A method of obtaining a c2-hydrocarbons
(57) Abstract:The inventive original mixture of methane and oxygen in contact with the catalyst, the composition of which corresponds to the following empirical f - Le: where Me strontium or barium; Me - magnesium or calcium; a= 0,6 - 2,0; b= 0,5 - 2,5; c= 7,0 - 8,9; e= 10,6 - 16, and the introduction of the reaction mixture of water vapor in a quantity of 50 - 80 about. % . The process is carried out at 800 - 850C in flow mode at atmospheric pressure and contact time of 0.25 to 1.0. The content of methane and oxygen in the mixture is from 14 to about 40. % and 4 to about 20. % respectively. The yield of ethylene is 14 and 17.6 mol. % with hydrocarbons up to 20 - 24 mol. % (based on missed methane, after condensation of the water content of products in the mixture obtained after the reaction: ethylene 7,7 - 10,5 about. % , ethane 3 to about 5. % . The catalysts are characterized by high stability. 1 C. p. F. - ly, 1 table. The invention relates to a method for producing ethylene and ethane, predominantly ethylene. Ethylene is the most large the product of modern chemistry, which is based on a significant part of the production of organic chemistry. Currently, the industrial method for producing ethylene is the cracking of light fractions of petroleum refining. In Kant natural gas. Development of method of obtaining2hydrocarbon oxidative conversion of methane is a new direction of catalysis, which is rapidly developing in the last five years. Analysis of literature data on the search for efficient catalysts and process conditions shows that high output WITH2hydrocarbons (>18 mol. % ) are mainly using metacyclophane mixtures diluted with an inert gas, which leads to the production of gas mixtures after reaction with a low concentration of target products [1-5] .One of the main problems of the creation of this process is to develop a stable catalytic systems, therefore, proposed in many publications catalysts containing compounds of alkaline and legalistically metals, are of no interest from the point of view of practical implementation of the process [1-3,6] . Is not promising and use as additives in the catalyst halide compounds, although this allows to obtain ethylene with high yield (up to 16-30 mol. % ) [7-10] . This is due to the rapid loss of activity haloesters catalysts, corrosion problems in the equipment and contamination halide compounds.N the positive transformation of methane use as feedstock metacyclophane mixtures on the catalyst with a content of 0.8 to 10 wt. % La media MgO when 800-845aboutAnd the methane content in the initial mixture 64-78%  . The maximum yield of ethylene is to 6.8 mol. % catalyst containing 1.0 wt. % La. The disadvantage of this method is the relatively low yield of ethylene and ethane.The aim of the invention is to increase the yield of ethylene and ethane in the reaction of oxidative combination of methane without diluting the original reaction mixture with an inert gas in order to obtain, after the reaction gas mixture with a high concentration of target products on the catalysts are characterized by high stability.This goal is achieved by using a catalyst whose composition corresponds to the following empirical formula: LaaMeb'Mec"CdOeor LaaMeb'Mec"Oewhere Me', strontium or barium, MeI- magnesium or calcium; a = 0,6-2,0; b = 0,5-2,5; c = 7,0-8,9; d = 0.1 to 2.5; e = 10,6-16, and the introduction of the reaction mixture of water vapor in the amount of about 50-80. % . Use as diluent water vapor allows to increase the output WITH2hydrocarbons and after separation of the water of condensation to obtain a high concentration of them in the gas mixture after the reaction. The process osushestvlenie methane and oxygen in the mixture to be about 14-40. % and about 4-20. % respectively.The catalysts can be prepared by mixing or solutions of nitrate salts, or solutions of nitrates of La, and Me and carbonate Me', by steaming them in a boiling water bath and further annealing at 800about4 o'clockDistinctive features of the proposed method of carrying out the reaction of oxidative combination of methane in relation to the prototype are:
1) the use of the catalyst composition: LaaMeb'Mec"CdOeor LaaMeb'Mec"Oewhere Me', strontium or barium, Me" as magnesium or calcium; a = 0,6-2,0; b = 0,5-2,5; c = 7,0-8,9; d = 0.1 to 2.5; e = 10,6-16;
2) introduction in the original reaction mixture of water vapor in the amount of about 50-80. % ;
3) the methane and oxygen in the mixture to be about 14-40. per cent and 4.5-17,5 about. % respectively.Distinctive features of the proposed method of carrying out the reaction of oxidative dimerization of methane are new not only in relation to the prototype, but is unknown to the authors of all other sources related to a method for producing ethylene from methane. The invention has a new quality and can be classified as corresponding to the criterion of "significant differences".Conducting RL. % (based on missed methane and at the same time be obtained after condensation of the high water content of products in the mixture after the reaction: ethylene - 7,7-10,5 about. % , ethane - about 3-5. % . The proposed catalysts are characterized by high stability. Tests for 300 h show that this decrease in activity is observed. Analysis of the initial mixture and the reaction products spend chromatog - graficheskim method.P R I m e R 1. In the U-shaped quartz reactor with an inner diameter of 3.0 mm was placed 0.5 cm3catalyst composition La1,0Srthe 2.5Ca7,0Cthe 2.5O16with a grain size of 0.5-1 mm, the Reaction mixture was about. % : 25,5 CH4, 4,5 O2, 70 H2O, is passed through the catalyst at 850aboutWith and contact time = 0,5 sec.P R I m m e R 2. Similar to example 1, but the reaction mixture has a composition, on. % : 24 CH4, 6 O2, 70 H2O.P R I m e R 3. Similar to example 1, but the reaction mixture has a composition, on. % : 21 CH4, 9 O2, 70 H2O.P R I m e R 4. Similar to example 1, but the reaction mixture has a composition, on. % : 32,5 CH4, 17,5 O2, 50 H2O.P R I m e R 5. Similar to example 3, but the process is conducted on the catalyst composition La1,3Sr0,5Ca8,9C0,B>, 6 O2, 80 H2O, and the composition of the catalyst corresponds to the formula: La1,2Sr1,0Ca8,9C1,0O13,2.P R I m e R 7. Similar to example 1, but as the catalyst used, the sample composition of La1,3Sr0,5Ca8,9O11,3the reaction mixture has a composition: about. % : 40 CH4, 10 O2, 50 H2O, and the process is carried out at the time of contact = 0,2 sec.P R I m e R 8. Similar to example 3, but the reaction temperature is 800aboutWith, the process is carried out at contact time = = 1.0 in the presence of a catalyst composition: La1,1Sr2,0Cathe 7.5C2,0O15,1.P R I m e R 9. In the U-shaped quartz reactor with an inner diameter of 3.0 mm was placed 0.5 cm3catalyst composition La1,1Ba2,0Mgthe 7.5C2,0O15,1with a grain size of 1-2 mm, the Reaction mixture was about. % : 22,5 CH4, 7,5 O2, 70 H2O, is passed through the catalyst at 850aboutWith and contact time = 0.25 in C.P R I m e R 10. Similar to example 2, but the process is carried out in the presence of a catalyst composition La1,1Ba2,0Cathe 7.5C2,0O15,1and contact time = 0,4 sec.P R I m e R 11. Similar to example 3, but using the catalyst composition La1,0Sr2,52,0Srthe 2.5Ca6,5O12,0the reaction is carried out at a temperature of 800aboutWith and contact time = 1,0 C.P R I m e p 13. Similar to example 3, but using the catalyst composition Lafor 0.6Srthe 2.5Ca7,2O10,6.Outside of the intervals of the selected catalyst composition and the reaction mixture indicated in the claims, the purpose of the invention is not achieved. This is confirmed by the examples 14-19.P R I m e R 14. Similar to example 2, but the composition of the catalyst corresponds to the formula Lafor 0.4Srthe 2.5Ca7,3Cthe 2.5O15,4.P R I m e R 15. Similar to example 2, but the composition of the catalyst corresponds to the formula La1,3Sra 0.1Ca9,2Ca 0.1O12,4.P R I m e R 16. Similar to example 1, but the reaction mixture has a composition, on. % : 80 CH4, 20 O2.P R I m e R 17. Similar to example 1, but the reaction mixture has a composition, on. % : 64 CH4, 16 O2, 20 H2O.P R I m e R 18. Similar to example 2, but the reaction temperature is 700aboutC.P R I m e R 19. Similar to example 3, but the contact time is 0.05 with.The table presents the results of experiment the wordcourse, the concentration of ethylene and ethane in the dry gas mixture after the reaction.As can be seen from the data given in the table, the proposed method of carrying out the reaction for oxidizing a combination of methane can increase the yield of ethylene to 14-17,6 mol. % , C2hydrocarbons 20-25 mol. % , the ethylene concentration in the gas mixture after the reaction is 7.7 to 10.5. % . The proposed catalysts are characterized by high stability. (56) 1. Moriyama , T., Takasakii N. , Iwamatsu, E. , K. Aika Oxidative dimerization of methane over promoted magnesium oxide catalysts. Important factors // Chem. Lett. - 1986. - P. 1165-1168.2. Matsuura I. , Doi , T., Utsumi Y. Oxidative coupling of methane over a Li2O-BeO system catalyst // Chem. Lett. - 1987. - P. 1473-1476.3. Otsuka K. , Komatsu, T. Conversion of methane to aromatic hydrocarbons by combination of catalysts // Chem. Lett. - 1986. - P. 1955-1958.4. Machida K. , M. Enyo Oxidative dimerization of methane over cerium mixed oxides and its relation with their ionconducting characteristics // J. Chem. Soc. Chem. Commun. - 1987. - P. 1639-1640.01.5. Matsuura I. , Utsumi Y. , Nakai, M. , Doi, T. Oxidative coupling of methane over lithium-promoted zinc oxide catalyst // Chem. Lett. - 1986. - P. 1981-1984.6. Suleimanov, A. I. Oxidative dehydrodimerization methane. Thesis A. Suleymanova, I. Kida. chem. Sciences. - Novosibirsk, 1986. - 180 S.7. Otsuka K. , Liu Q. , Morikawa A. Selective synthesis of ethylene by partial oxidation of methane over LiCl-Sm2O3// J. Chem. Soc. Chem. Commun. - 1986. - P. 586-587.8. Wang F.-C , Xu, G. Y. Study of catalysts for the reaction of oxidative combination of methane: effect of lithium chloride on the activity of the oxides of transition metals // Cuihua xuebao, J. Catal. (whale. ). - 1988. - V. 9. - P. 214-217.10. Wang X.-P. , Lin, Q. , Chao Y. , Shen, U.-F. Oxidizing the combination of methane to put on BaCO3the oxides of metals // Cuihua xuebao, J. Catal. (whale. ). - 1988. - V. 9. - P. 423.11. USSR author's certificate N 1482905, class C 07 C 2/84, 1989. 1. A METHOD OF OBTAINING A C2-HYDROCARBONS by oxidative conversion of methane at elevated temperature in the presence of oxygen and a catalyst containing lanthanum, alkaline earth metal and oxygen, characterized in that the use of a catalyst containing as the alkaline earth metal is strontium or barium and magnesium or calcium and composition of which corresponds to the following empirical formula
LaaMe MeCdOe< / BR>where Me- strontium or barium;
Me- magnesium or calcium;
a = 0,6 - 2,0
b = 0,5 - 2,5
c = 7,0 - 8,9
e = 10,6 - 16,
and the process is carried out at 800 - 850oIn the presence of water vapor at the following content of components in the reaction mixture, about. % :
Methane 14 - 40
Oxygen 4,5 - 17,5
Water vapor od, the composition of which corresponds to the following empirical formula:
LaaMe MeCdOe< / BR>where MeMe, a, b, c, e have the indicated values,
d = 0.1 to 2.5.
FIELD: organic chemistry, petroleum chemistry, chemical technology.
SUBSTANCE: method involves preparing ethylene and hexane-1 from butene-1 by the exchange reaction of butene-1 and the isomerization reaction of synthesized hexane-3 to hexane-1. The parent material represents a mixed butene flow wherein butene-1 is isomerized to butene-2 after separation of isobutylene followed by the isomerization reaction of butene-2 to butene-1. Butene-1 is a raw for the exchange reaction.
EFFECT: improved preparing method, simplified technology process.
32 cl, 4 tbl, 4 ex
FIELD: petrochemical processes.
SUBSTANCE: invention relates to improved C2-C4-alkane oxidation process to produce corresponding alkene and carboxylic acid, which process comprises bringing indicated alkane in oxidation reaction zone into contact with molecular oxygen-containing gas and corresponding alkene and optionally with water in presence of at least one catalyst efficient for oxidation of alkane into corresponding alkene and carboxylic acid. Resulting product contains alkene, carboxylic acid, and water, wherein alkene-to-carboxylic acid molar ratio in oxidation reaction zone is controlled or maintained at desired level by way of controlling alkene and optional water concentrations in oxidation reaction zone and also, optionally, controlling one or several from following parameters: pressure, temperature, and residence time in oxidation reaction zone. Invention also relates to integrated process of producing alkyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone in contact with each other in presence of at least one catalyst effective in production of alkyl carboxylate to produce the same. Invention further relates to production of alkenyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone plus molecular oxygen-containing gas into contact with each other in presence of at least one catalyst effective in production of alkenyl carboxylate to produce the same.
EFFECT: enhanced process efficiency.
55 cl, 1 dwg, 7 tbl, 22 ex
FIELD: organic chemistry, chemical technology.
SUBSTANCE: invention relates to the improved method for oxidation of (C2-C4)-alkane and preparing the corresponding alkene and carboxylic acid. Method involves addition of this alkane to contact with molecular oxygen-containing gas in oxidative reaction zone and optionally at least one corresponding alkene and water in the presence of at least two catalysts with different selectivity. Each catalyst is effective in oxidation of alkane to corresponding alkene and carboxylic acid resulting to formation of product comprising alkene, carboxylic acid and water wherein the molar ratio between alkene and carboxylic acid synthesized in the reaction zone is regulated or maintained at the required level by regulation the relative amounts of at least two catalyst in the oxidative reaction zone. Also, invention relates to the combined method for preparing alkyl carboxylate comprising abovementioned stage in preparing alkene and carboxylic acid in the first reaction zone. Then method involves the stage for addition of at least part of each alkene and carboxylic acid prepared in the first reaction zone to the inter-contacting in the second reaction zone the presence of at least one catalyst that is effective in preparing alkyl carboxylate to yield this alkyl carboxylate. Also, invention relates to a method for preparing alkenyl carboxylate comprising the abovementioned stage for preparing alkene and carboxylic acid in the first reaction zone and stage for inter-contacting in the second reaction zone of at least part of each alkene and carboxylic acid synthesized in the first reaction zone and molecular oxygen-containing gas in the presence of at least one catalyst that is effective in preparing alkenyl carboxylate and resulting to preparing this alkenyl carboxylate.
EFFECT: improved method for oxidation.
30 cl, 1 dwg, 5 tbl, 14 ex
FIELD: petrochemical processes.
SUBSTANCE: process of producing benzene, ethylene, and synthesis gas from methane comprises following stages: (i) supplying into reactor initial gas containing methane and carbon dioxide; (ii) oxidation of methane in reactor under specific reaction conditions using first catalytic material and/or additional oxidant; and (iii) removal from reactor of gas stream formed containing benzene, ethylene, and synthesis gas, inside wall of reactor having been treated with first catalytic material.
EFFECT: increased conversion of methane and selectivity regarding benzene at reduced accumulation of coke fragments.
20 cl, 9 tbl, 9 ex
SUBSTANCE: invention relates to method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids. The method includes the following stages: (a) contact in the oxidation reaction zone of the alkane, which contains molecular oxygen gas, not necessarily corresponding to the alkene and not necessarily water in the presence of at least one catalyst, effective with the oxidation of the alkane to the corresponding alkene and carboxylic acid, alkane, oxygen and water; (b) separation in the first separating agent at least part of the first stream of products in a gaseous stream, which includes alkene, alkane and oxygen, and a liquid stream, which includes carboxylic acid; (c) contact of the mentioned gaseous stream with the solution of a salt of metal, capable of selectively chemically absorbing alkene, with the formation of a liquid stream rich in chemically absorbed alkene; (d) isolation from the flow of the solution of salt of the metal. The invention also relates to combined methods of obtaining alkyl-carboxylate or alkenyl-carboxylate (for example vinyl acetate), moreover these methods include oxidising of alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acid, isolation of alkene from the mixture of alkene, alkane and oxygen by absorption using the solution of the salt of metal and extraction of the stream rich in alkene from the solution of the salt from metal for using when obtaining alkyl-carboxylate and alkenyl-carboxylate.
EFFECT: improved method of oxidising alkane from C2 to C4 with the obtaining of corresponding alkene and carboxylic acids.
46 cl, 1 dwg
SUBSTANCE: invention concerns a method of obtaining low olefins from methylchloride involving passing of source gas reaction mix containing at least methylchloride over at least one catalyst layer with active centres characterised by the presence of absorption band with wave numbers within ν=1410-1440 cm-1 in the infrared spectres of adsorbed ammonium, the catalyst containing active component and high-silica carrier characterised by the presence of Si bands with chemical shifts of -100±3 ppm (band Q3) and -110±3 ppm (band Q4) in the NMR29 spectres with integrated intensity ratio of Q3/Q4 bands within 0.7 to 1.2, and by hydroxyl groups absorption bands with wave number ν=3620-3650 cm-1 and half-width 65-75 cm-1 in the infrared spectre, and specific surface area measured by BET method by argon heat desorption SAr=0.5-30 m2/g, surface area measured by alkali titration method SNa=10-250 m2/g at the SNa/SAr ratio of 5-30. The method also involves formation of active centres with higher acidity in the catalyst characterised by deuterium-hydrogen exchange depth of not less than 10% at 350-355°C in a deuterium and hydrogen mix containing 0.6% of hydrogen, 0.6% of deuterium, 0.05% of Ar and 98.75% of nitrogen, at volume feed rate of the said deuterium-hydrogen mix of 20000 h-1 in thermoprogrammed reaction mode at heating rate of 10 K/min and/or by additional introduction of either copper, or zinc, or silver to the active component content.
EFFECT: high selectivity of methylchloride transformation to light olefins together with high ethylene yield and improved deactivation resistance of catalyst.
3 cl, 8 ex
SUBSTANCE: active particles are synthesised on the first stage: in a plasmatron - atomic hydrogen, in a forreactor - methyl radicals, under the effect on natural gas, coming into a pyrolysis reactor, from which ethylene with acetylene impurities is produced, which, without separation from pyrolysis gas, is selectively hydrogenated into ethylene on the next stage in the presence of a catalyst in gaseous phase, with subsequent separation of concentrated ethylene from the hydrogenation products using low temperature rectification method, return of part of methane and hydrogen mixture from the hydrogenation stage to the pyrolysis stage in the forreactor and use of a balance quantity of methane and hydrogen mixture to produce electrical energy or as an end product. Content of methane in the methane and hydrogen mixture, fed into the forreactor, does not exceed 13 wt %.
EFFECT: increased output of ethylene with low energy consumption.
4 cl, 1 ex, 1 dwg
SUBSTANCE: invention relates to the method of producing low-molecular olefin hydrocarbons through pyrolysis of hydrocarbon material in the presence of an activating additive and water vapour. The method is characterised by that, the activating additive used are non-ionic surfactants.
EFFECT: increased output of low-molecular olefins during pyrolysis of vacuum gas oil.
3 cl, 6 ex
SUBSTANCE: invention relates to method of obtaining catalyst used for conversion of oxygen-containing compounds into light olefins. Described is method of obtaining silicoalumophosphate molecular sieves which includes: first, obtaining reaction mixture containing definite amount of primer which contains from 8 to 20% (weight) of silicon oxide calculated per amount of dry oxide, aluminium source, phosphorus source, at least one organic template and silicon source with further stimulation of formation of crystals of silicoalumophosphate molecular sieves and their separation. Also described is catalyst of conversion of oxygen-containing compounds into olefins, where oxygen-containing compounds are methanol and/or dimethyl alcohol, containing crystalline silicoalumophosphate molecular sieves, where first part of said crystalline silicoalumophosphate molecular sieves contains from 8 to 20% (weight) of silicon dioxide and where the second part of said crystalline silicoalumophosphate contains from 1 to 5% (weight) of silicon dioxide.
EFFECT: obtaining catalyst based on molecular sieves characterised by lower defect density and better selectivity with respect to light olefin obtaining.
9 cl, 1 ex
SUBSTANCE: invention relates to a method of producing aromatic hyhrocarbons and lower olefins, involving catalytic dehydrocyclisation of hydrocarbon material in the presence of a zinc-containing zeolite catalyst, at high temperature and pressure, separation of dehydrocyclisation products into product A - aromatic hydrocarbons C6+, and product B - mixture of non-aromatic hydrocarbons with hydrogen, subsequent hydrodealkylation of product A, obtaining commercial-grade benzol, and pyrolysis of product B, obtaining lower olefins, and characterised by that, the dehydrocyclisation material used is C2-C6 paraffins, the process is carried out at 0.9-1.3 MPa pressure, after separating the C10+ fraction, product A is subjected to hydrodealkylation, commercial-grade benzol, methane and ethane fractions, ethane fraction and product B are separated from hydrodealkylation products, or after separating over 50 vol % methane-hydrogen fraction from product B, product B is taken for pyrolysis, commercial-grade ethylene and propylene are separated from gaseous products of pyrolysis, liquid products of pyrolysis - pyrolysis condensate, containing aromatic hydrocarbons, is subjected to catalytic hydrogenation and hydrodesulphurisation, and subsequent hydrodealkylation, obtaining commercial-grade benzol, methane and ethane fractions, the latter is returned for pyrolysis.
EFFECT: increased output of lower olefins, significant improvement of economic parametres of the process due to increase of inter-regeneration period of dehydrocyclisation catalyst.
1 cl, 5 ex, 5 tbl
FIELD: chemical industry; other industries; methods and devices for conversion of the methane by the plasma-catalytic oxidation.
SUBSTANCE: the invention is pertaining to the method for conversion of the methane by the plasma-catalytic oxidation and to the and devices fro the method realization. The method of conversion of methane is conducted by the super high frequency (SHF)radiation plasma-catalytic oxidation with production of ethylene. The method includes activation of the catalyst by the SHF radiation and formation of the non-equilibrium "cold" SHF plasma. Simultaneously exercise activation of the catalyst by the super high frequency radiation and by the SHF plasma and create the non-equilibrium "cold" super high frequency plasma simultaneously in the Е010 type resonator or on Е01 with the symmetry of rotation from the SHF generator and on the total wave Н11° with rotation of the polarization plane of the continuous SHF generator. In the device realizing the indicated process the round waveguide is smoothly transforms into the waveguide with the partial dielectric filling-up and contains the aligner used for reduction of the reflections of the super high frequency energy, the encapsulant for provision of vacuum in the SHF plasma-catalytic reactor and the SHF plasma generation on the butt of the quartz rod, with the located on it quartz plates and the catalyst. The batchers of the uniform feeding of the reactants (СН4 + О2 + Аг) are installed with the capability of rotation and movement with respect to the SHF plasma. The system of the reaction products withdrawal is located in symmetry to the axis of the with respect to the plasmatron. The invention stimulates the increase of efficiency of the conversion process of methane into ethylene.
EFFECT: the invention ensures stimulation of the increased efficiency of the conversion process of methane into ethylene.
9 cl, 2 ex, 4 dwg, 1 tbl
SUBSTANCE: method involves partial burning of a mixture of methane, hydrogen, oxygen and optionally hydrocarbons, which are different from methane in contact with a catalyst, capable of maintaining burning beyond the normal upper flammable limit of fuel, where they react with formation of product, including one or more olefins. In the mixture coming into contact with the above mentioned catalyst, capable of maintaining burning beyond the normal flammable limit of fuel, can be less than 20 molar % (converted to the overall quantity of the hydrocarbons) of those hydrocarbons which are different from methane. In the mixture coming into contact with the catalyst, the volume ratio of hydrogen to oxygen ranges from 5:1 to 1:1 and methane and oxygen are put into the autothermal cracking device in a mixture at hourly average feed rate of more than 70000 h-1.
EFFECT: invention pertains to the method of obtaining olefins from methane.
12 cl, 2 tbl, 2 ex
SUBSTANCE: method of obtaining hydrocarbons C2-C3 by high-temperature catalytic oxidizing conversion of methane lies in supply to reactor, into which catalyst is placed, and whose free volume is filled with inert filling, of initial gas mixture, which contains mixture of methane and molecular oxygen, at rate 50000-70000 m/g/h, catalyst includes into its composition ions of alkali metal, manganese, tungsten and silicon oxide with molar ratio M:W:Mn:Si, where M-Na or K or Rb or Cs, equal 1.8-2.2:1:1.9-2.3:89-92, and is characterised by presence in it of tungsten in oxidation degree W6+, manganese oxidation degrees Mn7+, Mn6+, Mn3+, catalyst being obtained by thermal processing at 200°C and further incineration at temperature 795-799°C of initial solid powder-like mixture, consisting of salts and/or oxides of tungsten, manganese, alkali metal and SiO2, taken in said mole ratio in terms per mole of tungsten, manganese, alkali metal and silicon atoms.
EFFECT: increase of target product output, catalyst productivity, simplification of technology of obtaining target products and reduction of expenditures.
11 cl, 1 tbl, 30 ex
SUBSTANCE: aqueous suspension containing earth metal salt, powdered metal chloride and powdered transition metal oxide is made; aqueous suspension is made by dispersing in water the earth metal salt chosen from the group including barium and/or calcium and probably strontium or their combination. Water is added in powdered metal chloride, where powdered metal chloride is chosen from the group including Sn, Mg, Na, Li, Ba. Further powdered transition metal oxide is added being titanium oxide, to water; then plastic binder is added to until paste is formed; paste is dried up paste to powder; powder is heated up at raising temperature following preset temperature profile. Heated powder is baked to produce perovskite catalyst. Suspension contains mixed Ba and/or Ca and/or Sr (0.95mole) + TiO2 + metal chloride chosen from the group Sn, Mg, Na, Li, Ba in amount 0.05 mole.
EFFECT: simplified technology of catalyst producing.
19 cl, 14 ex, 2 tbl, 8 dwg
SUBSTANCE: invention relates to two versions of a method for synthesis of aromatic compounds, on of which involves: a methanation step involving contact between a hydrogen-containing gas and carbon monoxide and/or carbon dioxide in the presence of a catalyst which causes reaction of hydrogen contained in the gas with carbon monoxide and/or carbon dioxide and conversion of these components to methane and water; and a step for synthesis of an aromatic compound with reaction of lower hydrocarbon with methane obtained at the methanation step in the presence of a catalyst to obtain a gaseous reaction product containing aromatic compounds and hydrogen, where the aromatic compounds are separated from the gaseous reaction products obtained at the aromatic compound synthesis step, and the remaining hydrogen-containing gas is taken to the methanation step. The invention also relates to a method for synthesis of hydrogenated aromatic compounds obtained using methods described above.
EFFECT: possibility of obtaining aromatic compounds through catalytic reaction of lower hydrocarbons.
14 cl, 13 tbl, 3 ex, 2 dwg
SUBSTANCE: invention relates to a method of producing acetylene through oxidative pyrolysis of methane in the presence of oxygen and a catalyst, characterised by that the catalyst is heated to 700-1200°C by passing electrical current through it. The catalyst used is a fechral alloy which is thermally treated on air at temperature 900-1100°C. The ratio of methane to oxygen is varied in the range of 5:1-15:1.
EFFECT: high output and selectivity of the process.
2 cl, 17 ex, 1 tbl, 1 dwg
SUBSTANCE: invention relates to a method of converting methane to ethylene and ethane via oxidative conversion, characterised by that the catalyst used in this process is a mixture of quartz and phthalocyanine complexes of magnesium, aluminium or manganese, where the method is realised at temperature 700-800°C.
EFFECT: use of said catalysts increases output of the product.
2 cl, 7 tbl, 7 ex, 2 dwg
SUBSTANCE: invention relates to a method for chemical processing of mixtures of gaseous C1-C6 hydrocarbons (alkanes) into C2-C3 olefins (ethylene and propylene), involving oxidative condensation of methane and pyrolysis of C2-C6 alkanes, characterised by that oxidative pyrolysis of C2-C6 alkanes is carried out at temperature 450°C-850°C, pressure 1-40 atm and while feeding not more than 15 vol. % oxygen in the presence of oxide catalysts without preliminary splitting of the initial mixture of gaseous C1-C6 hydrocarbons (alkanes) into components and/or separation of methane; oxidative condensation of methane takes place in a stream of methane separated from products of oxidative pyrolysis of C2-C6 alkanes, in the presence of oxide catalysts at temperature 700°C-950°C, pressure 1-10 atm and molar ratio of methane to oxygen ranging from 2:1 to 10:1, wherein extraction of products of oxidative condensation of methane is carried out collectively or partly collectively with extraction of products of oxidative pyrolysis of C2-C6 alkanes, and methane, ethane and C3+ alkanes separated from reaction gases are recycled and redirected to the methane oxidative condensation and C2-C6 alkane pyrolysis steps, respectively.
EFFECT: method ensures high degree of conversion of the starting material, enables to reduce power consumption on extraction of the desired products, and reduces metal consumption of the equipment per unit product.
8 cl, 2 dwg