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Catalytic gas-phase fluorination Invention refers to a method for fluorination, which involves: the stage of activation involving contacting a fluorination catalyst and a gas flow containing an oxidant for at least one hour; and at least one reaction stage involving a reaction of a chlorinated compound and hydrogen fluoride in the gas phase in the presence of the fluorination catalyst to produce the fluorinated compound. The gas flow containing the oxidant is free from hydrogen fluoride. |
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Synthetic gas production method Invention is referred to the area of petroleum chemistry and may be used for synthesis of methanol, dimethyl ether, hydrocarbons according to Fischer-Tropsch method. Methane-containing raw material is subjected to oxidative conversion at temperature of 650-1100°C in the riser. Miscrospheric or shredded catalyst based on metal oxides capable of multiple reduction-oxidative transfers is used as the oxidizer. Regenerated catalyst is recovered by its oxidation in the regenerator and addition to the riser in the bottom-up flow of methane-containing raw material; the riser operates in a through flow mode and duration of the raw material stay in the reaction area is 0.1-10 s. The regenerated catalyst exiting from the riser is separated from the product of synthetic gas and delivered to the regenerator. Catalyst regeneration is performed in fluidized, forced fluidized or semi-through flow by oxidation with oxygen-containing agent. The produced synthetic gas has H2/CO ratio within the range of 7.5-2.5. |
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Regenerated catalyst of hydroprocessing Catalyst of hydroprocessing is obtained by the fixation of molybdenum and at least one component, selected from metals of 8-10 groups of the Periodic table, on an inorganic carrier, which contains aluminium oxide, in which the content of residual carbon is in the interval from 0.15 wt % to 3.0 wt %, intensity of peak of a molybdenum-containing complex metal oxide relative to the intensity of the main peak is in the interval from 0.60 to 1.00 in the X-ray diffraction spectrum (X-Ray), and either the intensity of peak of Mo-S bond, derivative from the peak of residual sulphur, relative to the intensity of the main peak is in the interval from 0.10 to 0.60 on a radial distribution curve, obtained from a spectrum of long fine structure of X-ray absorption in the analysis of the fine structure of X-ray absorption, or a part of Mo-S is in the interval from 77% to 99% in the structure spectrum close to the edge of X-ray absorption (X-ray), obtained in the analysis of the fine structure of X-ray absorption. The invention also relates to a method of obtaining a petroleum product, in which hydroprocessing of petroleum fraction is performed with the application of the said regenerated catalyst of hydroprocessing. |
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Method of catalyst regeneration Invention relates to methods of catalyst regeneration. First claimed method of regeneration is characterised by the fact that spent catalyst from reactor is introduced into first regenerator with fluidised bed, where it contacts oxygen-containing gas flow and, randomly, with water vapour to realise reaction of coke burning under conditions of regeneration, including range of temperatures from 550°C to 750°C, the average time of catalyst exposure being from 0.5 min to 6 min with ratio of vapour to oxygen-containing gas flow by weight being within the interval from 0 to 0.1. Obtained mixture of partly restored catalyst and smoke gas is introduced into second regenerator with fluidised bed and contacts water vapour and additional flow of oxygen-containing gas to realise further reaction of regeneration under conditions of regeneration including range of temperatures from 550°C to 700°C, the average time of catalyst exposure being in the range from 3 min to 30 min and oxygen-containing gas flow. Ratio of vapour to oxygen-containing gas flow by weight is selected in the range from 0 to 500. After that, regenerated catalyst is introduced into reactor. Second claimed method of catalyst regeneration is characterised by the fact that spent catalyst from reactor is introduced into regenerator with dense fluidised bed, where it contacts flow of oxygen-containing gas and vapour to realise reaction of coke burning under conditions of regeneration, including range of temperatures from 550°C to 750°C, the average time of catalyst exposure being in the interval from 4 min to 30 min and presence of water vapour. Ratio of vapour to oxygen-containing gas flow by weight is selected in the interval from 0 to 0.2, with vapour being introduced into regenerator with dense fluidised layer. After that, regenerated catalyst is introduced into reactor. |
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Method of producing regenerated hydrofining catalyst and method of producing petrochemical product Disclosed is a method of preparing a regenerated hydrofining catalyst by regenerating a spent hydrofining catalyst in a given temperature range, where the given temperature range is from T1 -30°C or higher to T2 +30°C or lower, said temperature range being defined by conducting differential thermal analysis of the spent hydrofining catalyst, converting differential heat in a temperature measurement range from 100°C or higher to 600°C or lower into an electromotive force difference, double differentiation of the converted value on temperature to obtain the least extremal value and a second least extremal value, and presenting temperature which corresponds to the extremal value at the side of lower temperatures as T1 and temperature corresponding to the extremal value at the side of higher temperatures as T2. The invention also discloses a method of producing a petroleum product using said catalyst and the regenerated catalyst itself. |
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Method of catalytic pyrolysis of methylene chloride Pyrolysis of methylene chloride is carried out on a catalyst with a carbonisation degree in the range of 2.6-5.2 wt %, which is obtained during 60-150 minutes of a reactor work, after which in order to support the obtained degree of carbonisation a catalyst is constantly discharged into a regenerator, excessive carbon is removed by burning with air at a temperature of 550°C. After that it is returned into the reactor, providing constant circulation of the carbonised catalyst from the reactor of pyrolysis into the regenerator and back. |
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Invention relates to catalysis. Described is a method of regenerating one or more particles of a cobalt-containing Fischer-Tropsch catalyst in situ in a reactor tube, the method comprising steps: (i) oxidising the catalyst particle(s) at temperature of 20-400°C; (ii) treating the catalyst particle(s) for more than 5 min with a solvent; (iii) drying the catalyst particle(s); and (iv) optionally reducing the catalyst with hydrogen or any hydrogen-containing gas. |
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System and method of catalyst activation Described are methods of chrome catalyst activation, which include increasing chrome catalyst temperature in, at least, bilinear changing, which contains increase of chrome catalyst temperature at first speed during first period of time to first temperature on first site of changing of bilinear changing; and increase of chrome catalyst temperature at second speed during second period of time from said first temperature to second temperature on second site of changing of bilinear changing, which follows directly after first area of changing, and first speed is larger, than second speed, and first period precedes second period; with first temperature being in the range from approximately 650°C to approximately 750°C, with second temperature being in the range from approximately 750°C to approximately 850°C. Method of obtaining polyolefines in presence of catalyst, activated by claimed method, is described. |
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Method of producing c3-c5 olefin hydrocarbons and catalyst therefor Described is a method of producing C3-C5 olefin hydrocarbons via dehydrogenation of corresponding C3-C5 paraffin hydrocarbons or mixtures thereof in the presence of a catalyst which contains chromium oxide, zinc oxide, aluminium oxide and additionally a aluminium-magnesium spinel and at least tin oxide in amount of 0.1-3.0 wt %. Before the regeneration step, reaction products are removed from the catalyst by first passing C1-C5 hydrocarbons or mixtures thereof and then nitrogen through the catalyst. The catalyst contains chromium oxide, zinc oxide, aluminium oxide, aluminium-magnesium spinel and tin oxide, with the following ratio of components in terms of oxides, wt %: Cr2O3 - 10.0-30.0, ZnO - 10.0-40.0, SnO2 - 0.1-3.0, MgO - 1.0-25.0, Al2O3 - the balance. The catalyst can further contain a manganese compound in amount of 0.05-5.0 wt %. |
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Invention relates to field of catalyst. Described is method of regenerating waste catalytic mixture, which contains (i) catalyst of isomerisation, containing magnesium oxide, and (ii) metathesis catalyst, which contains inorganic carrier and at least one component from molybdenum oxide and tungsten oxide, which includes: (a) removal of coke from waste catalytic mixture in presence of oxygen-containing gas, with obtaining coke-free catalytic mixture; and (b) contact of coke-free catalytic mixture with steam at temperature in the interval from 100 to 300°C with obtaining regenerated catalytic mixture. |
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Invention relates to a regenerated hydrofining catalyst, a method of regenerating deactivated catalysts and a method of hydrofining oil distillates. Described is a regenerated catalyst for hydrofining hydrocarbon material, having pore volume of 0.3-0.8 ml/g, specific surface area of 150-280 m2/g, average pore diameter of 6-15 nm, which contains molybdenum, cobalt or nickel, sulphur and a support, wherein the molybdenum, cobalt or nickel is contained in the catalyst in form of nitrate complexes of compounds Co(C6H6O7), Ni(C6H6O7), H4[Mo4(C6H5O7)2O11], and the sulphur is contained in form of a sulphate anion SO4 -2 in the following concentrations, wt %: Co(C6H6O7) or Ni(C6H6O7) - 7.3-16.6; H4[Mo4(C6H5O7)2O11] - 17.3-30.0; SO4 -2 - 0.25-2.70; support - the balance; cobalt or nickel citrates can be coordinated to molybdenum citrate. Described is a method of regenerating a catalyst for hydrofining hydrocarbon material according to which a deactivated catalyst is fired and then saturated with citric acid solution and the dried in conditions which enable to obtain the catalyst described above. Described is a method of hydrofining hydrocarbon material at temperature of 320-400°C, pressure 0.5-10 MPa, weight flow rate of material of 0.5-5 h-1, volume ratio hydrogen/material equal to 100-1000 m3/m3 in the presence of the catalyst described above. |
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Regeneration of alkane dehydrogenation catalysts Invention relates to a method of dehydrogenating alkanes, according to which a mixture containing hydrocarbons, particularly alkanes, which can contain water vapour, is continuously fed through a catalyst bed at ordinary dehydrogenation conditions. The many-hours-long dehydrogenation step is followed by a step with bleeding of oxygen-free gas through a reactor layer in order to blow and remove reaction gas from the reactor layer, and this is followed by a step for bleeding oxygen-containing regeneration gas in order to remove deposits on the catalyst formed during the dehydrogenation reaction. This is followed by a step for bleeding oxygen-free gas in order to blow and remove regeneration gas from the reactor. Duration of bleeding oxygen-containing gas during catalyst regeneration is equal to or less than 70% of the total duration of regeneration, total regeneration time is equal to 1 hour and regeneration starts after a seven-hour step of obtaining the product. The method is characterised by that regeneration starts with a five-minute blowing step, followed by a step for regeneration with a gas which contains oxygen and water vapour for 20 minutes, followed by an additional blowing step. |
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Described is purifying from disperse particles material, used for filter-catalyst for purification from disperse particles, and filter-catalyst is located on the way of flow of exhaust gases of internal combustion engine, catching disperse particles in exhaust gases, which are formed in internal combustion engine, and burning precipitated disperse particles in order to be regenerated, and purifying from disperse particles material includes: oxide, containing cerium (Ce), possessing ability to accumulate-release oxygen; and at least one metal (Me), selected from group, consisting of zirconium (zr), yttrium (Y), lanthanum (La), praseodymium (Pr), strontium (Sr), nioubium (Nb) and neodymium (Nd), and ratio of content of (Ce:Me) cerium to metal constitutes from 6:4 to 9:1 in units of atomic ratio, and degree of crystallinity (CR), represented by the following formula (1), lies within the range 36-60%: Degree of crystallinity (CR)=I/I0× 100(%) (1), where I represents intensity of X-ray diffraction peak with respect to plane (111) of phase CeO2 in purifying from disperse particles material, and I0 stands for intensity of X-ray diffraction peak with respect to plane (111) of phase CeO2 after roasting material, which purifies from disperse particles, in the air at 1000°C. Described is filter-catalyst for purification from disperse particles, which is located on the way of flow of exhaust gases of internal combustion engine, catching disperse particles in exhaust gases, which are formed in internal combustion engine, and burning precipitated disperse particles in order to be regenerated, and filter-catalyst includes: filter-carrier, made from porous ceramics with continuous small pores; and layer of catalyst, formed on the wall of filter-carrier, and catalyst layer contains: 25-100 g/l of mixture of described above purifying from disperse particles material and noble metal; and 0.25-1.0 g/l of noble metal, counted per unit of volume of filter-carrier. Described is method of regeneration of described above filter-catalyst, including control of internal temperature of filter-catalyst at the level from 350°C to 800°C, thus ensuring burning and removal of disperse particles, precipitated on filter-catalyst. |
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Controlled execution of thermocompressors for continuous catalyst regeneration Invention relates to catalyst regeneration. Described is a catalyst regeneration system comprising: a catalyst regeneration column (104), having a cooling zone (112) which receives a catalyst cooling stream (148); a first thermocompressor (138) using first working steam (142); and a second thermocompressor (140), arranged in parallel to the first thermocompressor, in which nitrogen is used as the working steam (152); and one or more valves (154) which are able to selectively direct the cooling stream (132) into at least one thermocompressor selected from the first thermocompressor (138) or the second thermocompressor (140) to obtain a catalyst cooling stream (148). Described is a catalyst regeneration system method involving: removing a first gas stream (118) from the regeneration column (104); feeding the first gas stream (118) into an air heater (122) to obtain a heated first gas stream (124); splitting the heated first stream (124) to obtain a return stream (126) of the regeneration column and a cooling loop stream (128); cooling the cooling loop stream (128) in the cooler (130) of the cooling zone to obtain a cooled stream (132); selectively feeding the cooled stream (132) into at least one thermocompressor selected from the first thermocompressor (138) using first working steam (142) or the second thermocompressor (140) using nitrogen as the second working steam (152), to obtain a catalyst cooling stream (148); and feeding the catalyst cooling stream (148) into the regeneration column (104). |
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Invention discloses a method of producing a highly active catalyst for reforming resin-containing gas, where resin-forming gas is formed during thermal decomposition of carbon material. The method involves obtaining a catalyst by adding a precipitation agent to a mixed solution of a nickel compound and a magnesium compound, forming a precipitate via coprecipitation of nickel and magnesium, forming a mixture by adding aluminium oxide powder and water or aluminium oxide sol to said precipitate, stirring and at least drying and calcining said mixture, where the catalyst for reforming resin-containing gas is obtained such that nickel content ranges from 1 to 50 wt %, magnesium content ranges from 5 to 45 wt %, and aluminium oxide content ranges from 20 to 80 wt %, wherein the resin-containing gas contains 20 ppm or more hydrogen sulphide. The invention also discloses a version of the method of producing the catalyst, methods of reforming resin and catalyst regeneration methods. The catalyst is resistant to carbon deposit even when reforming resin-containing gas with high content of hydrogen sulphide. The catalyst is highly efficient. Regeneration ensures stability of the catalytic result and consistency of results until regeneration. |
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Method for regenerating catalyst for producing isoprene from 4,4-dimethyl-1,3-dioxane Invention relates to methods of regenerating catalysts. Described is a method of regenerating a catalyst for producing 4,4-dimethyl-1,3-dioxane by firing coke and resin in the presence of water vapour and air or an oxygen-containing mixture in series-connected reactors at temperature 400-500°C and pressure in the first reactor of 0.9-1.4 atm and pressure at the output of the second reactor of 0.5-0.7 atm. |
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Procedure for processing gas condensate Here is disclosed procedure for processing gas condensate consisting in its preliminary heating in corresponding process vessels, in contacting in adiabatic reactor at temperature 320-480°C and pressure 0.1-4 MPa with zeolite containing catalyst, in cooling and in separation of reaction products into gaseous and liquid fractions by separation and rectification, and in successive oxidising regeneration of catalyst. Also, prior to process of regeneration heavy resins collected on catalyst are removed by vacuumising of adiabatic reactor during 0.5-6.0 hours. Catalyst is regenerated in a regenerator at temperature 350-620°C and pressure 0.1-0.2 MPa with air with contents of oxygen 21 vol. %. Upon heating an upper or lower layer of catalyst air is supplied from a side opposite to a heated layer. |
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Method of processing catalyst when converting oxygen-containing compounds to olefins Invention relates to a method of separating and freeing a catalyst during conversion of oxygen-containing compounds to olefins, involving the following steps: (a) converting oxygen-containing compounds to olefins in a fluidised zone in a reactor in the presence of a molecular sieve type catalyst, having carbon-containing deposits, where said oxygen-containing compounds are selected from a group consisting of methanol, ethanol, dimethyl ether or mixtures thereof; (b) tapping the output stream containing olefins from the reactor, where the output stream surrounds part of the catalyst, having carbon-containing deposits; (c) separation of part of the catalyst from the output stream through contact of the output stream with neutralised liquid slaking medium in a slaking column in order to form a stream which contains the catalyst; where neutralisation of the slaking medium is carried out in a separate section after separating part of the catalyst; and (d) burning in an installation for burning carbon-containing deposits which are in that part of the catalyst which lies in the stream containing the catalyst. |
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Present invention relates to a method of regenerating catalytic activity of a spent hydrogen processing catalyst which does not contain an additive. A method is described for regenerating catalytic activity of a spent hydrogen processing catalyst which does not contain an additive (versions), which involves: bringing a spent non-additive containing hydrogen processing catalyst which contains a metal component and carrier material, which has low catalytic activity with respect to the catalyst in fresh state before its use, which results in the catalyst being spent, with a solution, where the said solution contains a chelating agent chosen from a group of compounds consisting of amino carboxylic acids, and a solvent, and where said contacting takes place in a period of time longer than 10 hours, with provision for regenerated catalytic activity, obtaining old catalyst containing said chelating agent and said solvent, where said spent hydrogen processing catalyst contains amount of said chelating agent in the interval from 0.005 mole of chelating agent per mole of active metal to 1 mole of chelating agent per mole of active metal; keeping said old catalyst in conditions which include drying temperature so as to remove part of said solvent from said old catalyst with removal of not less than 50 wt % of said chelating agent from said old catalyst, obtaining dried old catalyst as a result; and treatment of said dried old catalyst with sulphur, obtaining regenerated catalyst. Also described is a catalyst produced using methods described above and hydrogen processing method, involving bringing hydrocarbon starting material in hydrogen processing conditions with a catalyst produced using methods described above. |
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Present invention relates to a method of regenerating catalytic activity of spent catalyst. A method is described for regenerating catalytic activity of spent water treatment catalyst (versions), where the said method involves: provision for said spent water treatment catalyst with first carbon concentration of over 3 wt %; reduction of carbon concentration on the said spent water treatment catalyst, obtaining catalyst with low carbon concentration as a result, with second carbon concentration ranging from 0.5 wt % to 2.5 wt %, with bringing the said spent water treatment catalyst into contact with oxygen-containing gas in carbon burning conditions and regulation of amount of carbon removed from the said spent water treatment catalyst so as to obtain the said catalyst with low carbon concentration, with the said second carbon concentration; and bringing the said catalyst with low carbon concentration into contact with a solution which contains a chelating agent and a solvent so as to introduce the said chelating agent into the said catalyst with low carbon content; ageing of the said catalyst with low carbon content, containing the said solution during ageing time, obtaining aged catalyst as a result, where the said ageing time is sufficient for regenerating catalytic activity of said catalyst with low carbon content; and drying the said aged catalyst with removal of part of the said solvent from the said aged catalyst, obtaining dried aged catalyst as a result; and sulphur treatment of the said dried aged catalyst, that way obtaining the said regenerated catalyst. |
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Present invention pertains to the method of prolonged heterogeneous catalysed partial oxidation of propene to acrolein in gaseous phase. The initial reaction gaseous mixture, containing propene, molecular oxygen and at least one inert gas-diluting agent, is passed through a fixed catalyst bed at high temperature. The catalysts are such that, their active mass contains at least, one multi-metal oxide, which contains molybdenum and/or tungsten, as well as at least, one of the elements bismuth, tellurium, antimony, tin, and copper. The temperature of the catalyst bed is increased for a period of time. Partial oxidation in gaseous phase is interrupted at least, once in a calendar year, and at 250-550°C temperature of the fixed catalyst bed a gas mixture, containing molecular oxygen, inert gas and, if necessary, water vapour, is passed through the fixed catalyst bed. |
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Process for thermal removal of coke from zeolite catalyst and apparatus Invention relates to a process and apparatus for thermal removal of coke from loose mass of granulated selective zeolite catalyst based on pentasil-type crystalline aluminosilicates for production of olefins having 2 and 3 carbon atoms from mixture of olefins having 4-8 carbon atoms or methanol or dimethyl ether. Process is carried out in reactor (1) wherein catalyst is used in the form of loose mass. In preliminary stage, reactor (1) is flushed by heated nitrogen stream at entry temperature 460-500°C in order to replace hydrocarbons out of catalyst. Then, reactor is cooled by heated nitrogen stream at entry temperature from 420 to less than 460°C. In the main stage, nitrogen/air mix slowly heated to entry temperature 460-500°C is passed through reactor and, in additional stage, reactor is flushed by nitrogen stream heated to entry temperature 460-500°C in order to wash out air out of zeolite catalyst. Apparatus for implementation of described process comprises heater (6) designed to heat nitrogen and nitrogen/air streams, in series connected reactor (1), in series connected air cooler (12), and in series connected pressure gun (14). |
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Method of regenerating exhausted oil feedstock hydrofining catalyst Invention, in particular, relates to catalysts based on nickel, cobalt, molybdenum, aluminum oxides. Regeneration of exhausted catalyst is carried out through heat treatment in air atmosphere at 550-600°C for 1-1.5 h followed by: mechanical activation at energy concentration at least 6.6 W/g on vibrational mill; grinding into powder; adding at stirring a mixture containing nitric acid solution (concentration 3,5-7%), cobalt or nickel nitrate and ammonium paramolybdate; molding; drying; and calcination. |
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Method of a catalyst carrier material production of and a method of production of the catalyst The invention is dealt with the field of chemical industry. The method of production of a catalyst carrier material includes the following stages: (a) treatment of the utilized catalyst of titanium dioxide-on-silicon dioxide to clear from coke; (Ь) washing of the catalyst cleared from the coke by a flushing fluid chosen from a water solution of an inorganic acid, a water solution of an ammonium salt and their combinations; (c) drying and calcination of the catalyst washed out and cleared from the coke with production of the catalyst carrier material. The technical effect - the material produced this way is fit for use as the carrying agent material for titanium dioxide in a heterogeneous catalyst for epoxidation of olefines in alkylene oxide. |
Another patent 2551310.