysts of the prior art.

The essence of the invention

The invention relates to a catalyst containing at least one metal M of group VIII, tin, phosphorous promoter, a halogenated compound, a porous substrate and at least one promoter X1 is selected from the group consisting of gallium, indium, thallium, arsenic, antimony and bismuth. The catalyst in the reduced form, according to mössbauer spectroscopy119Sn shows a signal having a quadrupole splitting value from 0 to 0.45 mm/s, and the chemical shift IS in the range from 1.5 to 2.4 mm/s relative to CaSnO3the area of the specified signal is from 1 to 30% of the total area of the signals.

Detailed description of the invention

The invention relates to a catalyst containing at least one metal M from the platinum group, tin, phosphorous promoter, a halogenated compound, a porous substrate and at least one promoter X1 is selected from the group consisting of gallium, indium, thallium, arsenic, antimony and bismuth, preferably from the group consisting of gallium, thallium, indium and bismuth, more preferably from the group consisting of gallium and indium, even more preferably the promoter X1 is indium, with the specified catalyst in the reduced form shows, according to mössbauer spectroscopy119Sn, the signal having the quadrupole splitting value from 0 to 0.45 mm/s and the chemical shift IS from 1.5 to 2.4 mm/s relative to CaSnO3the area of the specified signal is from 1 to 30% of the total area of the signals, preferably from 4 to 20%.

The catalysts according to the invention have improved catalytic properties. In particular, increases the selectivity of these catalysts in relation to the formation of compounds C5+ (i.e. compounds containing at least 5 carbon atoms), greatly reduced the formation of coke.

The method of preparation of the catalyst includes the step of introducing phosphorus and promoter or promoters X1 at the stage of preparation of the substrate.

The atomic ratio Sn/M is usually about the 0,5 to 4,0, more preferably from 1.0 to 3.5, and more preferably from 1.3 to 3.2. The ratio X1/M is usually from 0.1 to 5.0, more preferably from 0.2 to 3.0, and most preferably from 0.4 to 2.2. The ratio P/M is typically in the range from 0.2 to 30.0, more preferably from 0.5 to 20.0, and most preferably from 1.0 to 15.0. The metal content is usually from 0.01 to 5 wt.%, more preferably from 0.01 to 2% and even more preferably from 0.1 to 1 wt.%.

The metal M is usually platinum or palladium, more preferably platinum. Halogen-containing compound is typically selected from the group consisting of fluorine, chlorine, bromine and iodine. The content of the halogenated compound is usually from 0.1 to 15.0 wt.%, more preferably from 0.1 to 8.0 wt.%, even more preferably from 0.2 to 5 wt.%. If halogen-containing compound is chlorine, the chlorine content typically ranges from 0.0 to 5.0 wt.%, preferably from 0.5 to 2.0 wt.%.

The experiments to determine the local electronic environment of tin, performed by conventional mössbauer spectroscopy using a source of γ-radiation Ba119mSnO3with a nominal activity of 10 MCI. The spectrometer operates in the transmission mode with the oscillator motion with constant acceleration, operating in triangular mode, 512-channel analyzer, reg is controlled by the microcomputer. The detector is a crystal of NaI (T1) of the thickness of 0.1 mm Scale calibrated using a standard spectrum of iron α with 6 lines obtained from source57Co(Rh). All chemical shifts are given relative to CaSnO3. For the decomposition of the experimental spectra to Lorentzian shape and to determine various parameters used software ISO (W. Künding, Nucl. Instrum. Method., 75, 336 (1969)).

According to the invention the catalyst in the reduced form usually has, according to mössbauer spectroscopy119Sn, the signal having the quadrupole splitting value from 0 to 0.45 mm/s and the chemical shift IS from 1.5 to 2.4 mm/s relative to CaSnO3the area of the specified signal is from 1 to 30% of the total area of the signals, preferably from 4 to 20%.

According to the allocations published by J. Olivier Fourcade, etc. in Chem. Phys. Chem. 2004, 5, 1734, the method of obtaining leads to the formation on the recovered catalyst centres tin Sn0connected with a part of the atoms of the platinum group metal. Thus, the observed alloy MxSnyis an indicator of a very strong interaction between the metal atoms of the platinum group and tin.

The substrate typically contains at least one oxide selected from the group consisting of oxides of magnesium, titanium, zirconium, aluminum, silicon. Prepact the sory is silicon oxide, the aluminum oxide or aluminum silicate, and more preferably alumina. According to the invention specified porous substrate is preferably in the form of beads, extrudates, tablets or powder. More preferably, the substrate is in the form of balls or extrudates. The pore volume of the substrate is preferably from 0.1 to 1.5 cm3/g, more preferably from 0.4 to 0.8 cm3/, in Addition, this porous substrate preferably has a specific surface area of from 50 to 600 m2/g, preferably from 100 to 400 m2/g, even from 150 to 300 m2/year

The method of preparation of the catalyst according to the invention usually contains the following steps:

a) the introduction of a promoter or promoters X1 and phosphorus on podate or sub-steps a1) or a2), and the specified step a1) corresponds to the synthesis of a precursor of a basic oxide, and the specified step a2) corresponds to the formation of the substrate,

b) introduction of tin on at least one of the sub-steps a1) and a2), and the stages a) and b) can be sequential or simultaneous,

c) drying the product obtained at the output of stage b),

d) calcination of the product obtained in stage c)at a temperature of from 350 to 650°C,

e) deposition of at least one metal M of the platinum group,

f) drying in a stream of inert gas or in a gas stream containing oxygen, at a reasonable price the first temperature, not exceeding 150°C,

(g) calcining the product obtained in stage f), at a temperature of from 350 to 650°C.

During molding of the substrate may be only part of the tin, and in this case, the method comprises an additional step of deposition of the rest of the tin on a substrate, or between steps d) and e)what can go (optional) drying and firing, or between steps e) and f), or after step g), followed by drying and firing.

The firing step (g) is usually conducted in the presence of air, possibly enriched with oxygen or nitrogen.

Promoters X1, P and Sn may be introduced by any method known to the expert. When injected into the substrate promoters X1, P and Sn may be added by mixing, co-precipitation, dissolution, and this list is not restrictive.

Thus, the introduction of tin can be performed simultaneously or separately, before or after introduction introduction predecessors X1 and P.

If the introduction of a promoter or promoters X1 and phosphorus were carried out during the synthesis of the precursor of the oxide, in accordance with one preferred method of receiving according to the invention, tin, phosphorus and predecessor or predecessors X1 injected during the synthesis of the precursor of the primary oxide method type Sol-gel.

According to another preferred method, the precursor is added in the ol pre-formed predecessor basic oxide.

The molded substrate is corresponding to the prior art methods of forming substrates, such as molding, extrusion or coagulation of droplets (Oil-Drop, according to English terminology).

There are several types predecessors X1, depending on the nature of the X1, which can be used alone or in a mixture. In the case of India suitable halides, nitrate, sulfate, perchlorate, cyanide, hydroxide India. Can be used predecessors types of halides, nitrate, sulfate, cyanide, hydroxide and oxyhalogenation gallium. Thallium may be in the form of nitrates, sulfates and thallium hydroxide. In the case of suitable antimony nitrate, sulphate and hydroxide antimony. Can be used precursor halides and oxanaloginova arsenic. Bismuth may be in the form of halides, nitrate, hydroxide, oxyhalogenation, carbonate of bismuth and bismuth acid.

Predecessors tin can be inorganic or ORGANOMETALLIC possibly ORGANOMETALLIC compounds water-soluble type. Can be used various predecessors, individually or in the form of a mixture. In particular, the tin can be selected without limitation from the group comprising halogenated compounds, hydroxides, carbonates, carboxylates, sulfates, tartratami and nitrates. These forms of tin may be utilized is directly introduced into the reaction mixture during preparation of the catalyst or can be prepared in situ(for example, through the introduction of tin and carboxylic acids). The ORGANOMETALLIC precursor type on the basis of tin can be, for example, SnR4where R means alkyl group, for example boutelou group, Me3SnCl, Me2SnCl2Et3SnCl, Et2SnCl2, EtSnCl3, iPrSnCl2and hydroxides Me3SnOH, Me2Sn(OH)2Et3SnOH, Et2Sn(OH)2oxides (Bu3Sn)2O, acetate Bu3SnOC(O)Me. Preferably will be used halogenated tin compounds, in particular chlorinated. In particular, it is advantageous to use SnCl2or SnCl4.

If the promoters Sn, X1 and P were introduced in a pre-molded substrate or on a substrate in the case of tin, the Protocol of preparation of the catalysts according to the invention requires firing before deposition of the metal M of the platinum group (step d). This firing is preferably carried out at a temperature of from 350 to 650°C, preferably from 400 to 600°C and even more preferably from 400 to 550°C. higher temperatures can be regular or include intermediate sections of constant temperature, and these areas can be achieved with fixed or variable rates of temperature increase. Thus, these cycles of temperature increase may be identical or different speed (in degrees per minute or per hour). Gas atmosphere, and is used when firing, includes oxygen, preferably from 2 to 50% by volume, more preferably from 5 to 25%. Thus, at this stage, firing can also use the air.

After receiving substrate is the deposition of at least one platinum group metal M (step e). At this point, the metal M can be entered by way of the dry impregnation or in excess mortar using a precursor or mixture of precursors containing metal M from the platinum group. Impregnation may be carried out in the presence of compounds that affect the interaction between the precursor of the metal M and the substrate. These compounds can be, without limitation, inorganic (HCl, HNO3) or organic (such carboxylic or polycarboxylic acids) acids and organic compounds of the type of complexing agents. Preferably the impregnation is carried out by any method known to the specialist, which allows to obtain a homogeneous distribution of the metal M within the catalyst.

The precursors of the metal M are members of the following group, and this list is not restrictive: hexachloroplatinic acid, bromopentanoate acid, chloroplatinic ammonium chlorides of platinum, dichlorocarbene dichloride, platinum chloride tetraamine platinum.

At this stage, the catalyst containing X1, Sn, P and platinum, dried (step f) in a neutral atmosphere or at the osphere, containing oxygen (which may be air), at a moderate temperature, preferably not exceeding 250°C. Preferably, drying is carried out at a temperature of less than or equal to 200°C and in continuation from several minutes to several hours.

Then at this stage it is fired product obtained in step f. This firing is preferably conducted in the presence of air. This air can also be enriched with oxygen or nitrogen. Preferably, the oxygen content in the gas is from 0.5 to 30.0%vol., even more preferably from 2 to 25%.

This firing is carried out at a temperature in the range from 350 to 650°C, preferably from 400 to 650°C and even more preferably from 450 to 550°C. the temperature Increase may (optionally) contain plots of constant temperature.

When the various precursors used in the preparation of the catalyst according to the invention, halogen-free or contain halogen insufficient, you may need to add a halogenated compound during retrieval. Can be used any compounds known to the expert that are introduced at any stage of the preparation of the catalyst according to the invention. In particular, you can use the connection type Friedel-such as the chloride or bromide of aluminum. You can also use the organizer is practical connection such as methyl - or arilgalogenide, for example dichloromethane, chloroform, dichloroethane, chloroform or carbon tetrachloride.

In the catalyst according to the invention can also add chlorine through oxychloride processing. Such processing may be performed, for example, at 500°C for 4 hours in a stream of air containing the number of chlorine gas are required for deposition of the desired amount of chlorine, and some water, when the molar ratio of H2O/Cl about, for example, 20.

Chlorine can also be added by impregnation with an aqueous solution of hydrochloric acid. A typical Protocol consists in the impregnation of the solid phase to enter the desired amount of chlorine. The catalyst is maintained in contact with the aqueous solution for a sufficiently long period of time to precipitate this amount of chlorine, then the catalyst was squeezed and dried at a temperature of from 80 to 150°C, and then finally calcined in air at a temperature of from 450°C to 650°C.

Typically, the catalyst is subjected to recovery processing. This recovery phase is usually carried out in the atmosphere diluted or pure hydrogen at a temperature, a positive component from 400°C to 600°C, preferably from 450°C to 550°C.

Examples

The following examples illustrate the invention.

Example 1 (comparative)

<> Preparation of A catalyst: Pt/(Al2O3-Sn)-Cl

The substrate in the form of beads of alumina containing 0.3 wt.% tin, with a mean diameter of 1.2 mm is produced by the interaction of tin dichloride with a Hydrosol of alumina obtained by the hydrolysis of aluminium chloride. Then the resulting Hydrosol of alumina is carried out through the vertical column filled with oil containing additives. Thus obtained spheres is subjected to heat treatment to a temperature of 600°C to obtain beads with good mechanical strength. Thus obtained substrate has a surface on BET 205 m2/year

Catalyst A is obtained on the basis of the substrate, depositing a 0.3 wt.% platinum and 1 wt.% chlorine in the calculation of the final catalyst. To 100 g oxytelinae substrate containing tin, add 400 cm3aqueous solution hexachloroplatinic acid and hydrochloric acid. Leave for 4 hours, then wring out. Dried at 120°C, then calcined for 2 hours at 500°C under air flow of 100 liters per hour, with the rate of temperature rise of 7°C per minute. The catalyst A obtained after firing contains 0.29 wt.% platinum, 0.30 wt.% tin and 1,02% wt. of chlorine.

Example 2 (comparative)

Preparation of catalyst B: Pt/(Al2O3-Sn-In-Cl

The substrate in the form of beads oxide and uminia, containing 0.3 wt.% tin and 0.3 wt.% India, with a mean diameter of 1.2 mm is produced by the interaction of tin dichloride and nitrate India with a Hydrosol of alumina obtained by the hydrolysis of aluminium chloride. Then the resulting Hydrosol of alumina is carried out through the vertical column filled with oil containing additives. Thus obtained spheres is subjected to heat treatment up to 600°C, to obtain beads with good mechanical strength. Thus obtained substrate has a surface on BET 201 m2/year

Catalyst B is obtained on the basis of this substrate in order to obtain the same amount of platinum and chlorine, as in example 1. Catalyst B obtained after firing contains 0.29 wt.% platinum, 0.29 wt.% tin, 0.30 wt.% India and 1.05 wt.% of chlorine.

Example 3 (comparative)

Preparation of catalyst C: Pt/(Al2O3-Sn-P)-Cl

The substrate in the form of beads of alumina containing 0.3 wt.% tin and 0.4 wt.% phosphorus, with a mean diameter of 1.2 mm, was obtained analogously to example 1, by reacting tin dichloride and phosphoric acid with a Hydrosol of alumina. Thus obtained substrate has a surface on BET 198 m2/year

Catalyst C is obtained on the basis of this substrate in order to obtain the same amount of platinum and chlorine, as in example 1. Cat is the lyst C, obtained after firing contains 0.30 wt.% platinum, 0.31 wt.% tin, to 0.39 wt.% phosphorus and 1.00 wt.% of chlorine.

Example 4 (according to the invention)

Preparation of catalyst D: Pt/(Al2O3-Sn-In-P)-Cl

The substrate in the form of beads of alumina containing 0.3 wt.% tin, 0.3 wt.% India and 0.4 wt.% phosphorus, with a mean diameter of 1.2 mm, was obtained analogously to example 1, by reacting tin dichloride, nitrate India and phosphoric acid with a Hydrosol of alumina. Thus obtained substrate has a surface on BET 196 m2/year

Catalyst D is obtained on the basis of this substrate in order to obtain the same amount of platinum and chlorine, as in example 1. Catalyst D obtained after firing contains 0.30 wt.% platinum, 0.31 wt.% tin, 0.32 wt.% India, 0.38 wt.% phosphorus and 1.00 wt.% of chlorine.

Example 5 (according to the invention)

Preparation of catalyst E: Pt/(Al2O3-Sn-In-P)-Cl

The substrate in the form of balls of aluminum oxide receive is identical to example 4, with the same amount of tin and phosphorus, but enter only 0.2 wt.% India. Thus obtained substrate has a surface according to BET of 210 m2/year

Catalyst E is obtained on the basis of this substrate in order to obtain the same amount of platinum and chlorine, as in example 1. Catalyst E obtained after firing, contains 0.31 wt.% p is tiny, 0.31 wt.% tin, 0.22 wt.% India, 0.40 wt.% phosphorus and 1,02% wt. of chlorine.

Example 6 (comparative)

Preparation of catalyst F: Pt-In/(Al2O3-Sn-P)-Cl

The substrate receiving, in an effort to get the same amount of tin and phosphorus, as in example 3. Thus obtained substrate has a surface according to BET of 180 m2/year

Catalyst F is obtained on the basis of this substrate in order to obtain the amount of 0.3 wt.% platinum, 0.3 wt.% India and 1 wt.% chlorine in the final catalyst.

To 100 g oxytelinae substrate containing tin and phosphorus, add 400 cm3aqueous solution hexachloroplatinic acid and hydrochloric acid. Leave for 4 hours, then wring out. Dried at 90°C, then enter into interaction with 200 cm3an aqueous solution of nitrate of India in the presence of hydrochloric acid. Leave for 4 hours, drained, dried at 120°C, then calcined for 2 hours at 500°C under air flow of 100 liters per hour, with the rate of temperature rise of 7°C per minute. Catalyst F obtained after firing contains 0.30 wt.% platinum, 0.32 wt.% tin, 0.29 wt.% India, 0.41 wt.% phosphorus and 1.04 wt.% of chlorine.

Example 7 (comparative)

Preparation of catalyst G: Pt-In-P/(Al2O3-Sn)-Cl

The substrate is prepared in order to obtain the same amount of tin, as in example 1.

Catalyst G get on osnovets substrate, in order to obtain the amount of 0.3 wt.% platinum, 0.3 wt.% India, 0.4 wt.% phosphorus and 1 wt.% chlorine in the final catalyst. Thus obtained substrate has a surface on BET 209 m2/year

To 100 g oxytelinae substrate containing tin and phosphorus, add 400 cm3aqueous solution hexachloroplatinic acid and hydrochloric acid. Leave for 4 hours, then wring out. Dried at 90°C, then enter into interaction with 200 cm3an aqueous solution of nitrate India and phosphoric acid in the presence of hydrochloric acid. Leave for 4 hours, wring out moisture, dried at 120°C, then calcined for 2 hours at 500°C under air flow of 100 liters per hour, with the rate of temperature rise of 7°C per minute. Catalyst G obtained after firing contains 0.30 wt.% platinum, 0.31 wt.% tin, 0.33 wt.% India, 0.38 wt.% phosphorus and 1.05 wt.% of chlorine.

Example 8 (according to the invention):

Preparation of catalyst H: Pt-Sn/Al2O3-Sn-In-P)-Cl

The substrate is prepared in order to obtain the same amount of indium and phosphorus, as in example 4, but with 0.2 wt.% the tin. Thus obtained substrate has a surface on BET 182 m2/year

Catalyst H is obtained on the basis of this substrate, precipitating 0.35 wt.% platinum, 0.2 wt.% additional tin to get 0.4 wt.% tin and 1 wt.% chlorine in the final catalyst.

To 100 g of the oxide is lumineau substrate, tin and indium, add 400 cm3aqueous solution hexachloroplatinic acid and hydrochloric acid. Leave for 4 hours, then wring out. Dried at 90°C, then enter into interaction with 200 cm3an aqueous solution of tin tetrachloride in the presence of hydrochloric acid. Leave for 4 hours, drained, dried at 120°C, then calcined for 2 hours at 500°C under air flow of 100 liters per hour, with the rate of temperature rise of 7°C per minute. Catalyst H, obtained after firing, contains 0.36 wt.% platinum, 0.41 wt.% tin, 0.29 wt.% India, 0.41 wt.% phosphorus and 0.99 wt.% of chlorine.

Example 9 (according to the invention)

Preparation of catalyst I: Pt-Sn/Al2O3-Sn-Sb-P)-Cl

The substrate in the form of beads of alumina containing 0.1 wt.% tin, 0.4 wt.% antimony and 0.4 wt.% phosphorus, with a mean diameter of 1.2 mm, get analogously to example 4, using dichloride, tin, gallium nitrate and phosphoric acid. Thus obtained substrate is characterized by a specific surface according to BET 191 m2/year

Catalyst I is obtained on the basis of this substrate in order to obtain the same amount of platinum, tin and chlorine, as in example 7. Catalyst G obtained after firing contains 0.29 wt.% platinum, 0.30 wt.% tin, 0.32 wt.% India, 0.42 wt.% phosphorus and 1.10 wt.% of chlorine.

Example 10

Defining features is to catalysts A-I using Mossbauer spectroscopy

Catalysts A-I restore stream of hydrogen at 450°C for two hours and transferred without access of air into the sealed glass chamber, adapted to the mössbauer spectrometer. The values of chemical shifts and quadrupole splitting catalysts A-I of examples 1-9 were identified according to the methods presented in the description, and are shown in table 1.

Example 11

Evaluation of characteristics of the catalysts A-I in the catalytic reforming unit

Samples of catalysts, which are described in examples 1-9 was used in the reaction layer, which is suitable for the conversion of hydrocarbons, naphtha, obtained from the distillation of crude oil. This nafta allows the following composition (by weight):

- 52,6% paraffin compounds

of 31.6% naphthenes,

with 15.8% of aromatic molecules

when full density 0,759 g/cm3.

The desired octane number of the raw materials close to 55.

After loading into the reactor, the catalyst is activated by heat treatment in an atmosphere of pure hydrogen for 2 hours at 490°C.

Evaluation of catalytic performances is carried out in conditions of reforming reactions, in risotti hydrogen and naphtha, previously described. In particular, conditions of use and comparison of catalysts the following:

is the gauge pressure of the reactor is maintained at 8 bar (0.8 MPa),

the feed rate of 2.0 kg/h per kg of catalyst

- the molar ratio hydrogen/hydrocarbons: 4.

The comparison is carried out with the same required octane number of the liquid product flows (called reformate), the resulting catalytic conversion of raw materials. The comparison is carried out for the desired octane rating of 104.

8,39
Table 2
Characteristics of catalysts
CatalystOutput C5+ through 148 h (wt.%)Output C4 - through 148 h (wt.%)Deactivation (°C/h)Coke (wt.%/h)
A88,38of 8.37+0,088+0,034
B88,798,05+0,140+0,038
C88,29+0,099+0,033
D89,367,34+0,084+0,026
E89,127,58+0,099+0,030
F88,648,11+is 0.102+0,034
G88,518,23+0,092+0,038
H89,227,45+0,085+0,029
I89,25of 7.48+0,089+0,029

The catalysts according to the invention (catalysts D, E, H and I) demonstrate improved selectivity (higher yield of C5+) and improved stability (low content of coke).

1. The catalyst for catalytic reforming of hydrocarbons, containing at least one metal M of group dps is Tina, tin, phosphorous promoter, a halogenated compound, a porous substrate and at least one promoter X1 is selected from the group consisting of gallium and indium, with the specified catalyst in the reduced form shows, according to mössbauer spectroscopy119Sn, the signal having the quadrupole splitting value from 0 to 0.45 mm/s and the chemical shift IS from 1.5 to 2.4 mm/s relative to CaSnO3the area of the specified signal is from 1 to 30% of the total area of the signals specified catalyst was prepared by the method comprising the introduction of this promoter X1 and phosphorus at the stage of preparation of the substrate.

2. The catalyst p. 1, in which the atomic ratio Sn/M is from 0.5 to 4.0.

3. The catalyst p. 1, in which the ratio of X1/M is from 0.1 to 5.0.

4. The catalyst p. 1, in which the ratio P/M is from 0.2 to 30.0.

5. The catalyst according to one of paragraphs.1-4, in which the content of metal M is from 0.01 to 5 wt.%.

6. The catalyst p. 5, in which the metal M is platinum or palladium.

7. The catalyst p. 1 in which the halogenated compound selected from the group consisting of fluorine, chlorine, bromine and iodine.

8. The catalyst according to p. 7, in which the content of the halogen-containing compound is from 0.1 to 15.0 wt.%.

9. The catalyst p. 8, in which the halogenated compound is chlorine is om, and the chlorine content is from 0.1 to 5.0 wt.%.

10. The catalyst p. 1, in which the substrate contains at least one oxide selected from the group consisting of oxides of magnesium, titanium, zirconium, aluminum, silicon.



 

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6 cl, 1 dwg, 2 tbl, 3 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting straight-run gasoline to a high-octane gasoline component with low benzene content. Described is a catalyst containing the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, and a heteropoly compound based on cobalt tungstobismuthate or cobalt tungstophosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst by mechanochemical treatment of the H form a H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3=30-50 in a vibrating mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and saturating with chloride solutions of corresponding heteropoly compounds of cobalt tungstobismuthate or cobalt tungstophosphate, followed by drying, and the catalyst is formed during heat treatment at 540-550°C for 0.1-12 hours. Described is a method of converting straight-run gasoline to a high-octane gasoline component in the presence of the described catalyst at 350-425°C, bulk speed of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: obtaining an active and selective catalyst for converting straight-run gasoline to a high-octane gasoline component with low benzene content of not more than 2,0 wt %.

3 cl, 1 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting a straight-run gasoline fraction into a high-octane gasoline component with low benzene content. Described is a catalyst which contains the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, cobalt molybdo-bismuthate or molybdo-phosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst, which involves hydrothermal crystallisation of a reaction mixture at 120-180°C, which contains sources of silicon, aluminium and alkali metal oxides, hexamethylenediamine and water, followed by drying and calcining, mechanochemical treatment in a vibration mill, moulding with further saturation of the H-form of the H-ZSM-5 type high-silica zeolite with silica modulus SiO2/AI2O3=30-50 with chloride solutions of corresponding heteropoly compounds: cobalt molybdo-bismuthate or cobalt molybdo-phosphate, as a modifying additive, followed by mechanochemical treatment in a vibration mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and calcining at 540-550°C for 0.1-12 hours. Described is a method of converting a straight-run gasoline fraction into high-octane gasoline component with low benzene content in the presence of the catalyst described above at 350-425°C, volume rate of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: high activity and selectivity of the catalyst.

3 cl, 1 tbl, 7 ex

FIELD: process engineering.

SUBSTANCE: invention relates to petrochemical and oil processing industries. Zeolite-bearing catalyst comprises zeolite ZSM-5 with silicate module SiO2/Al2O3=30-80 mol/mol, and zeolite structure elements, e.g. niobium oxide and/or molybdenum oxide and/or cobalt oxide, or mixes thereof, and zirconium oxide, at the following ratio of components, wt %: zeolite - 70.00-90.0; ZrO2 - 0-3.00; Nb2O3 - 0-3.00; MoO3 - 0-3.00; CoO - 0-2.00; Na2O - 0.03-0.10, and binder making the rest. Proposed method of producing said catalyst comprises mixing reagents, hydrothermal synthesis, washing, drying and calcination of precipitate. Note here that reaction mix produced by mixing water solutions of aluminium nitrate, sodium hydroxide, silicic acid or KCKG silica gel, niobium pentachloride, zirconium sulphate, molybdenum trioxide, zeolite seed crystals with ZSM-5/MF1 structure in amendment Na- or H-form, for example, butanol-1, monoethanolamine, dibutylamine, diethylentriamine, is loaded into reactor for hydrothermal synthesis at 175-185°C for 8-24 h. Thereafter, pulp of Na-form zeolite is filtered. Obtained precipitate is repulped in water solution of sodium oxide hydrate. Zeolite precipitate is filtered and repulped in water solution of ammonia bicarbonate. Zeolite precipitate is filtered and directed for acid or salt ion exchange by treatment with nitric acid water solution or water solutions of ammonia salts at pulp heating and mixing. Ammonia bicarbonate is added to pulp obtained after said acid or salt ion exchange and filtered out. Washed H- or NH4-zeolite is dried and subjected to preparation of catalyst mass by mixing zeolite powder with active aluminium hydroxide and concentrated nitric acid. Produced catalyst mass is extruded and pelletised. Produced pellets are dried at 150°C and calcined at 550-600°C. Proposed method of converting virgin gasoline fractions into high-octane gasoline with the help of zeolite-bearing catalyst comprises forcing vapors of virgin gasoline fractions through stationary bed of above described catalyst with additional feed of hydrogen into reaction zone.

EFFECT: higher quality and increased yield.

4 cl, 9 tbl, 21 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil-refining and petrochemical industry and production of catalysts used in conversion of C2-C12 aliphatic hydrocarbons and methanol to high-octane gasoline and aromatic hydrocarbons. Described is a zeolite-containing catalyst for converting C2-C12 aliphatic hydrocarbons and methanol to high-octane gasoline and aromatic hydrocarbons, which contains zeolite ZSM-5 with silica modulus SiO2/Al2O3=40-100 mol/mol and residual content of sodium oxide of 0.02-0.04 wt %, zeolite structural units and a binding component, wherein the zeolite structural units of the catalyst are niobium oxide and iron oxide or a mixture of oxides of said metals and zirconium oxide, and chromium oxide, with the following content of components (wt %): zeolite 65.00-85.00; ZrO2 0-3,00; Nb2O5 0-0.50; Fe2O3 0-1.00; Cr2O3 0-3.00; Na2O 0.02-0.04; binding component - the balance. Described is a method for obtaining a zeolite-containing catalyst, which involves mixing reactants, hydrothermal synthesis, washing, drying and calcining the residue. The reaction mixture obtained by mixing aqueous salt solutions of aluminium, zirconium, niobium, iron, chromium and sodium hydroxide, silica gel, zirconium sulphate, niobium pentachloride, inoculating zeolite crystals with a ZSM-5 structure in Na- or H-form, a structure-forming agent, for example diethylene triamine (bis-(2aminoethyl)amine) is fed into an autoclave, where hydrothermal synthesis is carried out at 160-190°C for 20-80 hours with constant stirring; at the end of hydrothermal synthesis, Na-form pulp of the zeolite is filtered; the obtained residue is washed with tap water and taken for salt ion exchange by treatment with aqueous ammonium chloride solution while heating and stirring the pulp; the pulp obtained from salt ion exchange is filtered, washed with tap water and then washed with dimineralised water to residual sodium oxide content of 0.02-0.04 wt % with respect to the dried and calcined product; the washed residue of the ammonium zeolite form is taken for preparation of the catalyst mass by mixing the ammonium zeolite form with active aluminium hydroxide; the obtained catalyst mass is extruded and granulated; the granules are dried at 100-110°C and calcined at 550-650°C; the calcined granules of the zeolite-containing catalyst are sorted; the fraction of the finished zeolite-containing catalyst is separated, and the fraction of granules smaller than 2.5 mm is ground into homogenous powder and returned to the step of preparing the catalyst mass. Described also is a method of converting C2-C12 aliphatic hydrocarbons and methanol to high-octane gasoline and aromatic hydrocarbons, which involves heating and passing material - vapour of straight-run gasoline fraction of oil or methanol through a fixed bed of the catalyst described above.

EFFECT: achieving high phase purity of the zeolite catalyst and wide distribution of acid sites thereof according to strength, introduction of more than one modifying element into the zeolite structure, high quality and output of end products on the disclosed catalyst.

4 cl, 9 tbl, 15 ex

FIELD: chemistry.

SUBSTANCE: invention relates to heterogeneous catalysts for producing benzene aromatic hydrocarbons. Described is a catalyst for converting methanol for producing benzene aromatic hydrocarbons, which contains decationated pentasil-type zeolite which is modified by mixture of zirconium pyrophosphate, zinc oxide and zirconium dioxide, has molar ratio SiO2/Al2O3 of 120-200 and contains sodium cations in an amount which is equivalent to 0.059-0.010 wt % sodium oxide, formed with binder from a gamma-modification of aluminium oxide and zirconium dioxide, with the following content of components, wt %: 65 (zeolite - 96.5-97.8 with content of modifier of (59 wt % ZrP2O7; 31 wt % ZnO and 10 wt % ZrO2), of 3.5-2.2) and 35 binder, from the sum of anhydrous oxides (γ-aluminium oxide - 80 and zirconium dioxide - 20). Described is a catalyst for producing benzene aromatic hydrocarbons, which contains decationated pentasil-type zeolite which is modified by mixture of copper oxide, zinc oxide and gallium oxide, has molar ratio SiO2/Al2O3 of 120-200 and contains sodium sodium cations in an amount which is equivalent to 0.24-0.11 wt % sodium oxide, formed by binder, with the following content of components, wt %: 65 (zeolite - 93.0-95.0, with content of zeolite modifier of (80 wt % CuO; 13 wt % ZnO and 7 wt % Ga2O3), of 7.0-5.0) and 35 binder, from the sum of anhydrous oxides (γ-aluminium oxide - 80 and zirconium dioxide - 20). Described is a method of producing benzene aromatic hydrocarbons from methanol which involves catalytic conversion of methanol in at least two reactors with different catalysts into a mixture of olefins and water vapour in a first reactor and subsequent conversion of said mixture in a second reactor, cooling the obtained gaseous products, condensation, separation with extraction of light paraffins, water, a mixture of aromatic hydrocarbons and recycling the cooled paraffins through both catalysts while feeding methanol into the first reactor, wherein said methanol conversion catalyst is used in the first reactor when converting methanol to olefins and formation of aromatic hydrocarbons from olefins in the second reactor takes place using said catalyst for producing benzene aromatic hydrocarbons, wherein conversion of methanol to olefins is carried out at temperature of 300-360°C, pressure of not more than 0.5 MPa and methanol mass feed rate of 2-3 h-1, and conversion of olefins in the reactor for formation of aromatic hydrocarbons is carried out at temperature of 450-530°C, pressure of 1.0-2.0 MPa and mass feed rate of methanol conversion products of 1.7-3.0 h-1, and recycling is carried out at a rate of 7 moles paraffins per mole methanol.

EFFECT: reduced amount of light hydrocarbon gases and high content of alkylarenes produced onshore.

9 cl, 9 ex

FIELD: chemistry.

SUBSTANCE: invention relates to versions of method of hydrocarbon aromatisation. One of method versions includes introduction of nitrogenate, oxygenate or both into hydrocarbon flow with obtaining improved hydrocarbon flow, containing from approximately 2 ppm to 10 ppm of nitrogenate, oxygenate or both, interaction of improved hydrocarbon flow with catalyst of aromatisation in reaction zone, where catalyst contains non-acidic zeolite carrier, group VIII metal and one or more halogenides; removal of output flow, which contains aromatic hydrocarbons, where nitrogenate refers to ammonia or any chemical compound, which forms ammonia in conditions of catalytic reaction, and where oxygenate refers to water or any chemical compound which forms water in conditions of catalytic reaction.

EFFECT: application of claimed invention makes it possible to preserve and increase aromatisation catalyst productivity.

19 cl, 8 ex, 1 tbl, 13 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention refers to catalytic reforming method of gasoline fractions at increased temperature and pressure in presence of platinum erionite containing catalysts, which is implemented in block consisting of five in-series located reactors, in the first one of which (forcontactor) there performed is preliminary dehydration of cyclohexane hydrocarbons contained in raw material, in presence of halogen-containing platinum catalyst, and in the next reactors (from the second one to the fifth one) there performed is reforming process with subsequent increase in erionite content in modifications of catalysts in the direction of the supplied raw material. Reforming process is performed in presence of catalysts with the following content of erionite in them as to reactors: to the second (in the direction of raw material) and the third reactors there loaded are catalysts with erionite content in each of them, which is equal to 0.5-3.0 wt %, and the fourth and the fifth reactors - with erionite content of 2.5-3.7 wt %; at that, to forcontactor there loaded is platinum catalyst containing mixture of fluorine and chlorine as haloid.

EFFECT: improvement of reforming process properties - activity, selectivity and stability.

1 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: catalyst for reforming of gasoline factions is described; it contains platinum (possibly rhenium), chlorine, zeolite and gamma aluminium oxide, amorphous aluminium silicate at the following ratio of the above components, wt %: platinum - 0.1-1.0; (possibly) rhenium - 0.1-0.5; chlorine - 0.1-1.0; zeolite - 0.5-3.9; amorphous aluminium silicate - 1-2; gamma aluminium oxide - the rest. Reparation method of the above catalyst is implemented by mixing of powders of aluminium hydroxide with zeolite, peptisation of mixture with water solution of acid, granulation, heat treatment of obtained granules of carrier with further application to surface of active components - platinum in the form of water solution of platinum-chlorohydric acid and chlorine in the form of hydrochloric acid, drying and annealing of catalyst; at that, peptisation of mixture of powders of aluminium hydroxide with zeolite is performed with 0.5-20% water solution of organic acid, for example lemon, acetic and oxalic acids, and heat treatment of carrier is performed at temperature of 630-700°C.

EFFECT: increasing activity, stability and selectivity of catalyst.

3 cl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting straight-run gasoline to a high-octane gasoline component with low benzene content. Described is a catalyst containing the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, and a heteropoly compound based on cobalt tungstobismuthate or cobalt tungstophosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst by mechanochemical treatment of the H form a H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3=30-50 in a vibrating mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and saturating with chloride solutions of corresponding heteropoly compounds of cobalt tungstobismuthate or cobalt tungstophosphate, followed by drying, and the catalyst is formed during heat treatment at 540-550°C for 0.1-12 hours. Described is a method of converting straight-run gasoline to a high-octane gasoline component in the presence of the described catalyst at 350-425°C, bulk speed of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: obtaining an active and selective catalyst for converting straight-run gasoline to a high-octane gasoline component with low benzene content of not more than 2,0 wt %.

3 cl, 1 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting a straight-run gasoline fraction into a high-octane gasoline component with low benzene content. Described is a catalyst which contains the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, cobalt molybdo-bismuthate or molybdo-phosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst, which involves hydrothermal crystallisation of a reaction mixture at 120-180°C, which contains sources of silicon, aluminium and alkali metal oxides, hexamethylenediamine and water, followed by drying and calcining, mechanochemical treatment in a vibration mill, moulding with further saturation of the H-form of the H-ZSM-5 type high-silica zeolite with silica modulus SiO2/AI2O3=30-50 with chloride solutions of corresponding heteropoly compounds: cobalt molybdo-bismuthate or cobalt molybdo-phosphate, as a modifying additive, followed by mechanochemical treatment in a vibration mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and calcining at 540-550°C for 0.1-12 hours. Described is a method of converting a straight-run gasoline fraction into high-octane gasoline component with low benzene content in the presence of the catalyst described above at 350-425°C, volume rate of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: high activity and selectivity of the catalyst.

3 cl, 1 tbl, 7 ex

FIELD: oil and gas industry.

SUBSTANCE: invention refers to application of a honeycomb catalyst, i.e. a catalyst with three or more beds for making phthalic anhydride by vapour-phase oxidation of orthoxylene and/or naphthalene. There is described application of the catalyst for making phthalic anhydride by vapour-phase oxidation of orthoxylene and/or naphthalene containing at least one bed from gas intake, the second bed closer to a gas output, and the third bed even closer to the gas output or at the gas output; and the catalyst beds, preferentially all of them, include an active material with TiO2, and activity of the first catalyst bed is higher than that of the second bed. There is also described method for making phthalic anhydride, according to which gaseous flow containing orthoxylene and/or naphthalene, and also molecular oxygen, at higher temperature are passed through the three-bed or honeycomb catalyst described above.

EFFECT: maintained high activity combined with very high selectivity.

27 cl, 4 ex, 6 tbl

FIELD: petroleum chemistry, organic chemistry, chemical technology.

SUBSTANCE: method involves contacting a mixture of carbon monoxide and hydrogen at increased temperature and pressure with a catalyst comprising manganese and cobalt on a carrier wherein cobalt, at least partially, presents as metal and catalyst comprises also inorganic phosphate in the amount at least 0.05 wt.-% as measure for elementary phosphorus relatively to the catalyst weight. Also, catalyst can comprise vanadium, zirconium, rhenium or ruthenium additionally. Method provides selectivity in formation (C5+)-hydrocarbons and decrease in formation of CO2.

EFFECT: improved preparing method.

7 cl, 1 tbl, 2 ex

The invention relates to the field of organic chemistry and petrochemicals, and in particular to catalysts for production of methyl tert-butyl ether

The invention relates to the field of organic chemistry and petrochemicals, and in particular to catalysts for the production of phenol and acetone

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting straight-run gasoline to a high-octane gasoline component with low benzene content. Described is a catalyst containing the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, and a heteropoly compound based on cobalt tungstobismuthate or cobalt tungstophosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst by mechanochemical treatment of the H form a H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3=30-50 in a vibrating mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and saturating with chloride solutions of corresponding heteropoly compounds of cobalt tungstobismuthate or cobalt tungstophosphate, followed by drying, and the catalyst is formed during heat treatment at 540-550°C for 0.1-12 hours. Described is a method of converting straight-run gasoline to a high-octane gasoline component in the presence of the described catalyst at 350-425°C, bulk speed of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: obtaining an active and selective catalyst for converting straight-run gasoline to a high-octane gasoline component with low benzene content of not more than 2,0 wt %.

3 cl, 1 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining and petrochemical industry, particularly to methods of producing catalysts for converting a straight-run gasoline fraction into a high-octane gasoline component with low benzene content. Described is a catalyst which contains the following, wt %: H-ZSM-5 type high-silica zeolite with silica modulus SiO2/Al2O3 = 30-50 - 94.0-99.0, cobalt molybdo-bismuthate or molybdo-phosphate 1.0-6.0, formed during heat treatment. Described is a method of producing a catalyst, which involves hydrothermal crystallisation of a reaction mixture at 120-180°C, which contains sources of silicon, aluminium and alkali metal oxides, hexamethylenediamine and water, followed by drying and calcining, mechanochemical treatment in a vibration mill, moulding with further saturation of the H-form of the H-ZSM-5 type high-silica zeolite with silica modulus SiO2/AI2O3=30-50 with chloride solutions of corresponding heteropoly compounds: cobalt molybdo-bismuthate or cobalt molybdo-phosphate, as a modifying additive, followed by mechanochemical treatment in a vibration mill for 0.1-24 hours, moulding the catalyst mass into granules, drying and calcining at 540-550°C for 0.1-12 hours. Described is a method of converting a straight-run gasoline fraction into high-octane gasoline component with low benzene content in the presence of the catalyst described above at 350-425°C, volume rate of 1.0-2.0 h-1 and pressure of 0.1-1.0 MPa.

EFFECT: high activity and selectivity of the catalyst.

3 cl, 1 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of decontaminating nitrous oxide, including low-concentration emissions of nitrous oxide, for example in exhaust gases from production of nitric acid, using a catalyst based on an iron-containing zeolite. Described is a method of preparing a catalyst for decomposing nitrous oxide by mixing a zeolite having a structure selected from the following: MFI, MEL, BEA, FER, MOR and having the composition: y·El2On·SiO2, where y = 10-5-5·10-2 , El is at least aluminium and one element from periods 2, 3, 4 and 5 of the periodic table of elements, n is valence of the element, with iron-modified binder, the binder being aluminium oxide with additives selected from the following oxides: silicon oxide, titanium oxide, zirconium oxide, iron oxide, cobalt oxide, copper oxide, lanthanum oxide, phosphorus oxide, with weight ratio of aluminium oxide to any of the listed oxides ranging from 0.01:100 to 10:100, with weight ratio of the zeolite to binder ranging from 1:9 to 9:1, where the modifying iron in the catalyst is x·Fe2O3, where x=10-5-5·10-2; modification is carried out by adding to the binder a dry or hydrated salt and/or solution of an iron salt with subsequent formation and activation of the catalyst to obtain a catalyst, wherein at least 0.5-50% of the contained iron and not less than 5·1017 iron atoms per gram catalyst are in reduced form in the form of special complexes of α-centres which are detectable and measurable using a special technique, involving determination of the amount of surface oxygen deposited from nitrous oxide at temperature of 100-300°C on the surface of the catalyst. A method of decontaminating gaseous emissions is also described.

EFFECT: simple method of producing a highly efficient catalyst for decomposing nitrous oxide.

6 cl, 1 tbl, 19 ex

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