Catalyst for methylmercaptane preparation from methanol and hydrogen sulfide

FIELD: chemistry.

SUBSTANCE: invention refers to methylmercaptane synthesis prepared from aluminium oxide, alkali metal wolframate and at least one of ammonium salt containing sulphur or nitrogen with catalyst pH in water suspension 10% being 5.0 - 9.7. The method of methylmercaptanes preparation from methanol and hydrogen sulfide using said catalyst is described also.

EFFECT: enhancing of catalyst activity and selectivity particularly at low hydrogen sulfide/methanol ratios.

6 cl, 2 tbl, 4 ex

 

The present invention concerns a catalyst to obtain mercaptan from methanol and hydrogen sulfide.

The mercaptan is an important intermediate product for the synthesis of methionine, to obtain dimethyl sulfoxide and dimethyl sulfone or for the synthesis of alkanesulphonic acids. Today mercaptan receive preferably by interaction of hydrogen sulfide and methanol on the catalyst is aluminum oxide in the gas phase. Synthesis of methylmercaptan carried out usually at a temperature of from 300 to 500°C. and at a pressure of from 1 to 25 bar.

To improve the activity and selectivity of the catalyst is aluminum oxide it is usually alloyed with tungstate of an alkali metal (for example, EP-A-832878). In the publication edited by Mashkina and others described that the catalysts, which on the surface contain acidic centers are very active, but give respectively the same amount of mercaptan and dimethyl sulfide in the output. Catalysts that contain a strong main centres are less active, but show a higher selectivity with respect to the mercaptan (Mashkina et al., React. Kinet. Catal. Lett. 1987, 407-412). Thus, increased activity and selectivity is explained by the presence of both basic and acidic reaction center.

Aluminum oxide is also alloyed with other substances, in the example a carbonate of an alkali metal (US 5847223).

The activity and selectivity increase by increasing the molar ratio of hydrogen sulfide to alcohol. Typically, the molar ratio is between 1 and 10. A higher molar ratio from 10 to 13 indicates the presence of a high excess of hydrogen sulfide in the reaction mixture, and, thus, arises the need to supply large quantities of gas in the loop.

US 2685605 relates to a method of obtaining mercaptan by reacting the hydrogen sulfide and methanol on the catalyst, preferably thorium/pumice catalyst, and together with hydrogen sulfide and methanol in a reactor are introduced minor amount of water.

US 2647151 describes obtaining allylmercaptan by the interaction of hydrogen sulfide and alcohol on thorium/pumice catalyst, in which the education necessary allylmercaptan should be increased by suppressing the formation of such by-products as organic sulfides. This increase selectivity reached by feeding into the reactor a small amount of hydrogen.

DE-A-37773 recommends together with alcohol and hydrogen sulfide in the implementation of cooperation in the reactor be submitted with oxygen in the presence of a catalyst of aluminum oxide and potassium tungstate. Oxygen reduces the number of unwanted deposits on the catalyst during the method is its regenera the Oia.

US 3935376 describes the method, the improvement which consists in the optimization of the temperature regime, and loss of quality of the catalyst and the formation of by-products is reduced to a minimum. The catalyst consists of aluminum oxide and a promoter. It was found that when creating the at least three zones of the catalyst can be observed optimum temperature for the entire system. The total number of the hydrogen sulfide fed to the first zone of the catalyst, and the flow of methanol can be distributed to all areas of the catalyst. The ratio of hydrogen sulfide to methanol is from 1.1 to 2.5.

In EP-A-832878 described improved catalysts which are obtained by deposition of the promoter (potassium tungstate) in a special way the two portions on the active alumina. Then the catalysts sulfiderich under identical reaction conditions.

According to the publication Mashkina et al. (React. Kinet. Catal. Lett. 1988, 159-164) the form of the promoter modify using hepta-, dodeca - and meta-tungstate. In addition, use doped with potassium carbonate, the ammonium tungstate, potassium tungstate with a small addition of acid and/or with the addition of silicon oxide. As a result of this extensive experiment found that the net doping of potassium tungstate without additional submission of the promoter or process is the best to stand the deprivation of selectivity with respect to the mercaptan, and speed of reaction.

According to SU 1316127, SU 1608923, EN 2056940 and WO 99/14172 it was found that increasing the selectivity reaches through the use of media on aluminum borate, or by the addition of oxides of boron to the promoter on the basis of tungstate or using the mixture of promoters containing potassium aluminate, amorphous tungsten oxide and sodium oxide and/or boron oxide.

Known from the prior art catalysts and methods for producing mercaptan with regard to their selectivity and activity or cost-effective way to use require improvements.

Therefore, the present invention is the development of the most active and selective catalyst for getting methylmercaptan without the need for multistage methods of preparation of the catalyst, the supply of expensive or toxic active mass or the use of special modes of operation of the reactor. In addition, to reduce the energy consumption ratio of hydrogen sulfide to alcohol should be slightly different from 1.

This problem is solved by using a catalyst, which is obtained by applying the active aluminum oxide of the alkali metal tungstate as a promoter and at least one ammonium salt and/or at least one protonic acid selected from the group that includes the policy acid, phosphoric acid, sulfurous acid, tungstic acid, phosphorous acid, posterolateral acid, hydrogen fluoride, bromovalerate and iodovidonum. In addition, it was found that the mercaptan can preferably be obtained when using the catalyst according to the invention. As the alkali metal tungstate, preferably using potassium tungstate. The tungstate is applied in an amount of from 1 to 20 wt.% (depending on the total mass of the catalyst), preferably from 10 to 16 wt.%.

It is preferable to use ammonium salt. As ammonium salts, particular preference is given to the sulfates, phosphates, sulphides, wolframates, molybdates, sulfites, peroxodisulfate, phosphites, hypophosphites, halides and carbonates. Preferably use sulfates, phosphates, sulfides, wolframate, molybdates, sulfites, peroxodisulfate, phosphites and hypophosphites. Particular preference is given to salts containing sulfur or phosphorus, and tungstate salts. In addition, use of a mixture of ammonium salts. It is preferable to use from 0.01 to 15 wt.% ammonium salts (calculated on the total weight of the catalyst, in particular from 0.01 to 10 wt.%.

Instead of ammonium salts or a mixture of these salts can be used proton acid selected from the group comprising sulfuric acid, phosphoric acid, cernis the second acid, tungsten acid, phosphorous acid and posterolateral acid. Particular preference is given to proton acids containing sulfur or phosphorus.

This catalyst according to the invention is obtained by impregnation of activated alumina mixture promoter containing the alkali metal tungstate and ammonium salt or by nabryzgivaniya this mixture of promoter to catalyst is aluminum oxide. The impregnation is carried out by hydrating, i.e. the amount of solution corresponds to the pore volume of the carrier, or by excessive impregnation, i.e. the volume of the solution is greater than the pore volume. The alkali metal tungstate before the application can also be obtained by reacting tungstate salts, such as, for example, the tungstate ammonium meta-tungstate ammonium or para-ammonium tungstate, respectively, in the form of hydrates or tungsten acid, for example, with a solution of caustic potash or caustic soda solution. After that, the catalyst calicivirus on the air or in the presence of oxygen, for example at a temperature of from 400 to 500°C.

Thus, the method of obtaining is a simple one-step method. If necessary, the aluminum oxide before applying the promoter may be calcined within 1-10 hours, preferably 1-5 hours at a temperature of from 300 to 600°C, before occhialino from 400 to 500°C.

The catalyst preferably has a pH value of less 9,8, especially the pH value of the catalyst is from 5 to 9.7. Measurement of pH is carried out by receiving a 10%aqueous suspension of the investigated catalyst. This sample within a minute shake, leave for 5 minutes to stand and then using electrodes to measure the pH value of the suspension.

The use of this catalyst compared to the one described in the prior art catalysts helps increase the activity and selectivity of the finished catalyst, in particular at low molar ratio of 3 to 1 of hydrogen sulfide to methanol.

As aluminum oxide for such catalysts preferably used so-called active alumina. This substance has a large specific surface area of from 10 to 400 m2/g and mainly consists of the oxide of the transition series of crystallographic phases of aluminum oxide (see, for example, Ullmann's Enzyclopedia of Industrial Chemistry von 1985, Vol.A1, str-562). Such transitional oxides belong to χ-, κ-, γ-, δ-, η-, θ-aluminum oxide. Active aluminum oxide for catalytic use commercially different qualities and in different forms. Particularly suitable is γ-alumina, for example, in granulated or molded form. It is preferable to use aluminum oxide molded in f is RME with diameter from 1 to 5 mm Specific surface area is preferably from 150 to 400 m2/g, total pore volume from 0.3 to 1.0 ml/g, a bulk weight of from 300 to 1000 g/l

If necessary, before using for the synthesis of methylmercaptan catalyst pre sulfiderich in conditions close to the reaction. For this purpose through the catalyst particles for 0.5-100 hours, pass a stream of hydrogen sulfide at a temperature of from 200 to 450°C and a pressure of from 1 to 25 bar.

The molar ratio of hydrogen sulfide and methanol in the synthesis of methylmercaptan is generally from 1:1 to 10:1, preferably from 1:1 to 2:1. In such molar ratios of substances contain as part of the newly added hydrogen sulfide and methanol, and part of the recycled hydrogen sulfide and methanol.

The catalyst was fed into the reactor preferably in the form of solid particles with a diameter from 1 to 5 mm, for example 4 mm

In addition to hydrogen sulfide and alcohol in the reactor may also be lodged with oxygen, water and hydrogen, and inert gas or mixture of inert gases. Mostly fed to the reactor stream contains from 0 to 30 mol, preferably from 5 to 30 moles of inert gas per mole of alcohol. Suitable inert gases are, for example, nitrogen, methane, ethane, propane, butane and/or carbon dioxide. By supplying oxygen can avoid unwanted deposits on the catalyst. Thus it is possible the OS is to conduct the regeneration of the catalyst during the way. The concentration of oxygen in the implementation of the method is mainly <2.5 wt.%, depending on the amount fed into the reactor flow, and, thus, is significantly below the explosive concentration limits. Preferably the oxygen concentration is from 10 ppm to 0.5 wt.%, particularly preferably from 10 ppm to 500 h/million Oxygen can be fed into the reactor in any form. You can also apply pure oxygen, if necessary, in a mixture with inert gas. Typically, oxygen is supplied as air.

Fed to the reactor stream may also contain components containing sulfur separated from the resulting mercaptan (as, for example, described in DE-A-1768826).

According to the invention is a method of obtaining mercaptan by reacting the hydrogen sulfide and methanol on the catalyst, as a rule, is carried out in the form of gas-phase reactions in a tubular reactor. In addition, can be used several serially connected reactors. Typically, methanol and hydrogen sulfide are heated to a temperature which is high enough so as methanol and methyl mercaptan were in the gas phase, but below the temperature of decomposition of methylmercaptan. Generally, the method according to the invention is carried out at a temperature of from 250 to 500°C, predpochtitel is but from 300 to 450°C. The exact temperature of the reaction depends, among other things, on the reaction pressure and the used catalyst.

The method according to the invention is generally carried out at a pressure of from 1 to 25 bar. Needless to say the pressure is chosen not so high that fed to the reactor, the stream or mercaptan condensed. Preferably in the process according to the invention the pressure is from 1 to 10 bar. In order to reduce the risk of emission of harmful substances into the environment, the pressure can be from 1 to 3 bar, preferably closer to 0.

The method according to the invention is generally carried out continuously. Processing the received mercaptan that you are carrying out well-known specialist methods.

The volumetric rate (the ratio of the weight of the original substance to the weight of catalyst per hour) is generally from 0.1 to 10 h-1preferably from 0.1 to 5 h-1, particularly preferably from 0.5 to 2 h-1.

Conversion during the implementation of the method according to the invention is generally from 80 to 100%, preferably from 95 to 100%, in terms of the number used in a molar deficiency of components (i.e. in terms of the amount of methanol in the synthesis of methylmercaptan). In the process according to the invention are able to achieve selectivity of metalmark is prana from 80 to 100%.

Examples:

Example 1: Obtain comparative catalyst

(14 wt.% K2WO4on γ-Al2O3)

203 g of the hydrate meta-tungstate ammonium dissolved in 0,385 l of water, after that add 182 g of 48%aqueous solution of caustic potassium and fill to volume corresponding to the water absorption of the carrier. 1,048 l such impregnating solution evenly nabryzgivajut to 1,588 kg pressed γ-Al2About3. Then the catalyst for 2 hours calicivirus in a drying oven with air circulation at 450°C.

Obtaining a catalyst according to the invention aluminum oxide, potassium tungstate and ammonium salts

Example 2: ammonium phosphate

of 72.3 g of the hydrate meta-tungstate ammonium dissolved in 0,150 l of water, then add to 29.7 g of potassium hydroxide and 88.3 g of three-hydrate of ammonium phosphate. This solution is filled up to a volume corresponding to the water absorption of the carrier. Impregnating solution evenly nabryzgivajut on 500 g of pressed γ-Al2About3and the catalyst for 2 hours calicivirus in a drying oven with air circulation at 450°C.

Example 3: ammonium sulfate

Analogously to example 2 to obtain an aqueous solution of hydrate meta-tungstate ammonium, potassium hydroxide and 30.9 g of ammonium sulfate, dispersed in 500 g of pressed γ-Al2About3after this the catalyst for 2 hours calicivirus in the schiehlen oven with circulating air at 450°C.

Example 4: ammonium sulfide

Analogously to example 2 to obtain an aqueous solution of hydrate meta-tungstate ammonium, potassium hydroxide and the 36.1 g of ammonium sulfide, nabryzgivajut on 500 g of pressed γ-Al2About3after this the catalyst for 2 hours calicivirus in a drying oven with air circulation at 450°C.

Table 1.
Characterization of catalysts
CatalystPromotersSBET[m2/g]PHChemical analysis [weight. %]
Number [weight. %]
Comparative example 1--2219,8-
Example 2The ammonium phosphate5% P2O51627,9R: 2,2
The use of the 3 Ammonium sulfate5% (NH4)2SO41906,0S: 1,1
Example 4Ammonium sulfide3% (NH4)2S1898,2S: 0.4

Measurement of pH: the investigated catalyst receive a 10%aqueous suspension. The sample within a minute shake, leave for 5 minutes to stand, and then using electrodes to measure the pH value of the suspension.

Measurement of surface area by BET method (SBET): DIN 66131.

Operational test:

MeSH reactor (600 mm length, 25 mm in diameter) filled 280g extruded catalyst. At a temperature of 390°C (middle of the reactor) and a pressure of 1.1 bar in the tubular reactor serves 48 g/h (1.5 mol) of gaseous methanol and 64 g/h (1.9 mol) of hydrogen sulfide. The gas composition determined by gas chromatography (GC - area %).

Table 2
ExampleThe maximum temperature [°C]The decay products [GC-p. %]With lectively [%] Conversion Meon [%]Wind MeSH [%]
Comparative example 14321,10is 83.897,781,9
Example 24401,78899989
Example 3440the 1.44899787
Example 44431,38889786

1. Catalyst for the synthesis of methylmercaptan, derived from aluminum oxide, alkali metal tungstate and at least one sulfur-containing or phosphorus ammonium salt, and its pH value, measured in 10%aqueous slurry is from 0.5 to 9.7.

2. The catalyst according to claim 1, characterized in that the alkali metal tungstate is used, the potassium tungstate.

3. The catalyst according to claim 1 or 2, characterized in that wolframate of Molochny the metals applied in an amount of from 10 to 16 wt.% in terms of the total weight of the catalyst.

4. The catalyst according to claim 1 or 2, characterized in that the ammonium salt is applied in an amount of from 0.01 to 15 wt.% in terms of the total weight of the catalyst.

5. The method of producing mercaptans by reacting methanol and hydrogen sulfide, wherein the used catalyst according to any one of claims 1 to 5.

6. The method according to claim 5, characterized in that upon receipt of mercaptans, hydrogen and methanol are used in a molar ratio of from 1:1 to 2:1.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to caesium and tungsten-containing oxide catalyst of alkylmercaptane synthesis, method of its production and method of obtaining alkylmercaptanes with its application. Described is catalyst including oxide composition, which corresponds to general formula CsxWOy, in which x represents number from 0.8 to less than 2, and y represents number from 3.4 to less than 4. Described is method of production of catalyst which contains oxide compounds of caesium and tungsten, which lies in the following: a) carriers or substance-carrier, consisting of aluminium oxide is impregnated with water solution containing soluble caesium and tungsten compound with required molar ratio of caesium and tungsten given above, b) obtained impregnated formed carriers or obtained impregnated highly-dispersive aluminium oxide (preliminary prepared catalyst) are subjected to preliminary drying at room temperature, c) if necessary they are subjected to drying at temperature within the range from 100 to 200°C in order to remove residual moisture, d) are subjected to final burning during 2-10 hours at temperature within the range from 300 to 600°C and e) applied catalyst or impregnated highly-dispersive aluminium oxide is obtained, with content of promoter of general composition CsxWOy, where x and y have given above values, in amount from 15 to 45 wt %, preferably from 20 to 36 wt %, after which f) impregnated highly-dispersive aluminium oxide is suspended with addition of known auxiliary substances and applied on core-carrier from inert material or is extruded and pressed. Also described is method of obtaining alkylmercaptane by interaction of alkanols with hydrogen sulphide in presence of catalyst described above.

EFFECT: increase of catalyst activity and selectivity.

14 cl, 2 tbl, 10 ex

The invention relates to a catalyst used for the synthesis of mercaptan from methanol and hydrogen sulfide, as well as to a method for producing this catalyst

The invention relates to a catalyst for the synthesis of methylmercaptan and method thereof

The invention relates to a method of continuous receipt of methylmercaptan through catalytic interaction of methanol with hydrogen sulfide in the vapor phase at a temperature of 300-500°C.

The invention relates to the production of odorants for natural gas, in particular waste-free way to obtain mercaptan, as well as to a method for producing a catalyst, providing a higher degree of interaction between methyl alcohol and hydrogen sulfide and the use of such a method of producing hydrogen sulfide, which provides waste reduction production in General

The invention relates to catalysts for the synthesis of methylmercaptan used in the production of methionine, agricultural chemicals and other chemical compounds

FIELD: chemistry.

SUBSTANCE: catalyst is processed with sulphiding agent, which includes sulphur-organic compound and oil fraction, in particular 1.0-2.0%-solution of dimethyldisulphide in Diesel fuel, dimethyldisulphide being introduced into Diesel fuel step-by-step; thermoprocessing of catalyst being carried out as step-by-step increase of temperature within the interval 160-340°C, after which temperature is reduced to 28-290°C, with general activation duration 20-30 hours.

EFFECT: reduction of equipment corrosion with sulphur oxides, obtaining ecologically pure, low-sulphureous Diesel fuel, polycyclic aromatic hydrocarbons in small amount, increasing degree of unlimited hydrocarbons and reduction of gumming-up of main hydropurification catalyst.

3 cl, 6 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: description is given of a catalytic composition with general formula, in consideration of oxides: (X)b(M)c(Z)d(O)e (I), in which X represents at least one group VIII base metal, M represents at least one group VIB metal, Z represents one or more elements, chosen from aluminium, silicon, magnesium, titanium, zirconium, boron and zinc, O represents oxygen, one of b and c represents an integer 1, and d, e and one of b and c represents each a number bigger than 0, such that the molar ratio b:c ranges from 0.5:1 to 5:1, molar ratio d:c ranges from 0.1:1 to 50:1, and molar ratio e:c ranges from 3.6:1 to 108:1. The method of obtaining the composition involves heating a composition with general formula (NH4)a(X)b(M)c(Z)d(O)e (II), in which a represents a number bigger than 0, and X, M, Z, O, b, c, d and e are such that, they are bigger, at temperature ranging from 100 to 600°C, where the composition with formula II is in suspension form or is extracted from a suspension, optionally after maturing at temperature ranging from 20 to 95°C for a period of not less than 10 min. The above mentioned suspension is obtained by precipitation at temperature and within a period of time, sufficient for obtaining formula II composition, of at least one compound of a group VIII base metal at least one compound of a group VIB metal at least one refractory oxide material and alkaline compound in protonic liquid. At least one of the metal compounds is partially in solid state and partially in dissolved state. Description is given of volumetric metal oxide catalytic composition, obtained using the method given above, and a composition with general formula I, which can be obtained using a precipitation method, in which a refractory oxide material in quantity ranging from 15 to 40 wt % is precipitated at least with one compound of a group VIII base metal, and at least with one compound of a group VIB metal, as well as the method of obtaining it. Description is also given of the use of compositions, moulded or sulphided when necessary, in hydro-processing.

EFFECT: increased activity of catalytic compositions.

14 cl, 10 tbl, 24 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to catalyst for aromatization of alkanes, to a method of preparation thereof, and to aromatization of alkanes having from two to six carbon atoms in the molecule. Hydrocarbon aromatization method consists in that (a) C2-C6-alkane is brought into contact with at least one catalyst containing platinum supported by aluminum/silicon/germanium zeolite; and (b) aromatization product is isolated. Synthesis of above catalyst comprises following steps: (a) providing aluminum/silicon/germanium zeolite; (b) depositing platinum onto zeolite; (c) calcining zeolite. Hydrocarbon aromatization catalyst contains microporous aluminum/silicon/germanium zeolite and platinum deposited thereon. Invention further describes a method for preliminary treatment of hydrocarbon aromatization catalyst comprising following steps: (a) providing aluminum/silicon/germanium zeolite whereon platinum is deposited; (b) treating zeolite with hydrogen; (c) treating zeolite with sulfur compound; and (d) retreating zeolite with hydrogen.

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26 cl, 1 dwg, 5 tbl, 4 cl

FIELD: petroleum processing.

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EFFECT: simplified process.

2 cl, 1 tbl, 3 ex

FIELD: petroleum processing.

SUBSTANCE: invention concerns development of catalysts for use in petroleum fraction hydrofining processes. Presulfidized catalyst including alumina-supported cobalt, molybdenum, phosphorus, and boron, active components of which are converted into operational sulfide form using sulfidizing agent, in particular hydrogen sulfide, at sulfidizing temperature 80 to 500°C and hydrogen sulfide volume flow rate 0.02 to 6.00 h-1, catalyst further contains lanthanum oxide. Composition of catalyst is the following, wt %: MoS2 8.0-17.0, Co3S2 1.5-4.0, P2O5 2.5-5.0, B2O3 0.3-1.0, La2O3 1.0-5.0, and alumina - the balance.

EFFECT: simplified catalyst preparation technology without losses in catalytic and mechanical properties.

1 tbl, 3 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalytic system of hydrocarbon feedstock hydrofining is activated by circulating hydrogen-containing gas or mixture thereof with starting feedstock through layer-by-layer loaded catalysts in presulfided or in presulfided and oxide form at elevated temperature and pressure. Hydrogen is injected into circulating hydrogen-containing gas or mixture thereof with starting feedstock portionwise, starting concentration of hydrogen in circulating hydrogen-containing gas not exceeding 50 vol %. Starting feedstock consumption is effected stepwise: from no more than 40% of the working temperature to completely moistening catalytic system and then gradually raising feedstock consumption to working value at a hourly rate of 15-20% of the working value. Simultaneously, process temperature is raised gradually from ambient value to 300-340°C. Circulating factor of hydrogen-containing gas achieves 200-600 nm3/m3. Addition of each portion of hydrogen is performed after concentration of hydrogen in circulating hydrogen-containing gas drops to level of 2-10 vol % and circulation of hydrogen-containing gas through catalysts loaded into reactor begins at ambient temperature and further temperature is stepwise raised. Starting feedstock, which is straight-run gasoline or middle distillate fractions, begins being fed onto catalytic system at 80-120°C.

EFFECT: enabled prevention and/or suppression of overheating in catalyst bed.

5 cl, 6 tbl, 12 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalytic reforming carried out at temperature in the reforming zone entry not higher than 485°C is supplemented by sulfidizing accomplished by introducing sulfur-containing compounds by doses each constituting 0.001-0.02% sulfur of the weight of catalyst, intervals between doses being not less than 1/2 one dose introduction time and at summary amounts of added sulfur 0.02-0.2% sulfur of the weight of catalyst during additional sulfidizing period. Additional sulfidizing is performed one or several times over the service cycle lasting hundreds or thousands hours. One sulfur dose addition time ranges from 0.5 to 1.5 h.

EFFECT: increased yield of reforming catalysate.

3 cl, 1 tbl, 7 ex

FIELD: catalyst preparation methods.

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EFFECT: enhanced process efficiency.

14 cl, 2 dwg

FIELD: production of hydrorefining catalyst.

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EFFECT: the invention ensures production of a catalyst of excellent activity and stability at hydrorefining using lower temperatures, less number of stages and without calcination.

10 cl, 8 ex, 4 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to caesium and tungsten-containing oxide catalyst of alkylmercaptane synthesis, method of its production and method of obtaining alkylmercaptanes with its application. Described is catalyst including oxide composition, which corresponds to general formula CsxWOy, in which x represents number from 0.8 to less than 2, and y represents number from 3.4 to less than 4. Described is method of production of catalyst which contains oxide compounds of caesium and tungsten, which lies in the following: a) carriers or substance-carrier, consisting of aluminium oxide is impregnated with water solution containing soluble caesium and tungsten compound with required molar ratio of caesium and tungsten given above, b) obtained impregnated formed carriers or obtained impregnated highly-dispersive aluminium oxide (preliminary prepared catalyst) are subjected to preliminary drying at room temperature, c) if necessary they are subjected to drying at temperature within the range from 100 to 200°C in order to remove residual moisture, d) are subjected to final burning during 2-10 hours at temperature within the range from 300 to 600°C and e) applied catalyst or impregnated highly-dispersive aluminium oxide is obtained, with content of promoter of general composition CsxWOy, where x and y have given above values, in amount from 15 to 45 wt %, preferably from 20 to 36 wt %, after which f) impregnated highly-dispersive aluminium oxide is suspended with addition of known auxiliary substances and applied on core-carrier from inert material or is extruded and pressed. Also described is method of obtaining alkylmercaptane by interaction of alkanols with hydrogen sulphide in presence of catalyst described above.

EFFECT: increase of catalyst activity and selectivity.

14 cl, 2 tbl, 10 ex

FIELD: chemistry.

SUBSTANCE: catalyst includes carrier, which contains tungsten oxide or hydroxide of at least one element from grope IVB ("ИЮПАК 4"), first component from at least one element from lanthanide line, yttrium and their mixture, and second component, which contains at least one component of metal from platinum group or their mixture. Also described is method of hydrocarbons transformation by contacting of raw material with solid acid catalyst, described above, with transformed product formation. Described is method of paraffin raw material isomerisation by its contacting with said catalyst at temperature from 25 to 300°C, pressure from 100 kPa to 10 MPa and volumetrical speed of liquid feeding from 0.2 to 15 hour-1 , with further product release, enriched by isoparaffins.

EFFECT: stability in hydrocarbons transformation process, increase of isoparaffins content.

10 cl, 1 tbl, 2 ex, 8 dwg

FIELD: chemistry.

SUBSTANCE: description is given of a catalytic composition, containing: a) oxygen compound of an element, chosen from group IVB of the periodic table of elements; b) oxygen compound of an element, chosen from group VIB of the periodic table of elements; c) not less than approximately 1 wt % particles of colloidal silicon dioxide relative to the total mass of the catalyst; d) aluminium compound; and e) group VIII metal. Description is also given of the method of chemical conversion of a hydrocarbon, involving reaction of the hydrocarbon under conditions of the chemical conversion reaction with the given catalytic composition.

EFFECT: increased activity and selectivity of the catalytic composition.

16 cl, 3 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention can increase the efficiency of processes of nonoxidising conversion of methane due to increase in activity of W-containing zeolite catalysts. Described is the zeolite catalyst ZSM-5 for process of nonoxidising conversion of methane which has in its composition tungsten in the form of nano-sized powder, thus the content of tungsten in the catalyst is from 4.0 up to 10.0 mass %. Also the method of the preparation of zeolite catalyst for the process of nonoxidising conversion of methane is described, including modification of zeolite by tungsten as a solid, thus tungsten is introduced into zeolite in the form of nano-sized powder of the metal, obtained by the method of electrical explosion of the conductor in the environment of argon, thus the content of tungsten in the obtained catalyst is from 4.0 up to 10.0 mass %. The method of nonoxidising conversion of methane in the presence of zeolite catalyst is described.

EFFECT: obtaining of a catalyst with higher activity during conversion of methane in aromatic hydrocarbons.

3 cl, 1 tbl, 7 ex

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention relates to supported olefin metathesis catalyst and to a olefin metathesis process using the latter. Catalyst is essentially composed of transition metal or oxide thereof, or a mixture of such metals, or oxides thereof deposited on high-purity silicon dioxide containing less than: 150 ppm magnesium, 900 ppm calcium, 900 ppm sodium, 200 ppm aluminum, and 40 ppm iron. When pure 1-butene comes into interaction with this catalyst under metathesis reaction conditions, reaction proceeds with 2-hexene formation selectivity at least 55 wt %. Use of catalyst according to invention in olefin metathesis process minimizes double bond isomerization reactions.

EFFECT: increased olefin metathesis selectivity regarding specific products.

17 cl, 2 tbl, 2 ex

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