Process for thermal removal of coke from zeolite catalyst and apparatus |
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IPC classes for russian patent Process for thermal removal of coke from zeolite catalyst and apparatus (RU 2319544):
  
 Contact structures / 2318590
The invention is pertaining to the field of the reaction contact structures used in the reactors of the paraffin alkylation in the capacity of the internal static head of the system, such as the disperser. The system for commixing contains the vertical reactor for implementation of the catalytic reactions of stirring and the disperser, which is located in the reaction zone. The disperser is made in the form of the net spliced with the multiple-core component, or in the form of the stretching or rolled out metal interlaced together with the multiple-core component. At that the multi-core thread is selected out of the inert polymers, the catalytic polymers, the catalytic metals or out of their mixtures. The wire net ensures the structural integrity of the system, and also at least 50 volumetric % of the open-space in the reactors required for motion of the vapors and fluids through the system. The disperser can be made in the form of the sheets, bundles or the packets, or to be arranged inside the frame. The present invention allows to exercise more effectively the alkylation of the paraffin at the expense of the large degree of the contact between the liquid catalyst and the reactants in the form of the fluid mediums without the mechanical stirring, thereby eliminating the necessity of sealing of the drive gears and reduction of the product cost.
 Method of production of the non-saturated halogen-containing hydrocarbons and the device for the methods realization / 2316533
The invention is pertaining to the method of production of the ethylene non-saturated halogen-containing aliphatic hydrocarbons by the thermal fission of the saturated halogen-containing aliphatic hydrocarbons. The initial gas stream introduce into the reactor having, at least, one entering in its internal part feeding line, through which the heated gas formed from the fission promoters and containing the radicals comes into the reactor. The invention is also pertaining to the reactor used for realization of the method. At that generation of the radicals is exercised outside the reactor. The technical result of the invention is the increased output of the fission reaction.
 Module-type horizontal multideck catalytic reactor for high-heat chemical synthesis processes / 2312704
Module-type horizontal multideck catalytic reactor for high-heat hydrocarbon, alcohol, and ester synthesis processes comprises a set of cylindrical catalyst baskets with solid catalyst placed on grates-shelves thereof. Reactor further comprises a set of modular heat-exchange apparatuses, each of them being connected through reaction gas conduits to outlet of upstream basket and inlet of downstream basket. Each basket has its own supporting plate and high-pressure case and, together with heat-exchange apparatus and gas conduit between them, represents a reactor module. Reaction gases enter basket and heat-exchange apparatus from below.
 Method of conducting of the chemical reaction in the pseudo-isothermal conditions and the heat exchanger for the method realization / 2310502
The invention is pertaining to the method of the continuous conducting of the certain chemical reaction in the so-called pseudo-isothermal conditions, notably in the conditions, in which with the help of adjusting, the temperature of the reaction is maintained at the level of the previously preset optimal temperature with the small deviations from it. The invention provides, that the method of the continuous conducting of the chemical reaction in pseudo-isothermal conditions is conducted in the reaction medium, for example, in the catalyst layer, in which, at least, one heat exchanger is located, in which feed the first flow of the working heat-carrier with the preset temperature at the inlet with gating this flow from the inlet to the outlet. At least, into one heat exchanger through, at least, one dispenser in one or several via points along the path of motion of the working heat-carrier feed the second flow of the working heat-carrier for the temperature monitoring in the reaction medium. The invention also presents the heat exchanger for realization of the chemical reaction, which has two large walls (21, 22), the chamber located between the walls (21, 22), through which the working heat carrier is gating, the inlet fitting pipe (24) and the outlet fitting pipe (25) accordingly used for feeding and withdrawal of the working heat carrier from the chamber, at least one or two dispensers (30, 31) of the working heat carrier fixed, at least, on one or two walls (21, 22) with some spacing interval from the fitting pipes (24, 25) and communicating with the chamber, and, at least, the channel (28) for feeding of the working heat carrier, at least, in one of the dispensers (30, 31). The invention allows to maintain at the constant level of the preset temperature of the chemical reaction or to adjust it in the very narrow range of the values for more full completion of the chemical reaction.
 Catalytic apparatus / 2306172
The invention is pertaining to the catalytic devices used for purification of the technological and ventilation gases from the vapors of the organic substances and may be used in many branches of industry. The catalytic apparatus contains: the body made in the form of the spiral two-channel heat exchanger-recuperator, which spirals are fulfilled from the semi-cylindrical shells, the gases inlet and outlet fitting pipes, the catalytic and the electrically heated sections arranged in the inside concavity of the heat exchanger-recuperator. The spirals of the heat exchanger-recuperator contain the plane sections connecting the semi-cylindrical shells. At that the spiral of the inlet channel is connected to the electrically heating section, and the spiral of the outlet channel is connected to the catalytic section divided into parts. On the coils of the spiral channels of the heat exchanger-recuperator there are the mounted unions used for feeding the vapors of the organic substances - the production waste products, for feeding of the washing liquor, for feeding of the compressed air to cool the apparatus, for sampling the probes. The invention ensures protection of the catalytical apparatus against pollution, reduction of the power inputs, the improved conditions of the maintenance of the spirals of the heat exchanger-recuperator.
 Reactor for synthesis of the aromatic hydrocarbons / 2305594
The invention is pertaining to the field of the processes and the apparatuses of the chemical technology and may be used in the processes of conversion of the light hydrocarbon into the aromatic hydrocarbons. The reactor includes the body, the cover and the bottom, the unions for inlet of the initial gaseous mixture and the outlet of the target product, the gas-permeable horizontal partition, on which there is the immovable bed of the granular particles of the catalytic agent. Inside the reactor with a clearance to the main body the additional internal wall is installed, which has been made out of the sheet metal plate, the upper part of which is connected to the main body, and the lower part of which is connected with the gas-permeable horizontal partition. On the inlet union there is the mounted distributing device consisting of the inlet annular channel, the central axially symmetric outlet channel, several fitting pipes connecting the indicated channels and arranged tangentially to the indicated outlet channel, and the rod baffle. The invention ensures the homogeneous stirring of the two-phase flow at the inlet of the reactor and the flow uniform distribution on the catalyst bed, reduction of the heat losses through the walls of the reactor and feeding of the additional heat into the lower part of the catalyst bed.
 Reactor for the catalytic production of the petrol and the diesel fuel / 2305593
The invention is pertaining to the processes and apparatuses of the chemical technology and may be used in the catalytic process of production of the petrol and diesel fuel out of the hydrocarbon raw. The reactor includes the body, the cover and the bottom, the unions for the inlet of the initial gas-liquid mixture and the outlet of the target product, the gas-permeable horizontal partition, on which there is the fixed bed of the granular particles of the catalytic agent. Inside the reactor with the clearance to the main body there is the additional internal wall made out of the sheet metal plate, the upper part of which is connected to the main body, and its lower part - with the gas-liquid-permeable horizontal partition. On the inlet union there is the distributing device consisting of the inlet channel of the annular form, the central axially symmetric outlet channel, several fitting pipes connecting the indicated channels arranged tangentially to the indicated outlet channel and the rod baffle. The invention ensures the homogeneous stirring of the two-phase flow at the inlet of the reactor and the flow uniform distribution on the catalyst bed, reduction of the heat losses through the walls of the reactor and feeding of the additional heat into the lower part of the catalyst bed.
 Chemical reactor / 2302287
Chemical reactor comprises nozzle that is made of a stack of interconnected metallic plates. The nozzle receives a number of reaction zones and a number of catalytic zones. The plates have the first channel structure for transporting the first reagent between the reaction zones. The parts of the first channel structure connect the reaction zones and represent heat exchange passages at least in a part of their length. The second channel structure is provided in other plates and is used for supplying the second reagent to each reaction zone. The third channel structure is used for transporting the third reagent to the space between the zones provided with catalyzer.
 Reactor for realization of the non-adiabatic reactions / 2299093
The invention is pertaining to the field of chemical industry, in particular, to the reactor for realization of the non-adiabatic reactions. The reactor consists of the metallic ingot and contains, at least, one reactionary passage made through the ingot and designed for maintaining the catalyst for the non-adiabatic transformation of the reactants flow. The reactor contains the inlet channels for introduction of the stream of the reactants into the reactionary passage and the outlet channels for withdrawal of the reacted stream of the reactants; and also the heating-up or cooling device intended for maintaining the catalytic non-adiabatic transformation of the torrent of the reactants. The invention provides, that the mentioned inlet and outlet channels are made in the ingot and are located mainly perpendicularly to the reactionary passages and in parallel connect the reactionary passages. The technical result of the invention is the possibility to use of the reactor for the small-scale production works.
 Heat exchanger for isothermal chemical reactors / 2298432
The invention is pertaining to the chemical industry, in particular, to the heat exchangers for the isothermal chemical reactors and presents the block heat exchanger for the radial or radial-axial isothermal reactors and has essentially the annular and cylindrical structure with the axial through hole of the definite diameter and consists of the set of the essentially rectangular solid box-shaped heat exchangers located in several having the common axis concentric areas and forming in the block-shaped heat exchanger the set of the essentially radial groups consisting of the heat exchangers laying in one radial plane and in the different annular zones, the long sides of which are passing in parallel to the axis of the block heat exchanger, and their short sides are passing in the radial direction, and each such heat exchanger has the internal cavity, through which the running coolant is passing; at least one located on one side of the heat exchanger pipe for distribution of the fed in it running coolant and at least one located on the opposite side of the heat exchanger pipe, In which the running coolant having passed through the heat exchanger is collected. The indicated pipes are connected on the one side to the heat exchanger internal cavity at least through one hole present in them, and on the other side - with the branch-pipes located outside for feeding in the heat exchanger and for withdrawal from it of the running coolant. The technical result of the invention is provision of the flow of the running coolant in the radial direction side by side with the axial direction.
Method of regenerating exhausted oil feedstock hydrofining catalyst / 2299095
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.
Method of a catalyst carrier material production of and a method of production of the catalyst / 2251451
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.
 Method for regenerating catalyst for production of isoprene from 4, 4-dimethyl-1,3-dioxane / 2235592
The invention relates to a method of regeneration of catalysts, in particular calcium phosphate, and can be used in the petrochemical industry for the production of isoprene
 Method for regenerating catalyst tsiklitiria hydrolysis of aminonitriles in the lactam and the use of the regenerated catalyst for the production of lactams / 2205690
The invention relates to a method for regenerating catalyst tsiklitiria hydrolysis of aminonitriles order to obtain lactam
The activation method of the sorbent on the basis of metal oxides / 2129463
The invention relates to the field of sorption techniques, namely the clean air mixtures of carbon monoxide and can be used for the regeneration and activation of sorbents on the basis of metal oxides
 Method of regeneration of a copper-chromium catalyst / 2071378
The invention relates to the production of higher fatty alcohols (WGS) method for the hydrogenation of fatty acids and their esters, in particular to a technology for copper-chromium catalysts from spent catalyst slurry hydrogenation process
 The way the oxidative regeneration fine cracking catalyst / 2068733
The invention relates to the refining, in particular to a method of oxidative regeneration of spent catalyst in the catalytic cracking of crude oil
Method of regenerating catalytic systems of hydrogenation processes / 2290996
Method is accomplished by burning out carbon-containing compounds in oxygen-containing gas medium and comprises stages: desorption of hydrocarbons from catalyst surface performed in plant reactor and burning out of hydrocarbon thickening products performed on a special installation in indirect-heating rotary kiln at 450-550°C and excessive pressure 0.4-1.0 bar. Desorption of hydrocarbons from catalyst surface is carried out in a hydrogen-containing gas medium with 60-80 vol % H2, while gradually raising temperature from 200-220°C to 380-400°C at a rate 35-30°C/h following by aging of catalysts at 380-400°C until concentration of hydrocarbons in hydrogen-containing gas is no higher than 0.5 wt %, after which temperature is lowered to 100-120°C at a rate 20-25°C/h and active catalyst components are passivated. Passivation is accomplished by treatment at 100-120°C and excessive pressure 4-10 bar with mixture of inert gas and oxygen-containing gas, in particular carbon dioxide and/or air used in amount providing oxygen concentration in gas mixture 0.02-0.5 vol %, which corresponds to consumption of gas mixture 400-600 nm3/m3 catalyst. Treatment is conducted until oxygen concentrations at inlet and outlet of reactor are leveled.
 Method for oxidation of alkene / 2283308
Invention proposes a method for oxidation of alkene. Method involves interaction of alkene with hydroperoxide in the presence of aluminum-free titanium-containing zeolite catalyst and the following regeneration of catalyst by a method involving thermal treatment of catalyst in the presence of hydrogen-containing gaseous flow at temperature above 120°C. Proposed method of regeneration of catalyst provides retaining mainly its initial catalytic activity and in using the stationary layer of catalyst the regeneration can be carried out without discharge of catalyst. Identical solvents can be used both for regeneration of catalyst and for carrying out the oxidation reaction and these solvents can be recirculated.
Method of regenerating aliphatic hydrocarbon dehydrocyclodemerization catalysts / 2270719
Invention relates to regeneration of silica powder-containing catalysts with SiO2/Al2O3 ratio at least 12, which are deactivated by coking occurring during aliphatic hydrocarbon dehydrocyclodemerization reaction. Regeneration process comprises preliminary nitrogen purge of reactor system to remove hydrocarbons until their content drops below 0.5%, treatment of catalyst at 300-550°C and pressure 0.1-2.0 MPa with catalyst-regeneration gas in the form of nitrogen-oxygen mixture pumped through closed regeneration circuit, withdrawal of a part of combustion products and moisture formed during coke combustion reaction, wherein regeneration gas loss is continuously recompensed to maintain specified working thermobaric conditions in the regeneration circuit. Simultaneously, oxygen content in regeneration gas is stepwise raised from 0.1 to 21 mol % followed by ageing of catalyst under each step conditions. Regeneration gas utilized is emission gases from process furnaces used to preheat feed for various chemical processes and operated with the main-pipeline natural gas, which emission gases are processed in mixture with said main-pipeline natural gas in flow-type reactor on metal block catalyst, wherein concentration of natural gas (methane) in mixture with emission gases should be 2.75, 2.4, and 0.5 vol % for three regeneration gas compositions used in regeneration cycle, which, at regeneration gas intake 40 m3/h used to replenish process flowsheet, will require consumption of natural gas for preliminary treatment of emission gases on metal block catalyst prior to being fed into regeneration circuit 1.1, 0.96, and 0.2 m3/h, respectively.
 Method for regenerating catalyst dehydrocyclization aliphatic hydrocarbons / 2159676
The invention relates to the regeneration of catalysts containing zeolite type pentasil, deactivated as the result of kokoulina when carrying out the reaction of dehydrocyclization aliphatic hydrocarbons
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FIELD: petrochemical process catalysts. SUBSTANCE: 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). EFFECT: preserved catalytically activity of zeolite catalyst. 10 cl, 1 dwg
The invention concerns a method and device for thermal removal of coke from the loose mass of granulated selective zeolite catalyst based on crystalline aluminosilicates type pentasil used in the reactor for the production of lower olefins, preferably olefins with 2 or 3 carbon atoms, of a mixture of higher olefins, preferably olefins with 4 to 8 carbon atoms, methanol or dimethyl ether, and at a preliminary stage reactor is washed with a stream of hot nitrogen, on the main stage through the reactor pass oxygen-containing gas with a temperature of 460 to 500°With the purpose of complete removal of coke from the zeolite catalyst, the additional stage reactor is washed nitrogen containing hydrocarbon stream of nitrogen is removed from the reactor. In European patent application EP-IN-0448000 described a method of obtaining a lower olefins from methanol by conversion of the reaction mixture containing vapors of methanol and/or dimethyl ether and water vapor carried out in a tubular reactor for indirectly cooled catalyst based on crystalline aluminosilicates type pentasil with the atomic ratio of silicon/aluminum constituting at least 10. A similar method is described in German patent application DE-A-19723363. From German patent application DE-A-19648795 a method of obtaining olepi the s with 3 and 4 carbon atoms of the initial mixture, containing olefins with 4-7 carbon atoms, by turning the mixture at a temperature of from 380 to 700°pellet selective zeolite catalyst based on crystalline aluminosilicates type pentasil as placed in a container of loose weight, and the atomic ratio si/al is in the range from 10:1 to 200:1. Similar zeolite catalyst used in the method of producing olefins with 2 or 3 carbon atoms from a source of hydrocarbon, described in the German patent application DE-A-10000899. In European patent application EP-A-0359843 describes a method of catalytic conversion of the original substances containing hydrocarbon and hydrogen, in light olefins in a fluidized bed of fine particles of catalyst at a temperature of from 400 to 500°C. to regenerate the catalyst Particles in a fluidized bed with a mixture of air/nitrogen. Before and after regeneration in a fluidized bed introducing the cleaning agent, e.g., nitrogen, with the aim of laundering linked with catalyst particles of the original substance, formed of light olefins, a mixture of air/nitrogen and the resulting regeneration products. The object of U.S. patent US-A-5648585 is a method of isomerization of linear olefins of at least four carbon atoms. The original substance in the presence improves the oxidation of the metal is passed through the stationary layer sintet the ical zeolite. As soon as the particles of zeolite are formed coke deposition, the layer of catalyst is washed with hot nitrogen and/or hydrogen. Then at a temperature not exceeding 490°To carry out the regeneration of the catalyst using oxygen-containing gas; in conclusion, the reactor is washed with nitrogen. European patent application EP-A-0071137 relates to a method of regeneration of catalysts with deposits of coke and/or coke precursors through a gas mixture containing molecular oxygen and water vapor. Catalysts containing more than 50 wt.% United with oxygen, silicon, regenerate at a temperature of from 300 to 450°C. In European patent application EP-A-0909804 describes a method of producing ethylene and propylene by catalytic pyrolysis of heavy hydrocarbons. In the presence of zeolite catalyst type pentasil heavy hydrocarbons are subjected to catalytic degradation using water vapor carried out at a temperature of from 650 to 750°C. Since the transformation of higher olefins in the lower olefins accompanied by the formation of coke deposits on the particles of the zeolite catalyst, after about 1000 hours of operation zeolite catalyst becomes necessary to remove coke. To this end, as is well known in the reactor it is necessary to introduce heated to a temperature of about 500 With water vapor. By opening the appropriate valve in the reactor serves the air in such quantity that the initial ratio of air and water vapor was about 0.1 (mass ratio). Begins spontaneous burning of coke, further propagating along zakochany sections. Must be under strict control zones possible overheating and, if necessary, to reduce the air flow before the reaction temperature exceeds the maximum allowable value. If zones of overheating are not detected and the process of removing coke stabilized, the air flow rate increases, increasing the ratio of air/water vapor to 0.3. In the process of removing coke temperature in the reactor is maintained at a level of 500°C. In the process of removing coke consumption of supplied air increases in several stages, maintaining a constant flow of water vapor and temperature at the exit of the furnace. At the same temperature at the outlet of the reactor (500° (C) on completion of the removal of coke from the catalyst can be judged by the termination of the temperature increase at the outlet of the reactor. The disadvantage of this method of removal of coke is that water vapor washes away from the zeolite catalyst components containing aluminum, and the resulting changes in the structure then has about the negative impact on the activity of the zeolite catalyst, which in extreme situations can be completely lost. The present invention is to design the above-described method, to ensure the highest possible conversion of higher olefins in the lower olefins at the lowest possible consumption of zeolite catalyst based on crystalline aluminosilicates type pentasil. This problem is solved due to the fact that at the preliminary stage, the reactor is washed with a stream heated to the temperature at the inlet of 460 to 500°With nitrogen to push the hydrocarbons from the zeolite catalyst, and then the reactor is cooled to the appropriate stream heated to the temperature at the entrance from 420 to less than 460°With nitrogen, on the main stage passed through the reactor is slowly heated to a temperature input from 460 to 500°With a mixture of nitrogen/air to the complete removal of coke from the zeolite catalyst, and an additional stage reactor is washed by the flow of heated up the temperature at the entrance of 460 to 500°With nitrogen, with the aim of leaching contained in a zeolite catalyst air. In accordance with a preferred embodiment of the method according to the invention a mixture of nitrogen/air can optionally contain up to 75 vol.%, preferably from 40 to 60 vol.% water vapour. Depending on the degree of coke formation on predvaritelnaya the catalyst is washed with nitrogen during the period, comprising from 8 to 16 hours, and then cooled with nitrogen during the period of from 1 to 8 hours. Next on the main stage through the reactor in several technological steps through the mix with nitrogen/air, heated at every process stage 5-20°during the period of, respectively, 0.5 to 1.0 hour, and at every process stage maintain a constant temperature mixture of nitrogen/air inlet to the reactor over a period of from 6 to 16 hours, preferably from 8 to 12 hours, if necessary, up to 24 hours. The air content in the mixture of nitrogen/air ranges from 2 to 10 vol.%, and as the process of removal of coke, at least on the latest technological level, it increases to 50%vol. Coming out of the reactor stream containing hydrocarbons nitrogen flushing sent for heat treatment, in which process stream removed from the reactor used for cooling of nitrogen discharged into the atmosphere or returned to re-cycle. A large part coming from the reactor a mixture of nitrogen/air return in the reactor and only a small portion is discharged into the atmosphere. The device for implementing the method according to the invention consists of a heater intended for heating the flow of nitrogen and the flow of the mixture of nitrogen/in the spirit serially connected reactor sequentially attached dust collector, sequentially attached cooler and consistently attached blower. Special design of the device provides for the availability before the heater heat exchanger, through which pass coming out of the reactor containing the dust is a mixture of nitrogen/air prior to its entering the dust collector. The invention is illustrated with the aid of the drawing process flow diagram and example of execution. Upon receipt of ethylene and propylene at the facility for ethylene production in large quantities as by-products are formed olefins with 4 and 5 carbon atoms. These olefins through the implementation of the gas-phase adiabatic reactions on zeolite catalyst (2) based on crystalline aluminosilicates type pentasil placed in granular mass in a horizontal reactor (1)can be converted into olefins with 2 or 3 carbon atoms. According to the invention after about 1000 hours of operation, this catalyst must be regenerated, that is, removal of the covering particles of catalyst coke. To this end, the reactor (1) via the corresponding valve cut off from the rest of the operating reactors. In accordance with the programme of removal of coke on Tr is aprovado (3) to the heat exchanger (4) and further along the pipeline (5) to the heater (6) serves 15.600 m 3/h of nitrogen, where it is heated to a temperature 480°C. Coming out of the heater (6) a stream of nitrogen directed by pipeline (7) into the reactor (1). Containing absorbed hydrocarbons stream of nitrogen is removed from the reactor (1) and pipe (8) is directed to the heat exchanger (4). Emerging from the heat exchanger (4) through the pipeline (9) the flow of nitrogen is directed through the collector (10) and the pipe (11) to the evaporator (12) and then through the pipe (13) to the compressor of the exhaust gas (14). Coming out of the supercharger (14) through line (15) stream of nitrogen through the pipeline (16) is directed to the torch. The duration of the washing of the zeolite catalyst is 12 hours. Then the reactor (1) for 4 hours, cooled appropriate amount of nitrogen, heated in the heater (4) to the temperature at the inlet to the reactor 440°C. Leaving the reactor (1) a stream of nitrogen through the pipeline (17) return to the circulation loop installation. Order the immediate removal of coke to nitrogen admixed with 5% vol. supplied by pipeline (18) of the air, and the temperature of the mixture of nitrogen/air inlet in the reactor increase in several technological steps (10°at each step)until it reaches 480°s, and temperature, which has the gas mixture at the inlet of the reactor at each of these processing stages, maintain at a constant level is 12 hours. Upon reaching the temperature of the mixture of nitrogen/air inlet in the reactor 480°With the air content in it increases initially up to 25%and then to 50%, and the duration of transmission of each of the respective mixtures is 12 hours. The removal of coke is finished when the temperature rise in the loose mass of the catalyst approaches zero or the consumption of oxygen in the reactor is reduced or completely stopped. The final technological stage, the addition of air stopped, and the reactor (1) for 12 hours, washed with nitrogen to remove oxygen of the zeolite catalyst and reactor. The advantage provided by the present invention is, in particular, that due to the use of a mixture of nitrogen and air to remove coke from the zeolite catalyst of its catalytic activity is fully preserved. 1. The method of thermal removal of coke from granulated, selective zeolite catalyst based on crystalline aluminosilicates type pentasil to obtain olefins with 2 or 3 carbon atoms from a mixture of olefins with 4 to 8 carbon atoms or methanol or dimethyl ether used in the reactor (1), and at the preliminary stage reactor is washed with a stream of hot nitrogen, on the main stage through the reactor pass oxygen-containing gas with the temperature of the t 460 to 500° To complete removal of coke from the zeolite catalyst, the additional stage reactor is washed with nitrogen, and containing the hydrocarbon stream of nitrogen is removed from the reactor, characterized in that the said catalyst is used in the form of a layer of granular mass (2) and at the preliminary stage reactor (1) is washed with a stream heated to the temperature at the inlet of 460 to 500°With nitrogen to push the hydrocarbons from the zeolite catalyst, and then the reactor is cooled by a flow of heated up to the temperature at the entrance from 420 to less than 460°With nitrogen, on the main stage through the reactor miss slowly heated to the temperature at the inlet of 460 to 500°With a mixture of nitrogen/air, and an additional stage reactor is washed by the stream heated to the temperature at the inlet of 460 to 500°With nitrogen, with the aim of removing air from the zeolite catalyst. 2. The method according to claim 1, characterized in that at the preliminary stage reactor (1) is washed with nitrogen over a period of from 8 to 16 o'clock 3. The method according to claim 1 or 2, characterized in that at the preliminary stage reactor (1) is cooled by nitrogen during the period of from 1 to 8 hours 4. The method according to claim 1, characterized in that on the main stage through the reactor (1) in several technological steps through the mix with nitrogen/air, heated at every process stage 5-20°for per the ode, constituting, respectively, from 0.5 to 1.0 h, and at each technological stage maintain a constant temperature mixture of nitrogen/air inlet to the reactor over a period of from 8 to 16 hours, preferably from 8 to 12 hours, if necessary, up to 24 hours 5. The method according to claim 4, characterized in that a mixture of nitrogen/air and air content of 2 to 10 vol.%, which as the process of removal of coke, at least on the latest technological level, increase up to 50%vol. 6. The method according to claim 1, characterized in that the output from the reactor (1) stream containing hydrocarbons nitrogen is directed to thermal processing. 7. The method according to claim 1, characterized in that the flow extracted from the reactor (1), used for cooling of the nitrogen discharged into the atmosphere or returned to re-cycle. 8. The method according to claim 1, characterized in that a large part derived from the reactor (1) a mixture of nitrogen/air return into the reactor and a small portion is discharged into the atmosphere. 9. A device for implementing the method according to one of claims 1 to 8, characterized in that it consists of a heater (6), intended for heating the flow of nitrogen and the flow of the mixture of nitrogen/air, serially connected reactor (1), sequentially attached dust collector (10), sequentially attached vzducholod the body (12) and sequentially attached to the supercharger (14). 10. The device according to claim 9, characterized in that the front of the heater (6) is additionally installed, the heat exchanger (4).
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