The method of obtaining a mixture of 2-methyl-1-naphthol, 2,4-dimethyl-1 - naphthol
(57) Abstract:Usage: substituted condensed aromatic compounds, alkylation of the alcohol, the initial products of the synthesis of vitamin K3. The inventive catalytic vapor-phase methylation of 1-naphthol with methanol is carried out at 250-380°C., a molar ratio of 1-naphthol:methanol = 1:(5-10), space velocity of the raw material 100-1000 h-1. The catalyst contains iron oxide (3), vanadium (5) and manganese (2) in the following ratio, wt.%: Fe2O343-50, V2O5(42-51), MnO - rest. Get a mixture of 2-methyl-1-naphthol, 2,4-dimethyl-1-naphthol. table 1. The invention relates to the field of organic synthesis, namely to obtain methylated napolov, in particular a mixture of 2-methyl-1-naphthol, 2,6-dimethyl-1-naphthol used as feedstock for the synthesis of 2-methyl-1,4-naphthoquinone - synthetic vitamin K3(menadione).Synthesis of 2-methyl-1,4-naphthoquinone (menadione), having the properties of vitamin K3by oxidation of 4-R-2-methyl-1-Naftalan, where R = a) H, b) CH3received on this application may be used as the basis for a new waste technologies. Existing industrial method of obtaining menadi the quality of wastewater 15 times the mass of the product, the abundance of toxic waste in excess of the weight of product in 25 times.A method of obtaining 2-methyl-1-naphthol by methylation of 1-naphthol in methanol at 320-380aboutAnd pressure 21-35 kgf/cm2in terms of liquid-phase oxidation at a molar ratio methanol : 1-naphthol 0.1-1, in the presence of a solvent is toluene, xylene, mesitylene, naphthalene or water and a catalyst of aluminum oxide at the flow rate of liquid raw materials equal to 1-10 h-1.The degree of conversion of 1-naphthol in this way is 39-49%; the yield of 2-methyl-1-naphthol 32,37-40.7 per cent.The disadvantage of this method is the low output of the basic substance - 2-methyl-1-naphthol, sections 32-40,7%, low rate of conversion of 1-naphthol, reaching 39-49%, high pressure 21-35 kgf/cm2require the establishment of special equipment for carrying out this reaction, the presence of a solvent and unreacted 1-naphthol, leading to increased energy costs associated with the separation of reactional mixture.The closest to the technical essence and the achieved result is a method of obtaining 2-methyl-1-naphthol by methylation of 1-naphthol, metanol the grow 100-5000 h-1the temperature of 300-500aboutC and a pressure of 0.5 to 20 kgf/cm2catalyst consisting of oxides of cerium, antimony, germanium, tin and magnesium.The yield of 2-methyl-1-naphthol is 54.8-95.2 per cent.The disadvantage of this method is the low yield of 2-methyl-1-naphthol average of 54.8-95.2 per cent, the highest temperature methylation contributing to the high energy intensity of production, and the presence of unreacted 1-naphthol and/or other methylated 1-Naftalan in the reaction products, leading to the holding of additional stages of purification of the target product from the side. The presence of the original 1-naphthol and/or 4-methyl-1-naphthol in quantities of 3% in methylated 1-Naftalan with their oxidation in menadione significantly reduces the yield of the final product of menadione, having the properties of vitamin K3.The aim of the invention is to increase output and simplify the process of obtaining methylated 1-Naftalan used directly for the synthesis of 2-methyl-1,4-naphthoquinone, synthetic vitamin K3.This goal is achieved by the proposed method of obtaining a mixture of methylated 1-Naftalan, including vapor-phase methylation of 1-naphthol with methanol at an elevated pace is talesfore, the distinctive feature of which is the process of methylation at a temperature of 250-380aboutWith the use of a catalyst containing the oxides of vanadium (V), manganese (II) and iron (III) in the following ratio, wt. %: Vanadium oxide 42-51 manganese Oxide 6-8 iron Oxide Rest
Application of the proposed method allows a simpler way to get methylated 1-Naftali formula 4-R-2-methyl-1-naphthol, where R = a) H (2-methyl-1-naphthol), b) -CH3(2,4-dimethyl-1-naphthol), used as feedstock for the synthesis of vitamin K3with the release of 70-98%.The inventive method is new, as stated set of essential features that characterize the way, on the filing date is unknown.The comparison of the proposed solutions not only prototype, but also with other technical solutions in this field of technology is not allowed to reveal in them the features distinguishing the claimed solution to the prototype that allows to conclude that the criterion of "substantial differences".The method is as follows.To obtain the catalyst is first thoroughly mixed oxides of vanadium, manganese and iron in mass soothe not less than 880aboutWith, the melt is cooled, crushed and classified by fractions.In a flow type reactor with external heating, internal tube diameter and length, respectively, 14 and 700 mm (laboratory setting) or 27 and 1200 mm (pilot plant), download the fraction of the catalyst with a particle size of 1-2 mm (laboratory setting) or 2-3,5 mm (pilot plant).The reaction mixture of 1-naphthol: methanol in a molar ratio of 1: (5-10) served in the reactor through the evaporator with a bulk velocity of 100-1000 h-1. The reaction is carried out at a temperature of 250-380aboutAnd pressure of 0-2 kgf/cm2. The products of methylation collect distilled off excess methanol, and the resulting reaction mixture was analyzed on the chromatographic device brand Color 104 using ionization plasma detector and the carrier gas helium, supplied with a speed of 40 ml/min, column of 1 m length, filled with 5% SE-30 on chromaton N-AW-DMCS at the temperature of the column and evaporator 180 and 300aboutRespectively.Carrying out the methylation reaction of 1-naphthol in methanol at a higher temperature leads to the increase of the content of trimethyl-1-naphthol and the decrease in the output of major products of 2-methyl-1-naphthol, 2,4-dimethyl-1-naphthol, and when Bo is 2">Carrying out the reaction of methylation at different ratios of the starting components of the reaction mixture leads to the reduction outputs methylated Naftalan or increase the energy cost of the process associated with the distillation of methanol.The increase in the volumetric feed rate of the initial reaction mixture leads to a decrease of the yield of the target products, and reducing the speed to increase output of products.The change in the ratio of catalyst components leads to a sharp decrease in its catalytic activity. The service life of the catalyst is 1000 hoursThe invention is illustrated in the examples.P R I m e R 1. To obtain the catalyst is thoroughly mixed with 52 g of vanadium oxide (V) THE 6-09-4093-88 containing the basic substance 51 g, 6 g of manganese oxide (II) THE 6-09-3217-78 and 43.9 g of iron oxide THAT 6-09-563-85 containing 43 g of the basic substance, the mixture is then melted at a temperature of not less than 880aboutWith, the melt is cooled, crushed and classified on the screens, selecting the fraction of the catalyst with a particle size of 1-2 mm, the Catalyst has a specific surface area of 0.5 m2/g and a bulk density equal to 1.82 g/cm3.30 ml of the catalyst load in the laboratory setting - t is mThe reaction mixture of 1-naphthol:methanol in a molar ratio of 1:5 submit to the reactor through the evaporator with a bulk velocity 300 h-1. The reaction is carried out at 280aboutAnd atmospheric pressure. The products of methylation containing 26,65% methanol, 1,77% 1-naphthol, 61,42% 2-methyl-1-naphthol, 10,16% 2,4-dimethyl-1-naphthol, collect. Then distilled off unreacted methanol. Conversion of 1-naphthol is 97%. The yield of 2-methyl-1-naphthol 85%, 2,4-dimethyl-1-naphthol - 12%.P R I m m e R 2. For the preparation of the catalyst are thoroughly mixed to 428.6 g of vanadium oxide (V) THE 6-09-4093-88 containing 420 g of the basic substance, 80 g of manganese oxide THAT 6-09-3217-78 and 510,2 g of iron oxide (III) THE 6-09-563-85 containing 500 g of the basic substance. The mixture is then melted at a temperature of not less than 880aboutWith, the melt is cooled, crushed and classified on the screens, selecting the fraction of the catalyst with a particle size of 2-3 .5 mm.The catalyst has a specific surface area of 0.6 m2/g and a bulk density of at 1.91 g/cm3.525 ml of catalyst was loaded into a pilot plant, a tubular flow type reactor made of stainless steel with external heating and internal tube diameter 27 mmThe reaction mixture of 1-naphthol:methanol in a molar, zootoxin is the t 2 kgf/see The products of methylation is collected and distilled off the excess methanol. Conversion of 1-naphthol is 100%. The yield of 2-methyl-1-naphthol 42%, 2,4-dimethyl-1-naphthol - 38%.P R I m e R 3. To obtain the catalyst is thoroughly mixed with 52 g of vanadium oxide (V) THE 6-09-4093-88 containing 51 g of the basic substance, 6 g of manganese oxide (II), THE 6-09-3217-78, and 43.9 g of iron (III) oxide, THE 6-09-563-85 containing 43 g of the basic substance. The mixture is then melted at a temperature of not less than 880aboutWith, the melt is cooled, crushed and classified on the screens, selecting the fraction of the catalyst with a particle size of 1-2 mm, the Catalyst has a specific surface area of 0.7 m2/g, bulk density of 1.88 g/cm3.Further methylation of 1-naphthol in methanol were analogously to example 1, the difference being that the reaction mixture of 1-naphthol:methanol was applied in a molar ratio of 1:8 with a bulk velocity of 400 h-1. The reaction was carried out at 330aboutC. Conversion of 1-naphthol was 100% , the yield of 2-methyl-1-naphthol 65%, 2,4-dimethyl-1-naphthol - 31%.P R I m e R 4. To obtain the catalyst is thoroughly mixed 469,4 g of vanadium oxide, THE 6-09-4093-88 containing 460 g of the basic substance, 70 g of manganese oxide (II), THE 6-09-3217-78, and 479,6 g of iron oxide (III), THE 6-09-563-85 containing 470 g main VT on the screens, selecting the fraction of the catalyst particle size 2-3,5 mm Catalyst has a specific surface area of 0.5 m2/g and a bulk density of 2.00 g/cm3.Further methylation of 1-naphthol in methanol were as in example 2, the difference lies in the fact that the reaction was carried out at 300aboutAnd atmospheric pressure. Conversion of 1-naphthol was 98,3% , the yield of 2-methyl-1-naphthol 81%, 2,4-dimethyl-1-naphthol 17%.P R I m e R 5. Similar to example 2, the difference is that the methylation reaction of 1-naphthol with methanol was carried out at a temperature of 250aboutC, atmospheric pressure and the reaction mixture was applied with a bulk velocity of 100 h-1. The catalyst has a specific surface area of 0.6 m2/g and a bulk density of 1.92 g/cm3. The conversion of 1-naphthol was 70% , the yield of 2-methyl-1-naphthol 53%, 2,4-dimethyl-1-naphthol 17%.The catalyst composition, its physical and catalytic properties, conditions of methylation of 1-naphthol in methanol are summarized in table.Thus, this invention allows to obtain methylated 1-Naftali formula 4 - R-2-methyl-1-Naftali, where R = a) H (2-methyl-1-naphthol), b) CH3(2,4-dimethyl-1-naphthol) or their mixtures with a large 2.9 27.7% of the output in a more simple process conditions.To obtain 2-methyl-1,4-naphthoquinone.The simplification process is to reduce the reaction temperature and pressure, the exception under division and separation of methylated 1-Naftalan. The METHOD of OBTAINING a MIXTURE of 2-METHYL-1-NAPHTHOL, 2,4-DIMETHYL-1-NAPHTHOL catalytic vapor-phase methylation of 1-naphthol in methanol at elevated temperature, a molar ratio of 1-naphthol : methanol 1 : (5 - 10) and the space velocity of the feedstock 100 - 1000 h-1, characterized in that, to increase the yield of the target products and simplify the process, the methylation reaction is carried out at 250 - 380oWith the use of a catalyst containing the oxides of vanadium (V), manganese (II) and iron (III) in the following ratio, wt.%:
The vanadium oxide - 42 - 51
Manganese oxide - 6 - 8
Iron oxide - Rest
SUBSTANCE: catalytic composition contains compounds of formula: Mo1VaSbbNbcMdOx, in which Mo represents molybdenum, V stands for vanadium, Sb stands for antimony, Nb stands for niobium, M represents gallium, a constitutes from 0.01 to 1, b constitutes from 0.01 to 1, c constitutes from 0.01 to 1, d constitutes from 0.01 to 1, and x is determined by requirements of valency of other present elements.
EFFECT: increase of alkane conversion degree, increase of selectivity of catalytic composition in one stage process of alkane transformation into unsaturated carbonic acid.
9 cl, 1 tbl, 12 ex
SUBSTANCE: described is mass of metal oxides, intended as catalyst for heterogeneously-catalysed partial oxidation and/or ammoxidation of at least one saturated and/or unsaturated hydrocarbon, of general stechiometry I MO1VaM1 bM2 cM3 dOn (I), were M1= stands for Te; M2=stands for Nb; M3= stands for at least one of elements from group, which includes Pb, Ni, Co, Bi and Pd; a = 0.05 to 0.6, b= 0.01 to 0.5, c= 0.01 to 0.5, d = 0.0005 to 0.5 and n= equals the number determined by valence and number of different from oxygen elements in (I), whose X-ray diffractogragm has diffraction reflexes h, i and k , whose peaks are at diffraction angles (2Θ) 22.2±0.5° (h), 27.3±0.5° (i) and 28.2±0.5° (k), and - diffraction reflex h in the range of X-ray diffractogram is the most intensive and has peak half-width maximal value 0.5°, intensity Pi of diffraction reflex i and intensity Pk fulfill ratio 0.65≤R≤0.85, in which R is determined by formula R=Pi/(Pi+Pk) intensity ratio, and - half-width of diffraction reflex i and diffraction reflex k each constitute ≤1°, and at least one mass of metal oxides (I) represents such, X-ray diffractogram of which does not have diffraction reflex with peak position 2Θ=50.0±0.3°. Described is mass of metal oxides, which contains equal or more than 80 wt % of at least one mass of metal oxides, indicated above, and whose X-ray diffractogram has diffraction reflex with peak 2Θ=50.0±0.3°.Also described are methods of heterogeneously catalysed partial gas phase oxidation or ammoxidation of at least one saturated or unsaturated hydrocarbon, using as catalytic active mass at least one mass of metal oxides, described above. Described is method of obtaining metal oxides mass by mixing sources of its elementary components, calcination of dry mixture at 350-700°C and washing by organic and/or inorganic acid solution.
EFFECT: increasing target product selectivity.
17 cl, 1 tbl, 16 ex, 17 dwg
SUBSTANCE: present invention relates to mixed metal oxide oxidation catalysts and ammonolysis of propane and isobutane, methods of obtaining them and usage. Described is a mixed metal-oxide system, containing molybdenum, vanadium, niobium, antimony, germanium and oxygen or molybdenum, vanadium, tantalum, antimony, germanium and oxygen, with the following stoichiometric ratios of elements: molybdenum to antimony from 1:0.1 to approximately 1:0.5, and molybdenum to germanium from 1:>0.2 to approximately 1:1. Description is given of a catalyst, which is a mixed metal-oxide system, effective in vapour-phase conversion of propane to acrylic acid or acrylonitrile or conversion of isobutane to methacrylic acid or methacrylonitrile. The mixed metal-oxide system has an empirical formula Mo1VaNbbSbcGedOx or Mo1VaTabSbcGedOx, in which a ranges between 0.1 and 0.6, b ranges between 0.02 and 0.12, c ranges between 0.1 and 0.5, d ranges from more than 0.2 to 1, and x depends on the oxidation number of other elements in the mixed metal-oxide system. Described also is a method of obtaining the system described above, involving the following stages: addition into a reaction vessel of precursors Mo, V, Nb or Ta, Ge and Sb in an aqueous solvent to form a reaction medium with initial pH 4 or less, and optional addition of another aqueous solvent into the reaction vessel; sealing the reaction vessel; reaction of the reaction mixture at temperature above 100°C and pressure above atmospheric pressure for a period of time, sufficient for formation of a mixed metal-oxide system; optional cooling of the reaction mixture; and extraction of the mixed metal-oxide system from the reaction mixture. Description is given of a method of converting propane into acrylonitrile and isobutane into methacrylonitrile using the catalyst described above.
EFFECT: simple technology of making catalyst, increased catalyst activity and output of the target product in reactions of oxidative ammonolysis of propane and isobutane.
27 cl, 8 tbl, 50 ex, 1 dwg
SUBSTANCE: description is given of a method of obtaining an active phase of a heterogeneous catalyst based on oxides or mixed oxides of transition metals, chosen from a group containing Mo, V, Te, Nb, through successive mixture of aqueous solutions of molybdenum tellurate, vanadium sulphate and niobium oxalate. An aqueous solution of vanadium sulphate is added to the molybdenum tellurate solution first, obtaining a suspension after mixing, which is then added to niobium oxalate. The obtained mixture is further intensively stirred for 10 minutes, kept in an autoclave at 175°C for 50 hours and after filtration and washing, roasted at 600°C in a stream of inert gas. The heterogeneous catalyst for oxidative dehydrogenation of gaseous mixtures of hydrocarbons is a composite material in form of a mechanical mixture of solid dispersion powders obtained from an active phase and an inactive phase with specific surface area of 1-10 m²/g, relative the active dispersion matrix. The method of obtaining the catalyst involves mechanical mixture of powders of active and inactive phases with subsequent pressing, crushing and grading the particles through sieving. Described also is a method of oxidative dehydrogenation of ethane, in which a gas mixture, containing oxygen and ethane in ratio ranging between 1:2.5 and 1:3.5, is fed at pressure of 1 atm and bulk speed of 500-30000 h-1 into a flow reactor with a stationary layer of the heterogeneous catalyst described above, heated to 380-420°C.
EFFECT: increased output of the dehydrogenation process, while maintaining high conversion and selectivity.
11 cl, 1 tbl, 4 ex
FIELD: process engineering.
SUBSTANCE: invention relates to oxide catalysts for catalytic processes of hydrocarbon oxidative dehydration, in particular to oxidation catalysts. Oxidation catalyst for catalytic processes of hydrocarbon oxidative dehydration based on oxides of transition metals or mixes thereof selected from the group comprising Mo, V, Te, Nb of empirical formula MoaVbTecNbd, where a, b, c, d are gram-atomic proportions of corresponding elements, represents a geometrically structured solid calcinated structure with content of lattice oxygen not below 0.4 mmole of O2/g and containing the components in the following molar ratios: molybdenum (a) - >1.00-1.50; vanadium (b) - 0.20-2.00; tellurium (c) - 0.20-1.50; niobium (d) - 0.01-1.50.
EFFECT: yield of product not lower than 1000 g per kg of catalyst at high conversion (approx 30-50%) and selectivity not worse than 95-97%.
2 ex, 1 tbl
SUBSTANCE: invention relates to production of hydrofining catalysts. Described is a catalyst for hydrofining heavy petroleum cuts which contain active components: [Si·(WO3)12] in amount of 1.0-9.0 wt %; [P-(WO3)12] in amount of 1.0-9.0 wt %; [Si-(MoO3)12] in amount of 4.0-22.0 wt %; [P-(MoO3)12] in amount of 6.0-22.0 wt %; active component promoter - nickel oxide NiO, in amount of 3.0-8.0 wt %; carrier modifier - V2O5 in amount of 0.5-5.0 wt % and SnO2 in amount of 0.1-4.0 wt %; aluminium oxide Al2O3 in amount of 84.4-21.0 wt %. Described also is a method of preparing said catalyst, involving saturation of the carrier with a solution of a molybdenum or nickel compound, involving synthesis and saturation of the modified carrier: V2O5, SnCl4·5H2O, H4[Si(W12O40)]·10H2O, H4[P(W12O40)]·10H2O is added to aluminium hydroxide peptised with a monobasic acid; the mixture of starting compounds is evaporated to residual moisture of 60-70%, moulded in form of extruded articles, dried and calcined, with the final calcination temperature of the carrier equal to 550°C; the calcined extruded articles then undergo one-time saturation with an impregnating solution which contains heteropoly-compounds of molybdenum H4[Si(Mo12O40)]·21H2O, H4[P(Mo12O40)]·14H2O and nickel nitrate Ni(NO3)2·6H2O, with pH of the medium equal to 3.0-5.5, followed by thermal treatment of the ready catalyst.
EFFECT: catalyst characterised by high activity when hydrofining heavy petroleum cuts is obtained.
5 cl, 3 tbl, 7 ex
SUBSTANCE: invention relates to a method for liquid-phase synthesis of isoprene by reacting formaldehyde with isobutylene or derivatives thereof in the presence of a solid-phase catalyst and subsequent extraction of the end product, characterised by that the catalyst used is phosphates selected from zirconium, niobium or tantalum phosphates, wherein the reaction takes place at temperature 100-200°C, pressure 7-20 atm and molar ratio of isobutylene or derivative thereof to formaldehyde equal to (1-20)/1.
EFFECT: use of the method enables synthesis of isoprene with high output and selectivity.
7 cl, 17 ex, 1 tbl
SUBSTANCE: invention relates to a method of processing isoprene synthesis intermediate products obtained during condensation of formaldehyde and isobutylene or derivatives thereof, involving decomposition of synthesis intermediate products on a catalyst to obtain isoprene, characterised by that the catalyst used is zirconium, niobium or tantalum phosphate, or said phosphates deposited on an inorganic support, and the process is carried out at 100-200°C, pressure 7-20 atm, with mass flow rate of the liquid-phase isoprene synthesis intermediate products onto the solid-phase catalyst of 0.5-15 g/g h.
EFFECT: use of present invention simplifies the processing method and increases isoprene output.
3 cl, 12 ex, 1 tbl
SUBSTANCE: invention relates to a method of producing isoprene by reacting components of a raw material containing formaldehyde, isobutylene, isobutylene derivatives and isoprene precursors in the presence of a solid-phase acid catalyst which contains niobium phosphate, followed by separation of the end product. The method is characterised by that reaction of formaldehyde with isobutylene, isobutylene derivatives and isoprene precursors is carried out in molar ratio of isobutylene and derivatives thereof to formaldehyde of (3.5-8):1, molar ratio of isobutylene derivatives to isobutylene of (0.75-3.5):1, molar ratio of formaldehyde to isoprene precursors of (4-10):1, the raw material is fed into the reactor at temperature of 140-160°C and pressure of 13-17 atm in form of a continuous gas-liquid stream with volume rate of the gas phase of 20-250 h-1 and of the liquid phase of 10-25 h-1.
EFFECT: use of the present method increases isoprene output and reduces output of high-boiling by-products.
3 cl, 1 dwg
SUBSTANCE: invention relates to catalytic purification of exhaust gases of internal combustion engines. Claimed is composition for purification of exhaust gases of internal combustion engines based on cerium oxide, containing niobium oxide, with the following weight contents: niobium oxide from 2 to 20%, the remaining part - cerium oxide. Also claimed is composition with the following weight contents: cerium oxide at least 65%, niobium oxide from 2 to 12%, zirconium oxide to 48%. After calcinations for 4 hours at 800°C compositions have acidity at least 6·10-2, with said acidity being expressed in ml of ammonia per m2 of composition, with the surface, expressed in m2, used for determination of acidity, representing specific surface after calcinations for 4 hours at 800°C and specific surface at least 15 m2/g, and after calcinations for 4 hours at 1000°C it has specific surface at least 2 m2/g, in particular at least 3 m2/g. Invention relates to catalyst, which contains said compositions, to methods of oxidising CO and hydrocarbons, N2O, decomposition, for HOx and CO2 adsorption. Said compositions and catalyst are applied in reaction of gas with water, reaction of conversion with water steam, isomeration reaction, reaction of catalytic cracking and as triple action catalyst.
EFFECT: compositions possess satisfactory reducing ability in combination with good acidity, specific surface of which remains suitable for application in catalysis.
16 cl, 1 tbl, 14 ex
SUBSTANCE: invention relates to chemistry and can be used in removing sulphur oxides from recycle gases in the presence of a catalyst. The catalyst contains an active part, containing magnesium and calcium oxides, deposited on an alumina support. The active part additionally contains manganese oxide in the following ratio of components, wt %: magnesium and calcium oxide 6.0 to 20.0, manganese oxide 0.03 to 1.00, carrier - the rest to 100. Aluminium oxide trihydrate, annealed at temperature ranging from 750 to 900°C and saturated with active components at pH 0.5 to 2.5, is used as the carrier.
EFFECT: invention simplifies technology of producing catalyst, reduces damaging effect on the environment, reduces cost of catalyst.
3 cl, 4 ex
SUBSTANCE: invention relates to catalytic cracking of hydrocarbons. Described is method of obtaining light olefins by catalytic cracking of hydrocarbons with 4 or more than 4 carbon atoms, with boiling point 30-200°C, in presence of catalyst, characterised by the fact that 0.01-5.0 wt % of MnO2 and 1-15 wt % of P2O5 are simultaneously added to catalyst components, where catalyst components contain 1-50 wt % of zeolite, 21-70 wt % of clay and 1-40 wt % of inorganic oxide and where both MnO2 and P2O5 are introduced into (modify) each of catalyst components, such as ZSM-5 zeolite, clay and inorganic oxide.
EFFECT: increase of product outcome.
10 cl, 1 dwg, 6 tbl, 9 ex
FIELD: oil and gas industry.
SUBSTANCE: invention relates to the catalyst, containing the hexaaluminate, in which there is the hexaaluminate containing phase, including cobalt in the amount from 2 up to 15 moll. % and at least one other element, selected from the group consisting of lanthanum, barium and strontium in the amount from 2 up to 25 moll. %, and the amount of aluminium is from 70 up to 90 moll. %. Besides the hexaaluminate containing phase in the catalyst, there is from 0 up to 50 wt % of the accessory oxide phase. The proposed catalyst production method contains according to the invention the aluminium source preparing, preferably alumina and/or aluminium hydroxide (boehmite), in the form of dispersible primary particles ≤with the size 500 nm; placing into contact of the fine aluminium source to the fusible or soluble cobalt containing compound, and at least one soluble or fused salt of the metal, selected from the group consisting the barium, lanthanum and strontium; careful mixing of the aluminium source with dissolved, or, respectively, molten metal salts; the mixture drying; the mixture low-temperature calcination; moulding, or respectively shaping. Besides, the invention relates to the gas reforming method, containing more than 70 vol. % of hydrocarbons, preferably methane and in the presence of carbon dioxide, with the hexaaluminate catalyst, which is heated at the contact with gas to be reformed at the temperature above 700°C, preferably above 800°C, more preferably above 900°C in the reactor, the pressure higher than 5 bar, preferably higher than 10 bar, more preferably above 15 bar, the space velocity of the reforming gas, placed into contact to the catalyst, is in the range from 500 to 20,000 h-1, and the catalyst containing hexaaluminate, contains the cobalt and at least one other metal, selected from the group, consisting of barium, strontium and lanthanum.
EFFECT: catalyst with the low lanthanum content, with high coking resistance and high catalytic activity, using over the long periods of time in extremely hard process conditions.
15 cl, 4 dwg, 6 tbl
SUBSTANCE: invention relates to the methods for producing oxide catalysts on a metal support substrate that can be used in oxidation reactions of CO to CO2, which take place in the high-temperature processes for cleaning process and exhaust gases, in particular in the energy and automotive industries. The proposed method includes anodizing an aluminium substrate in a galvanostatic mode at the current density of 10-15 mA/cm2 for 20-60 min in 3% aqueous solution of oxalic acid C2H2O4, washing and drying, after which the intermediate porous alumina layer formed on the aluminium substrate is treated with a 1% solution of phosphoric acid heated up to 35°C, washed, dried, and applied to the treated aluminium substrate, ultrafine manganese dioxide, which is formed by impregnation with a 5% solution of potassium permanganate KMnO4 followed by annealing in air at 220-230°C for 10 minutes, while the operation of applying manganese dioxide can be carried out three times.
EFFECT: simplification and cheaper technology while expanding the range of composite catalytic materials containing a metal substrate with supported transition metal oxides.
2 cl, 4 dwg, 2 ex
SUBSTANCE: invention refers to a method for the one-stage production of (3-hydroxypropyl)naphthols of having a structure of R1=CH2CH2CH2OH, R2=OH, R3=H; R1=OH, R2=CH2CH2CH2OH, R3=H; R1=OH, R2=CH2CH2CH2OH, R3=CH2CH2CH2OH; R1=OH, R2=T-Bu, R3=CH2CH2CH2OH, effective biologically active substances of neutropic action. The method consists in conducting a reaction of α-, β-naphthols, their derivatives or their sodium salts with allyl alcohol and alkali at temperature 100-170°C. A purified product yield is 40-60%.
EFFECT: higher yield.
SUBSTANCE: application relates to a marking label for gasolines which represents hydroxyl-containing derivatives of aromatic series, wherein the hydroxyl group is connected directly to the aromatic ring, selected from a series of resorcinol, 4-hexylresorcinol or β-naphthol. The proposed label can be used in low concentrations.
EFFECT: absence of its influence on the performance characteristics of marked gasolines.
3 dwg, 4 ex