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Method of destruction of carbon and nitrogen-containing raw material and device for its realisation Method of destruction of a carbon and nitrogen- containing raw material includes supply of the carbon and nitrogen-containing raw material into a cylindrical case, its heating, creation of depression inside an internal case cavity, output of gas and discharge of a sol residue. The internal case cavity is preliminarily heated before supply of the raw material into a channel of loading, the raw material, supplied constantly from the channel of is loading, is moved by means of an auger and successively directed into a chamber of initial decomposition, heating to a temperature of 120-340°C under pressure of 600-500 KPa, formed moisture and initial pyrolysis gas are output though a gas-output net into a chamber of afterburning, supplying in it oxygen in a composition of air in a dosed way until oxides CO, NO are obtained, then the raw material is subjected to destruction at first in the first zone at a temperature of 340-1000°C and pressure 600-700 KPa, and then in the second zone at a temperature of 1700°C and pressure 900-700 KPa. Depression in the zones is regulated by changing depression in tubes of a depression contour, which belong to the respective zone, oxygen in the composition of air in the case shaft is supplied through a window of a sol canal. |
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Invention relates to vacuum oil production reactor comprises shaft with bearings and housing with mechanical seal to prevent shaft oil leaks and hydraulic seal arranged on drive side between mechanical seals (1, 3) and bearings (10). Hydraulic seal comprises oil chamber and housing pressure side chamber (12) communicated with pressure line (5) via feed line (13) and lined (15) with shutoff valve arranged at chamber bottom pressure side (12) equipped with shutoff valve (16) for removal of particles contained in oil. Oil chamber (4) is controlled by safety valve (9) at overpressure of 0.05 bar. Chamber pressure side pressure (12) is controlled by shutoff valve. Note here that said pressure (12) set to exceed oil chamber overpressure (4). Besides, invention covers to sealing of said reactor. Additionally, this method consists in application hydraulic seal in combination with mechanical seal. Note also that mechanical seal comprises oil chamber, its pressure being set to ensure sufficient shaft bearings lubing while chamber pressure in direction of seal is kept at minimum level. |
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Method of steam turbine power plant operation, and device for production of steam from lignite Invention relates to the chemical industry. A device contains a drier (1) with a fluidised bed, a lignite-heated steam boiler, a steam turbine. Lignite is subjected to indirect drying in the drier (1). The dried lignite is cooled, crushed and supplied into the steam boiler. Flue gas from the steam boiler undergoes absorption purification to separate CO2. The device of flue gas purification includes an absorption column (14), a desorption column (12), a reboiler (13). Energy, required for absorption purification is partially taken from the drier (1). |
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Claimed is a method of preparing a heterogeneous phthalocyanine catalyst for oxidation of sulphur-containing compounds by an activation of non-woven lavsan by microwave radiation with a frequency of 2450 MHz, power 500-2000 W for 3-15 minutes, processing the activated material in a solution of cobalt tetra-4-[(4'-carboxy)phenylsulpfanyl]phthalocyanine with a concentration of 0.2-0.6 g/l for 2-4 hours and further stand of the material in a sodium hydroxide solution at pH 8.0-8.5 for 40-80 minutes. |
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Invention relates to rocket fuels for liquid, hard fuel and hybrid rocket engines, as well as for extreme reciprocating and turboreactive engines. As an oxidant, fuel contains ammonium dinitramide, boron or beryllium nitrates, and nitrogen pentoxide. A peculiarity of the invention consists in application of high-energy reactions and a gas-containing oxidant. Oxidant gases serve only for formation of a reaction jet. |
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Refrigeration oil and working liquid composition for refrigerator Claimed invention relates to a composition of a working liquid for a refrigerating machine, and it contains oil for refrigerating machines, containing a mixture of at least two esters, selected from a group of esters of at least one multi-atomic alcohol, and a fatty acid with content of C5-C9 fatty acid 50-100% mol, a fluoropropene refrigerant and/or trifluoroiodine methane refrigerant (versions). |
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Catalyst contains tungsten oxide, a promoter and a carrier, which includes an oxide component and a binding agent. As the promoter used is Pd or Re or their oxides. The oxide component of the carrier represents granulated zirconium and/or cerium oxide with the length of granules 2-5 mm and diameter 2-2.5 mm. As the binding agent boehmite is used. The catalyst has the following composition (wt %): tungsten oxide - 5-20; promoter - 0.1-0.5; carrier boehmite - 10-20; zirconium and/or cerium oxide - 59.5-84.9. A method of the catalyst preparation includes preparation of a granulated carrier, application of a tungsten compound on the calcined carrier, drying, addition of the promoter and calcination. The carrier is prepared from zirconium and/or cerium oxide, boehmite, with preparation of the carrier being realised by mixing a boehmite powder and zirconium and/or cerium oxide with a particle size not larger than 0.5 mm, a plasticiser - truethylene glycol, a mixture is moistened and peptised with 60-64% solution of nitric acid, mixed until a homogeneous mass is obtained, which is granulated by extrusion with obtaining 2-5 mm long granules with a diameter 2-2.5 mm. The granules are dried at a temperature of 20-110°C and calcined in an air flow at a temperature of 450-650°C for 3-5 hours. Tungsten oxide is applied on the granules in an amount of 5-20% by their impregnation with a water solution of silicotungstic acid, after which the catalysts are dried in air. |
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Invention relates to compressor oil, which contains basic petroleum oil and polymethylsiloxane, and it additionally contains 4,4'-dinonyldiphenylamine, pentaerythritol ether 3,5-di-tert-bytul-4-hydroxyphenylpropionic acid, 1,2,3-benzotriazole, ester of dialkyldithiophosphoric acid and a mixture of complex amines, and as basic oil it contains a hydrogenated residual component with content of aromatic hydrocarbons 19.0-22.0%, with the following component ratio, wt %: 4,4'-dinonyldiphenylamine 0.95-1.0; pentaerythritol ether of 3,5-di-tert-bytul-4-hydroxyphenyl propionic acid 0.55-0.65; 1,2,3-benzotriazole 0.045-0.055; ester of dialkyldithiophosphoric acid 0.055-0.065; mixture of aliphatic and aromatic amines 0.055-0.065; polymethylsiloxane 0.004-0.005; basic oil - hydrogenated residual component to 100. |
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Underground gasification of brown coal fin and mid-thickness seams Proposed method comprises drying of coal seam, injection of oxidiser into reaction channel via vertical injection well, suction gasification products therefrom via gas discharge wells and minimisation of pressure in reaction channel. Note here that, additionally, two vertical wells are drilled to coal seam surface and two vertical 100-140 m long wells are drilled at boundaries of gasified coal seam at 50-60 m from each other. Besides, injection wells are drilled at the center of section under analysis with spacing of 15-20 m. Used oxidiser is atmospheric air with addition of steam-oxygen mix in amount of 20000-50000 m3/h Combustion face temperature is kept up equal to 550-700°C Combustion face is controlled by changeover to injection well which combustion face approaches and by varying the amount of forced oxidiser. |
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Invention relates to a method of obtaining oxygenates which increase exploitation properties of fuels for internal combustion engines, in which the interaction of glycerol with acetone takes place on an acidic catalyst, with the process taking place on a heterogenic catalyst in one stage in the flow reactor with regulation of a reagent supply in a ratio glycerol:acetone (1):5-20) and support in the reactor of a temperature from 35°C to 55°C, volume rate 0.5-1.5 h-1 and atmospheric pressure, with obtaining solketal as the main product, and return of acetone that did not react into the reactor. Also described is a method of obtaining oxygenates which increase exploitation properties of fuels for the internal combustion engines, in which the interaction of glycerol with acetone takes place on an acidic catalyst, with additional application of tert-butanol in interaction of glycerol with acetone, and the process takes place on a heterogenic catalyst in one stage in the flow reactor with regulation of a reagent supply in a ratio glycerol:tert-butanol:acetone (1):(3-5):(5-20) and support in the reactor of a temperature from 35°C to 55°C, volume rate 0.5-1.5 h-1 and atmospheric pressure, with obtaining solketal and tert-butyl ether of solketal as the main products, and return of acetone and tert-butanol that did not react into the reactor. |
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Fuel oil deasphaltising method Invention refers to oil processing industry. Invention is related to fuel oil deasphaltising method by contact of wide-pore adsorbent saturated with fuel oil with cracking catalyst. The method is implemented in a rotary drum-type furnace at temperature of 200-250°C, time of contact is 5-15 minutes at weigh ratio of the adsorbent and cracking catalyst equal to 1.0:(1.4-4.0) with further particles division of the adsorbent and cracking catalyst and then by catalytic cracking of the asphalt-free oil contained in pores of the cracking catalyst. |
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Method of combined refinery of oil fractions and polymer wastes Invention relates to the field of chemistry and can be used in oil processing in order to utilise the most widely spread polymer wastes and to obtain valuable oil refinery products. A method includes a combination of polymer wastes and oil fractions, introduction of the obtained mixture directly into a reactor and realisation of cracking at a higher temperature and atmospheric pressure, as oil fractions used is a vacuum distillate, and as the reactor - a catalytic cracking reactor, the said combination is realised by dissolution of polymer wastes, taken in a quantity of 1-7 wt % relative to the initial raw material, in oil fractions at a temperature, ensuring complete dissolution in them of polymer wastes, cracking is performed at a temperature of 475-525°C with the weight rate of the raw material supply 1.8-7.0 h-1 in the presence of a zeolite-containing catalyst of Y type, containing rare earth metals as exchange cations. |
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Hydrogen sulphide neutraliser and method for use thereof Invention relates to a hydrogen sulphide and light mercaptan neutraliser which contains, wt %: nitrogen-containing organic base and/or alkali metal hydroxide 0.05-15, paraformaldehyde 1-45 and formalin-methanol mixture - the balance. The invention also relates to a method of purifying oil, gas condensate and fractions thereof from hydrogen sulphide and light mercaptans. |
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Invention relates to a lubricant composition containing polysiloxane liquid, petroleum oil MS-14, ceresin 80, lithium soap of stearic or 12-oxystearic acid, wherein the composition further contains a biocide based on 2-octyl-3(2H)-isothiazolone, with the following content of components, wt %: polysiloxane liquid 56-59; ceresin 80 16-20; lithium soap of stearic or 12-oxystearic acid 5.5; biocide based on 2-octyl-3(2H)-isothiazolone 1.0; petroleum oil - the balance. |
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Deposit reduction in gasoline fractionation, water cooling system and product recovery section Invention relates to a method of selecting a solvent or mixture of solvents useful for reducing deposit formation, cleaning existing deposits, and/or decreasing the rate of deposit formation. The invention relates to a method of dispersing contaminants in a liquid hydrocarbon stream, wherein the method includes steps of determining the nature of contaminants in the liquid hydrocarbon stream by measuring flow rate of the liquid hydrocarbon and estimating the ratio of hydrogen to carbon in the liquid hydrocarbon stream based on the measured value; selecting a solvent or a mixture of solvents suitable to disperse the contaminants based on the determined nature, wherein the ratio of hydrogen to carbon in the selected solvent or mixture of solvents is less than the estimated ratio of hydrogen to carbon in the liquid hydrocarbon stream; and contacting the contaminants with the selected solvent or mixture of solvents. |
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Methods of producing jet fuel from natural oil as feedstock through metathesis reactions Invention relates to methods of producing jet fuel, characterised by reaction between feedstock containing natural oil and light olefin in the presence of a metathesis catalyst under conditions sufficient to form a metathesis reaction product. The metathesis reaction product is hydrogenated in conditions sufficient to form jet fuel. The methods may also include separating water and isomerising the jet fuel. |
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Invention relates to catalytic conversion of biorenewable material. The method for fluid catalytic cracking (FCC) of material containing at least one source of biorenewable material comprises the following steps: contacting material containing at least one hydrocarbon fraction and at least one source of biorenewable material with a cracking catalyst in FCC conditions, where said catalyst contains zeolite, having catalytic cracking activity, a matrix and at least 1% rare-earth metal oxide per total weight of the catalyst, wherein said catalyst is characterised by the ratio of zeolite surface area to matrix surface area of at least 2. |
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Invention relates to the complex bactericidal additive containing quaternary ammonium salts, polyhexamethylene guanidine and the solvent, at that as the solvent it comprises aqueous solution of ethyl alcohol and glycerol. Use of the complex bactericidal additive in small doses increases the efficiency of antibacterial treatment of aqueous solutions and surfaces in contact with oil products while production, storage and exploitation of petroleum products. |
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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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Preparation procedure for thermal conversion of heavy hydrocarbon stock Invention is referred to the preparation procedure of a heavy hydrocarbon stock for thermal conversion that includes preheating and mixing of the heavy hydrocarbon stock with a circulating part (recycle) of a gas dehydrocyclodimerisation product formed in result of thermal conversion, pretreated from hydrogen sulphide and potentially mixed with hydrocarbon gases, preferably containing hydrocarbons C3-C4. The recycle is obtained by means of the dehydrocyclodimerisation product cooling and its separation into gas and a liquid product, separation of the separated gas into balance and recycle parts, the latter is mixed up with the liquid product of separation. The balance part of the separated gas is used as a fuel for auxiliaries. |
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Invention describes an ignition device containing a combustible body made of a mixture including paraffin, or stearine, or wax as a combustible, which has the shape of a cylinder with a cone on one end face, along the axis of which a wick is partially buried; there is a coating on the surface of the ignition device. In addition, the mixture contains dry sawdust, and mixture component ratio (wt %) is as follows: sawdust/paraffin or stearine, or wax is equal to 1/(9-10); besides, the coating of side surface of the cylindrical part of the combustible body is made from paper. |
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Invention relates to a supercritical separator equipped with a heater of an extract phase and a waste heat exchanger. A hydrocyclone device is installed as a separator. It is connected to a three-sectional vertical column unit containing an upper heat recovery section as a waste heat exchanger, a middle thermoseparation section, a lower thermoseparation section as a heater of an extract phase, and an isothermal separation zone located between the middle and the lower thermoseparation sections and equipped with a distribution device adjacent to the lower thermoseparation section. With that, the middle thermoseparation section is separated from the heat recovery section by means of a semi-blind partition equipped with an axial pipeline located in intertubular space of the heat recovery section. The latter consists of an assembly of heat exchange elements located in annular space formed with the housing of the section and the axial pipeline equipped with extract inlet lines and lines for supply of heated extract to the hydrocyclone device, as well as it includes a regenerated solvent outlet line. The middle and the lower thermoseparation sections consist of assemblies of heat-mass-exchange elements equipped with heat carrier inlet/outlet lines, and the lower thermoseparation section is additionally equipped with an extract phase outlet line enriched with an extracted substance; besides, the hydrocyclone device is equipped with lines for supply of solvent and extract phase to the isothermal separation zone. |
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Refractory furnace doors, and refractory walls enveloping furnace doors; batteries of coke furnaces Invention relates to a locking device of a refractory door closing coke furnaces with a horizontal chamber and to a coke furnace closing and sealing method. The above device is made from refractory material; with that, material containing silicon oxide or that containing silicon and aluminium oxides is used. The door device consists of a coke furnace chamber wall enveloping the door that is essentially located above the door and a moving door located below and made in the form of a plug. Therefore, less cold air from outside environment enters the coke furnace chamber during the loading process, and heat loss is minimised. The door can contain ellipsoidal projections, due to which coal can be easier loaded to the coking chamber. The coke furnace chamber wall enveloping the furnace door is made from the same material as the coke furnace chamber door. Coking mass is located in the coke furnace chamber so that the lower end of the part of the coke furnace chamber wall, which is located above the coke furnace chamber door, is located above the upper end of the coking mass. |
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Multitubular device for coal decomposition with external heating Invention can be used for coal processing to high-quality fuel. Proposed device comprises airtight furnace body (1) with channel (4) for coal displacement and decomposition. Said channel (4) has coal inlet (2), coal outlet (3) and coal decomposition gas collector tube (14). Said channel (4) is connected with auxiliary rotary device (6) arranged outside the furnace body (1). Heat transfer chamber (5) is composed between said channel (4) and furnace body (1) inner wall. Note also that this chamber is collected with high-temperature gas heating device and comprises heated gas outlet (12) for preheating of material via tubes. Aforesaid channel (4) is composed of multiple closely located parallel pipes. One end of the channel comprises feed compartment (11) for communication with coal inlet (2) while opposite end comprises discharge compartment (13) for communication with coal discharge opening (3). |
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Gasification of carbon-bearing solid fuels Invention relates to gasification of solid carbon-bearing combustibles, i.e. lignite and coal, shale oil and peat. Gasification comprises heating and pyrolysis of solid carbon fuel fed into bath with fused melt of sealed electrode kiln at forcing gasifying agents through fused slag with solid carbon fuel. Besides, electric current is passed by electric circuit including electrodes fed into kiln bath and kiln hearth. Synthesis gas, slag and metal alloy is removed from kiln working space. Three-phase current if fed through fused slag with solid carbon fuel, current magnitude being defined in compliance with solid fuel consumption and required power defined by relationship: P a = G × w p 3 6 0 0 , M W , where G is solid fuel consumption, kg/h, wp is specific power consumption. |
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Invention can be used in the chemical industry, in particular for obtaining producer gas. Cocurrent gasifier contains a fuel tank (14) for storing fuel to be gasified, an upper ceiling (16a), forming the bottom of a fuel bunker, one gasification tank (20) for fuel gasification, located under the upper ceiling and means for passing gasifying air into a gasification tank. The upper ceiling contains several holes (30) for supply of fuel from the fuel bunker into the gasification tank. Under the upper ceiling (16a) there is a lower ceiling (16b). The gasification tank (20) is placed under the lower ceiling (16b). There are several concentric holes (30) passing from the fuel bunker (14) into the said gasification tank. |
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Method of vegetable oil re-etherification Method of a vegetable oil re-etherification includes introduction in a reactor heated up to 60°C of a vegetable oil, methyl alcohol in molar ratio 1:6, potassium hydroxide, taken in a quantity 1-3% of the oil volume, with the following mixing of a reaction mass. Mixing of the reaction mass is realised in a vortex device by interaction of two vortex streams, which move along the axis of the device towards each other. |
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Circulating fluidised bed reactor with improved circulation Invention is related to a circulating fluidised bed reactor. The fluid coking reactor includes a soaking section with a dense bed representing a circle in horizontal section in regard to the vertical axis limited by the reactor wall where heavy oil is subject to thermal cracking, the basis area to which fluidising gas is introduced in order to fluidise a layer of fine solid coke particles in the soaking section, a variety of inlet rings for heavy oil places along perimeter of the reactor wall in the soaking section and at different height over the basis area, the upper are where gas and fine solid coke particles are outputted from the soaking section, a variety of partitions of truncated cone shape placed at different height in the soaking section with the dense bed above the reactor basis area, at that each partition is placed between a successive pair of heavy oil inlet rings and is turned away from its upper edge near the reactor wall passing downwards and radially inwards from the reactor wall up to the lower inner edge defining its central opening. |
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Method of obtaining hydrogen and hydrogen-methane mixture Invention can be used in the chemical industry. A method of obtaining a hydrogen-methane mixture includes application of two parallel flows, which contain lower alkanes, as a source of raw material. The first flow is directed to partial oxidation with oxygen containing gas. Products of the first flow oxidation are supplied to cooling by means of the second flow heating, and after that, to catalytic conversion of carbon monoxide. After that, hydrogen is separated from the first flow. The second flow is mixed with water vapour and successively passed through a series of successive stages, each of which includes heating in a heat exchanger due to discharge of heat from the process of the partial first flow oxidation, and then through an adiabatic conversion reactor, filled with a catalyst filling. Products of the second flow conversion after separation of water vapour are mixed due to ejection with hydrogen, discharged from the first flow. |
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Gating of dust accumulating at dust trap plant for rough gas Accumulated gas gating from gasification process at pressure with the use of gas trap and gate bin should allow getting of nitrogen in rough gas to be minimised or completely ruled out. Note here that subsequent chemical synthesis should be, from the very outset, free of nitrogen admixtures. This method effects this by filter elements arranged in said dust trap and subjected to back purging with gas, other than air, containing gas carbon dioxide or pure carbon dioxide gas. Carbon dioxide containing gas for back purging is used in gating bin for pressure increase and dust loosening. |
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Production of isotropic pitch semi-coke Invention can be used in production of carbon materials used in nuclear power engineering, aircraft and space engineering, machine building. Proposed method for production of isotropic pitch semi-coke from initial cone with softening point of up to 100°C comprises carbonisation of said initial coke. Prior to carbonisation, initial coke is subjected to heat treatment in the presence of condensing additive and air. Heat treatment is conducted in reactor by heating said initial coke to 300-400°C. Carbonisation is performed by gradual coke heating to not over 750°C at rarefaction in reactor of 5-10 mm of water column. Carbonisation off-gases are trapped and decontaminated by mixing with mineral acids or its vapours. |
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Plant for feed thermal treatment and coke cooling Invention can be used in coke-chemical industry. The plant for feed thermal treatment and coke cooling consists of a heat exchange chamber (1), coke bunkers (2) and coal charge bunkers (3), a separator (4) installed at output of the heat exchange chamber (1) and intended for separation of coke and feed. The heat exchange chamber is equipped with water-cooled and heat-removal panels (5, 6). In cavity of the chamber (1) there are elements outputting steam generated during feed heating. Each steam removal element is made as a groove (7) passing through the chamber (1) cavity and communicating with its inner cavity. The steam removal elements are placed at several levels in height of the heat exchange chamber (1), one above another. The heat exchange chamber (1) is equipped with a vertical central channel (8) communicating with its inner cavity and the steam removal elements. The central channel (8) is outputted outside the upper part of the chamber (1). |
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Group of inventions may be used in the field of condensed and solid fuel processing to generate power. The method for production of pyrolysis resin-free combustible gas during gasification of condensed fuel includes fuel delivery through a loading unit (1) installed in the upper part of the gas generator and loading of a solid incombustible material through a separate loading unit (4) which ensures material staying in the counter-flow of gaseous products. Oxygen-containing gas is delivered to the lower part of the gas generator, pyrolysis and fuel combustion in the gas counter-flow are made. Solid residue is unloaded from the lower part of the gas generator. Gaseous products from the upper part of the gas generator are outputted from a layer of the solid incombustible material not mixed with the fuel. Gaseous products form in result of pyrolysis and drying are separated from the fuel layer and fed to the combustible area (9) placed below the area where fuel and solid incombustible material are mixed (8). The used gas generators are represented by multiple-bedded furnaces, a shaft reactor, and a rotating drum. |
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Methods and device for raw material mixing in reactor Invention relates to gasification systems and can be used in chemical reactors and pipeline systems for raw material injection. Injection system for raw material feed contains several ring channels 314, 316, 318 arranged in concentric configuration around longitudinal axis, and several helical elements 312 passing into path for fluid flow. The helical elements 312 are made with possibility to move axially in ring channel. At least one helical element 312 contains several blades placed along helical path and spaced from each other. In this structure, one of helical elements 312 is made capable to impart the first circular rotation to fluid flow, and the other helical element 312 is made capable to impart counterflow circular rotation. |
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Complex for natural gas supply to consumer Invention relates to supply of natural gas to consumer at its conversion into gas hydrate. Gas conversion means comprises reactor connected with gas and water sources, means to cool the mix of water and gas, means to maintain reactor pressure not lower than equilibrium pressure required for hydrate formation and means to discharge gas hydrate into carrier. The latter should have cargo compartments that can maintain thermodynamic equilibrium to rule out gas hydrate dissociation and means to decompose gas hydrate for gas production. Complex reactor can form gas hydrate pulp and is composed by the tank designed to sustain pressure over 1 MPa and to keep up temperature at the level of 0.2°C. For this, means to cool the mix of gas and water comprises the vacuum ice generator. The latter is composed of heat-insulated tank communicated with sea water source and vacuum outlet of turbocompressor. Note here that ice generator outlet is connected with separator of ice from brine, separator ice outlet being connected with ice mixer and sweet water. Note here that natural gas source is connected with reactor gas inlet and ice generator turbocompressor gas turbine. Reactor second inlet is connected via ice-bearing pulp duct with ice-bearing pulp accumulator composed of heat-insulated tank. Note here reactor hydrate outlet is connected via first pulp duct with hydrate-bearing pulp accumulator. Reactor water outlet is connected with ice mixer and sweet water. Note also that said outlet of ice mixer and sweet water is connected via second ice-bearing pulp duct with ice-bearing pulp accumulator inlet. Besides, gas hydrate discharge means comprise pulp pump and gate arranged at ice-bearing pulp accumulator discharge pipe to be connected with carrier cargo compartment intake pipe. Note also that carrier cargo compartment can be connected with discharge compressor intake pipe, discharge compressor outlet is connected with gas-holder. |
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Invention relates to a method of preparing fuel gas, which involves compression using a liquid-ring compressor, separating the compression product to obtain a gas and a liquid, membrane separation of the separation gas into a stripped gas and a recycled low-pressure unstripped gas, wherein before compression, raw gas is subjected to heating, catalytic dehydrocyclodimerisation and cooling; the working fluid used is prepared oil, and membrane separation of the separation gas further includes separation of a hydrogen-rich gas, which is then mixed with air and subjected to catalytic oxidation to obtain an oxidation gas, which is used as a heat carrier for maintaining temperature of catalytic dehydrocyclodimerisation. |
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Method of producing non-carcinogenic aromatic process oil Invention relates to a method of producing non-carcinogenic aromatic process oil containing less than 3.0% of an extract of polycyclic aromatic hydrocarbons according to the IP-346 method, which involves purifying petroleum oil fractions with selective solvents and separating the extract of selective purification of the oil, further treatment of the extract with a polar solvent and obtaining a raffinate as the desired product. The polar solvent used is propylene carbonate which is used to treat the raw material, wherein the raw material is a mixture of the extract from selective purification of oil obtained at the oil fraction purification step and a recycling raffinate solution obtained at the further treatment step; the raffinate solution obtained from further treatment is partially fed for mixing with the extract from selective purification of oil; the balance amount of the raffinate solution is fed to a step for regenerating solvent from the raffinate solution, and the extract solution obtained at the further treatment step is fed to a step for regenerating solvent from the extract solution. The ratio of the raw material to the polar solvent at the further treatment step is in the range of (0.67-0.2):1; temperature at the top of the extractor is in the range of 100-210°C and temperature at the bottom of the extractor is in the range of 85-200°C. |
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Electronic musical keyboard instrument "maxbox" Electronic musical keyboard instrument includes a system of interconnected sound-extraction units, wherein each unit is designed to generate one fundamental audio frequency and is matched on that frequency with audio frequencies generated by other units, wherein the number of sound-extraction units, the principle of their matching on generated audio frequencies, the labelling of sound-extraction units on the instrument and spatial arrangement thereof are defined by a multi-step musical pitch, formed from a discrete set of monochromatic sounds, the instrument being characterised by that the system of sound-extraction units consists of independent keyboards with control units and is configured to use an octave with the step 2, 3, 4, 5, 6, 7, 8, 9, 10, wherein the number of tones in an octave varies from 4 to 25, the structure of the octave itself has the capacity for a combinational set of a series of non-uniform tones: tone, 1/2, 1/3, 1/4, 1/5, 1/6, 1/7, 1/8, 1/9 and 1/10 tone, wherein the keyboard are arranged in two levels. |
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Production of base oil for lubricants Invention relates to production of bas oil for lubricants. Base oil for lubricants is produced at first stage whereat stock oil containing normal paraffins C20 or higher is subjected to isomerisation so that content of normal paraffins C20 or higher makes 6-20 wt % of total mass of hydrocarbons C20 or higher in produced reaction product. Lubing oil fraction including hydrocarbons C20 or higher is separated at second stage from first stage reaction products. Lubing oil fraction produced at second stage is separated at third stage to dewaxed oil and paraffin by dewaxing by solvent. Note here that dewaxed oil is used as base oil or subjected to purification by solvent and/or to hydrofining to produce base oil for lubricants. |
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Methods of hydrocracking with receiving of hydroisomerised product for base lube oils Invention is related to hydrocracking processes, under conditions of which large proportion of heavy hydrocarbon stock e.g. Vacuum Gas Oil (VGO) turns to hydrocarbons with lower molecular mass and lower boiling temperature. The invention relates to the method of production of base oil, involving: a) hydrocracking of heavy hydrocarbon stock with hydrocracking catalyst containing the preset amount less than 15 wt % of beta-zeolite with flow coming out of a hydrocracking plant containing at least 40 wt % of hydrocarbons boiling at temperature of 382°C (720°F), and b) separation from flow coming out of a hydrocracking plant of unconverted oil with pour point not above 18°C (65°F) in form of high-boiling fraction containing base oil. |
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Invention relates to production of fuel briquettes to be used in power engineering. In compliance with proposed method, initial stock is minced to grain size not over half the stroke of male die and conveyed to batcher. Then, minced material is fed to press stage for it to be formed. Note here that in mincing maximum fraction size is made equal to or smaller than the length of opening formed between male die and conveyor walls. Press stage is arranged in detachable conveyor. Packing is performed along with briquette forming in container layer-by-layer. Then, container is closed by cover. |
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Installation for production of fuel mixtures Installation comprises the sources of oil product and water, steam generator, pumps, steam lines, pipelines, water and oil product heaters, rotary machine, holding tank, oil product processing circuits, the system of preparing the metered components, the system of steam distribution, the system of drainage steaming and cleaning the equipment. The first circuit of oil product processing comprises a starting pump which inlet is in communication with a source of oil product and the outlet - with the inlet of the unit of rough cleaning. The outlet of the unit of rough cleaning is in communication with the inlet of the first pre-heaters of the cascade of the pre-heaters of oil product. The outlet of the last pre-heater is in communication with the intermediate damping capacity. The second circuit of oil product processing comprises a finishing pump which inlet is in communication with the first outlet of the intermediate damping capacity, and the outlet is in communication with the inlet of the first unit of fine cleaning. The second circuit of oil product processing comprises a preliminary mixer which outlet through the second unit of fine cleaning is in communication with the inlet of the rotary device. The system of preparing the metered components comprises a unit of oil product metering which inlet is in communication with the outlet of the first unit of fine cleaning and is equipped with a water pre-heater which inlet through the shut-off valve is in communication with a source of water, and the outlet through the unit of water metering is in communication with the inlet of the water pump, which outlet is in communication with the inlet of the third unit of fine cleaning. The outlet of the third unit of fine cleaning and the outlet of the unit of oil product metering are in communication with the inlet of the preliminary mixer. The steam generator is in communication with the heat transfer elements of the filters of rough and fine cleaning, the pre-heater and the water pre-heater. The cavities of filters of units of rough cleaning and the first and second units of fine cleaning, the pre-heater, the water pre-heater and the rotary machine with the modulation of flow are in communication with the steam generator. |
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Technology and device for obtaining synthesis gas from biomass by pyrolysis To obtain synthesis-gas from biomass performed is preliminary processing of biomass, including biomass crushing until particles with size 1-6 mm are obtained and drying raw material to moisture 10-20 wt %. After that, pyrolysis of biomass is carried out by means of fast pyrolysis technology, with temperature of pyrolysis layer being 400-600°C, and time of location of gaseous phase on pyrolysis layer being 0.5-5 s. Product of pyrolysis layer is pyrolysis gas and coal powder. Pyrolysis gas is separated from coal powder and solid heat carrier by means of cyclone separator. After that, coal powder and solid heat carrier are separated in separator to separate solid phases, coal powder is charged into coal powder bin for accumulation, solid heat carrier is heated in chamber of boiling layer heating and solid heat carrier is supplied to pyrolysis layer for re-use. After that, pyrolysis gas is supplied to condensate accumulator to condense aerosol and condensation of condensable part of pyrolysis gas is carried out to form bio-oil, after that formed bio-oil is pumped by high pressure oil pump and supplied to gasification furnace for gasification. One part of non-condensed pyrolysis gas is supplied on combustion layer for combustion with air, and the other part of non-condensed pyrolysis gas is supplied on pyrolysis layer as fluidising medium. |
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Device for influencing flow in coal gasification reactor connection pipe/gas cooler Invention relates to chemical industry and can be used for production of synthesis gas by coal gasification. Proposed device comprises horizontal connection pipe (1) arranged between coal gasification reactor and gas cooler/cleaner. Pipe (1) incorporates Venturi device to control the flow by cone (4a) arranged at the centre of pusher bar (4). Said pusher bar (4) is driven by leverage (4b) composed by lever arm extending through plugged pipe and lever arm extending from plugged pipe (8) via gland (6). |
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Coal thermal benefication and device to this end Invention relates to chemical industry and can be used for production of high-energy solid fuel from coal. Device consists of two communicated chambers. First chamber consists of coal feeder (1), fire grate (2) to remove separated ore, device to feed blow air (3) at the temperature not over 400°C and to add flue gas to 100%, waste gas removal system (4) and coal layer transfer pipe (5). Second chamber consists of the device (6) of initial blowing at the temperature not higher than 400°C, device (7) of secondary blowing to afterburning of combustible components for coal thermal decomposition and coke gasification at 600÷1000°C, heat energy recovery system (8), flue gas removal system (9) and coke discharge pipe (10). |
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Method of obtaining high-octane base gasoline Invention deals with two-stage method of obtaining high-octane base gasoline with application of liquid and gaseous hydrocarbon raw material in presence of catalyst, and circulation of nonconverted raw material and hydrocarbon gases. As liquid hydrocarbon raw material used is oil or gas condensate, or their mixture; as gaseous hydrocarbon raw material used is C1-C4 fraction and/or C3-C4 fraction and circulating hydrocarbon gases; liquid hydrocarbon raw material is subjected to fractioning in fractionation column with removal of straight-run fractions with limits of evaporation within the temperature interval C5-75°C, benzene fraction with limits of evaporation within the temperature interval 75-85°C, fraction 85-(160-220)°C and circulating hydrocarbon gases; fraction with limits of evaporation within temperature interval C5-75°C and 85-(160-220)°C are supplied to first stage of contact with zeolite-containing catalyst or system of catalysts, promoted with metals of I-VIII group of Periodic table, benzene fraction with limits of evaporation within the temperature interval 75-85°C is removed from fractionation products. Gaseous hydrocarbon raw material is supplied to second stage of contact; it contacts with zeolite-containing catalyst or system of catalysts, promoted with metals of I-VIII group of Periodic table, and contact in first and second stages takes place with the course of main reactions - isomerisation, aromatisation and hydration, products of contact of first and second stages together undergo stabilisation and fractionation with separation of target product - high-octane base gasoline, evaporating within temperature interval C5-(160-220°C), residue higher than (160-220°C), non-converted raw material, which circulates in first stage raw material, and hydrocarbon gases, which circulate in second stage raw material. |
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Zeolite-containing catalyst or oil fraction dewaxing Zeolite-containing catalyst is proposed based on high-silica zeolite, which includes hydrogenating components and additives with the following components ratios, wt %: zeolite 50.0-70.0; MoO3 4.0-5.0; ZnO 1.0-3.0; P2O5 1.0-2.0; B2O3 1.0-3.0; γAl2O3 - the other are up to 100. At that, zeolite of ZSM-5 structural type is used as a base, having: crystallinity degree 95-100%; crystallite size 5-30 mcm; static capacity by heptane 0.18-0.21 cm3/g; silica module 30.0-55.0. |
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Method of biomass thermal treatment with help of boiler plant Invention relates to thermal treatment of biomass. Particularly, it relates to the process including feed of biomass (6) into reactor (16). Biomass (6) is heated in said reactor to 180-350°C at low oxygen concentration. Here, components are produced that feature inertia relative to biological decomposition with formation of gaseous reaction products (10) and heat-treated biomass (8). Reaction gaseous products (10) are fed for combustion (13) while hot flue gases (11) of said combustion (13) are fed into reactor (16) for thermal treatment process. Combustion process (13) is executed in boiler (14) that combusts extra fuel (15) in amount not over 20%, preferably, not over 10% of the fuel energy equivalent are obtained from reaction gaseous products (10) in reactor (16). Biomass is heat treated in continuous action reactor 16 while flue gas flow flows in the same direction with biomass flow in reactor (16). |
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Invention is related to a combined method of conversion of oil-derived hydrocarbon fractions into high-quality hydrocarbon mixtures as fuel, which includes catalytic cracking of hydrocarbon fraction in catalyst fluidised bed with catalyst containing ERS-10 zeolite, where the specified catalyst contains at least two components, where the specified components represent: (a) a component containing one or more catalytic cracking catalysts in fluidised, and (b) a component containing ERS-10 zeolite for obtaining Light Cycle Gas Oil (LCGO), hydrotreatment of light cycle gas oil, interaction of hydrotreated light cycle gas oil obtained at the previous stage of hydrotreatment in presence of hydrogen with catalytic system. The invention also touches the method of catalytic cracking and a stage of catalytic cracking in fluidised bed. |
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Raw hydrocarbon hydroconversion method Invention relates to the hydroconversion method for raw hydrocarbons in the mix with the circulating part of the hydroconversion vacuum residue by a high-aromatic modifier, dispersion of a catalyst precursor and hydrogen-containing gas which is supplied in the amount of maximum 800 nm3 per 1 m3 of raw material in terms of hydrogen and of minimum the value of chemical hydrogen demand. The above is carried out in a reactor with an internal circular baffle plate which adjoins the reactor top in a pressure tight way and forms axial and circular cavities, and with separation space at the top of the circular cavity. Hydroconversion gas is removed from the separation space, liquid hydroconversion product is removed from the top of the axial cavity, circulating reaction mass is removed from the bottom of the reactor's circular cavity, cooled and delivered for mixing with heated raw liquid-vapour mixture, the temperature of the liquid hydroconversion product is kept close to the upper limit of the hydroconversion temperature range, the temperature of the heated raw mixture and the temperature of the circulating reaction mass are kept close to the lower limit of the hydroconversion temperature range. Hydroconversion products are separated and rectified to isolate light fractions, heavy gas oil and vacuum residue, part of the latter is recirculated, and the balance part is recovered to produce regenerated catalyst precursor. |
Another patent 2513073.