RU2773016C1 - Regenerator of the paraffin hydrocarbons dehydrogenation system c3-c5 (variants) - Google Patents

Abstract

FIELD: petrochemistry.

SUBSTANCE: invention relates to the field of petrochemistry, in particular to installations for dehydrogenation of paraffin hydrocarbons C3-C5 into corresponding olefin hydrocarbons used to produce basic monomers for synthetic rubber, as well as in the production of polypropylene, methyltretic butyl ether, etc. The invention concerns a regenerator of a C₃-C₅ paraffin hydrocarbon dehydrogenation system with a fluidized bed of a finely dispersed alumo-chrome catalyst having a cylindrical housing (1), an air supply pipeline (2) through a distributor (3) in the lower part of the fluidized bed, a fuel gas input pipeline (4) through a burner device (5) in the upper part of the fluidized bed, the transport pipe (7) for entering the upper part of the fluidized bed of a gas suspension from the catalyst spent in the reactor and the transporting air (46), partitioning gratings (8) located along the height of the fluidized bed, containing at the same time a catalyst heating zone (9) by burning fuel gas supplied to the burner device (5) and burning coke from the catalyst in the upper part of the fluidized bed, a catalyst oxidation zone and desorption of oxidation products (10) by air supplied to the regenerator in the lower part of the fluidized bed above the air distributor (3), as well as a catalyst preparation reduction-desorption cup (11) in the lower part of the regenerator housing (1), which has overflow holes (20) in the upper part for the flow of the catalyst from the regenerator into the reducing cup (11), distributors (13), (14) for supplying, respectively, the reducing gas through the pipeline (15) and inert gas through the pipeline (16), partitioning grids (12) located at the height of the reducing cup (11), a gas pipe (22) for removing the exhaust gases of the catalyst preparation to the upper part of the fluidized bed of the regenerator connected to the upper lid (21) of the reducing cup (11), and a nozzle (17) in the lower part of the reducing cup (11) for the output of the regenerated and prepared catalyst to the reactor through a pipeline (42), as well as the branch pipe of the regeneration gases (55) in the upper part of the regenerator housing (1). In the catalyst heating zone (9), a burner device (31) is installed for afterburning the exhaust gases of the catalyst preparation (39), containing a gas pipe (22) with an open upper end (64) pointing upwards. Mounted on the upper end (64) of the gas pipe (22), the first disk (23) surrounding the opening of the gas pipe (22), and the second disk (24) located some distance up from the first disk (23) and is rigidly connected to it to form between the disks (23), (24) an open ring-shaped space (25). The burner device (31) has a dispensing chamber (26), (43) connected to the air inlet pipeline (28), made in the form of a dispensing pipe (27) attached to the second disk (24) and located coaxially inside the gas pipe (22) or in the form of an annular box (47) surrounding the gas pipe (22), and the dispensing chambers (26), (43) have, respectively, metering holes (29), (45) located below the first disk (23) of the burner device (31) in the wall of the dispensing pipe (27) or in the wall of the gas pipe (22) located below the first disk (23) of the burner device (31), for the intake of air into the exhaust gas stream of catalyst preparation (39) with the formation of a ring-shaped channel (50) or cylindrical channel (37) on the section of the gas pipe (22) between the metering holes (29), (45) and the first disk (23) of the burner device (31), which are the mixing chamber for pre-mixing of the exhaust gases of the preparation of the catalyst and the air supplied through the pipeline (28). The invention also concerns a variant of the regenerator of the C₃-C₅ paraffin hydrocarbons dehydrogenation system.

EFFECT: increase in the efficiency of afterburning of the combustible part of the products of the reduction-desorption preparation of the catalyst in the fluidized bed of the regenerator heating zone, with improved conditions for the safe conduct of the process, an increase in the technical and economic indicators of the processes of dehydrogenation of paraffin hydrocarbons, reducing air consumption for regeneration, increasing the activity of the catalyst, stabilizing the operation and expanding the possibilities of increasing the capacity of dehydrogenation plants.

48 cl, 8 dwg, 1 tbl

Description

The invention relates to the field of petrochemistry, in particular to installations for the dehydrogenation of C ₃ -C ₅ paraffinic hydrocarbons into the corresponding olefinic hydrocarbons used to obtain basic monomers for synthetic rubber, as well as in the production of polypropylene, methyl tertiary butyl ether, etc.

Typical installations for the dehydrogenation of paraffinic hydrocarbons (I.L. Kirpichnikov, V.V. Beresnev, L.M. Popov "Album of technological schemes of the main industries of the synthetic rubber industry", Chemistry, Leningrad, 1986, pp. 8-12, 57-74) include a reactor and a regenerator with a fluidized bed of fine alumina-chromium catalyst with catalyst circulation between them. The regenerator has a cylindrical body, air inlet pipes through a distributor in the lower part of the fluidized bed, fuel gas inlet through the burner in the upper part of the fluidized bed, cyclones with dust risers connected to regeneration gas outlet pipes in the upper separation zone of the regenerator, a transport pipe with a catalyst distributor in the form of a baffle disc located above the level of the fluidized bed, for introducing the catalyst spent in the reactor in a coked and cooled form during the endothermic dehydrogenation reaction and the air transporting the catalyst, partitioning grids located along the height of the fluidized bed. At the same time, the regenerator contains a catalyst heating zone by burning the fuel gas supplied to the burner, which is a system of perforated pipes, and burning coke from the catalyst in the upper part of the fluidized bed, as well as a catalyst oxidation zone and desorption of oxidation products by air supplied to the regenerator in the lower part of the fluidized bed. layer above the air distributor. The regenerator also has a vessel for reduction-desorption preparation of a catalyst with a fluidized bed, which is divided by grids into sections, built into the lower part of the housing, and has branch pipes in the lower part for introducing a reducing gas for catalyst reduction, an inert gas for desorption of reduction products, and a transport pipe for outputting heated and regenerated catalyst in reduced form to the reactor.

The disadvantages of the known regenerator include insufficient activity of the regenerated catalyst and, accordingly, reduced yields of olefinic hydrocarbons due to the fact that a significant amount of residual reducing gas and reaction water poisoning the catalyst (Minachev Kh.M. et al., journal "Petrochemistry" , 1969, v. 27, No. 5, p. 677, Tyuryaev I.Ya., "Theoretical foundations for the production of butadiene and isoprene by dehydrogenation methods", Kyiv, "Naukova Dumka", 1973, p. desorption preparation of the catalyst and enters the lower part of the oxidation zone, significantly reducing the degree of oxidation of the catalyst and desorption of water in the specified zone of the regenerator.

The closest to the proposed solution is a regenerator with the removal of gases of the reduction-desorption preparation of the catalyst into the combustion zone of the gaseous fuel supplied to the regenerator (international application WO 2017/105283, IPC B01J38/30; C07C11/06; C07C11/08; C07C11/10; C07C5/ 333, published on June 22, 2017, patent RU 2666541, IPC B01J38/30; С07С11/06; С07С11/08; С07С11/10; С07С5/333, published on September 11, 2018). In said regenerator, above the catalyst preparation cup, there is a collection chamber for collecting gases of reduction-desorption preparation, consisting of a cylindrical shell adjacent to the upper edge of the cup and a truncated cone-shaped cover with a large base adjacent to the shell and with a smaller base directed upwards, to which adjoins a gas pipe installed in such a way that its upper end is located in the area of combustion of the gaseous fuel of the regenerator, while an elliptical baffle is installed above the upper end of the pipe, and in the cylindrical shell there are openings for the overflow of the circulating catalyst from the regenerator into the catalyst preparation cup. However, this regenerator has the following main disadvantages:

- local introduction into the fluidized bed of the heating zone of the regenerator of the products of the reduction-desorption preparation of the catalyst leads to incomplete combustion of the residual gas-reductant contained in the products of the preparation of the catalyst, its entry into the separation zone of the regenerator with a deterioration in the conditions for the safe conduct of the process, which requires an increase in the volume of the heating zone and , respectively, the amount of catalyst loaded into the regenerator, leading to an increase in the residence time of the catalyst in the high-temperature heating zone of the regenerator and to the creation of conditions for increasing the thermal deactivation of the catalyst, which also determines the increased consumption of the catalyst and requires an increase in the air supply to the regenerator;

- low efficiency of desorption of the catalyst directly with nitrogen due to the short residence time of the catalyst in the desorption zone in the lower part of the reducing glass (with a small distance between the distributors of the reducing gas and nitrogen) and low heat and mass transfer in a free, unorganized fluidized bed in this zone;

- unreliability and instability of the outflow of gases from the catalyst preparation cup through the narrow channel of the gas pipe, which is accompanied by a rapid clogging of the pipe with catalyst and practically leads to an analogue operation with the entry of these gases into the catalyst oxidation zone and to a decrease in the activity of the regenerated catalyst;

- limited possibilities for increasing the capacity of the dehydrogenation unit and increasing the activity of the catalyst by forcing the catalyst preparation mode by increasing the consumption of the reducing gas and inert gas in the beaker for the reduction-desorption preparation of the catalyst.

The objective of the present invention is to improve the technical and economic performance of paraffin hydrocarbon dehydrogenation processes by reducing catalyst consumption, reducing air consumption for regeneration, increasing catalyst activity, stabilizing operation and expanding the possibilities for increasing the capacity of dehydrogenation units.

To solve this problem, a regenerator of the C ₃ -C ₅ paraffinic hydrocarbon dehydrogenation system with a fluidized bed of a finely dispersed alumina-chromium catalyst is proposed, having a cylindrical body 1, an air supply pipeline 2 through a distributor 3 in the lower part of the fluidized bed, a fuel gas input pipeline 4 through the burner device 5 in the upper part of the fluidized bed, the transport pipe 7 for introducing into the upper part of the fluidized bed a gas suspension from the catalyst exhausted in the reactor and transport air 46, partitioning grates 8 located along the height of the fluidized bed, containing the heating zone of the catalyst 9 by burning the fuel supplied to the burner 5 gas and coke burning from the catalyst in the upper part of the fluidized bed, a zone for the oxidation of the catalyst and desorption of oxidation products 10 supplied to the regenerator with air in the lower part of the fluidized bed above the air distributor 3, as well as a glass for reduction-desorption preparation of the catalyst 11 in the lower part of the regenerator body 1, having overflow holes 20 in the upper part for the catalyst flow from the regenerator to the reducing glass 11, distributors 13, 14 for supplying respectively the reducing gas through the pipeline 15 and inert gas through the pipeline 16, partitioning grids 12, arranged along the height of the reducing vessel 11, a gas pipe 22 for removing exhaust gases from the preparation of the catalyst into the upper part of the fluidized bed of the regenerator, connected to the upper cover 21 of the reducing vessel 11 and a branch pipe 17 in the lower part of the reducing vessel 11 for outputting the regenerated and prepared catalyst through the pipeline 42, as well as the regeneration gas outlet 55 in the upper part of the regenerator housing 1, in which a burner 31 can be installed in the heating zone of the catalyst 9 for afterburning the exhaust gases of the catalyst 39 preparation, containing a gas pipe 22 with an open upper end 64 directed up, mouth the first disk 23, installed on the upper end 64 of the gas pipe 22, surrounding the opening of the gas pipe 22 and the second disk 24, located at some distance upwards from the first disk 23 and rigidly connected to it with the formation of an open annular space 25 between the disks 23, 24, while the burner device 31 has a distributing chamber 26, 43 connected to the air inlet pipeline 28, made in the form of a distributing pipe 27 attached to the second disk 24 and located coaxially inside the gas pipe 22 or in the form of an annular box 47 surrounding the gas pipe 22, and the distributing chamber 26, 43 have, respectively, in the wall of the distributing pipe 27 or in the wall of the gas pipe 22, located below the first disk 23 of the burner device 31, dosing holes 29, 45 for air inlet into the exhaust gas stream of preparing the catalyst 39 with the formation of gas pipe 22 between the dosing holes 29, 45 and the first disk 23 of the burner device 31 annular about the channel 50 or the cylindrical channel 37, which is a mixing chamber for pre-mixing the exhaust gases of the preparation of the catalyst and supplied through the pipeline 28 air.

Burner device 31 with an annular channel 50 may include a cone-divider 49, attached with its base to the lower end of the distributing pipe 27 of the distributing chamber 26 with the top pointing down.

The burner device 31 with a cylindrical channel 37 may contain a cone-reflector 6 attached with its base to the second disk 24, with the cone-reflector 6 directed with its top down and centered above the opening of the gas pipe 22.

In the burner device 31, which has a distributing chamber 43 connected to the pipeline for introducing air 28, made in the form of an annular box 47 surrounding the gas pipe 22, having in the wall of the gas pipe 22 located below the first disk 23 of the burner device 31 dosing holes 45 for air inlet into the stream exhaust gases of catalyst preparation 39, the transport pipe 7 can be located coaxially inside the gas pipe 22 with the formation of an annular channel 50 between the pipes, which is a mixing chamber for pre-mixing the exhaust gases of catalyst preparation 39 and air supplied through the pipeline 28, while the transport pipe 7 passes the second disk 24 in its central part with the location of the upper open end 63 of the transport pipe 7, equipped with a distributor of catalyst and transport air 40, above or below the level of the fluidized bed 38.

It is also proposed a regenerator of the system for dehydrogenation of paraffinic hydrocarbons C ₃ -C ₅ with a fluidized bed of a finely dispersed alumina-chromium catalyst, including a cylindrical body 1, a pipeline 2 for supplying oxygen-containing gas through the main distributor 3 in the lower part of the fluidized bed, a pipeline for introducing fuel gas 4 through the burner device 5 in the upper parts of the fluidized bed, a transport pipe 7 for introducing into the upper part of the fluidized bed a gas suspension from the catalyst exhausted in the reactor and transport air 46, partitioning grids 8 dividing the fluidized bed into sections arranged in series from top to bottom, the heating zone of the catalyst 9 by burning the feed into the burner 5 fuel gas and coke burning from the catalyst in the upper part of the fluidized bed and a zone for the oxidation of the catalyst and desorption of oxidation products 10 supplied to the regenerator by oxygen-containing gas in the lower part of the fluidized bed above the main distributor 3 of oxygen-containing gas, containing also built into the lower part of the body 1 of the regenerator glass reduction-desorption preparation of the catalyst 11 with a fluidized bed, partitioned gratings 12, having distributors 13, 14 in the lower part, connected to the pipelines, respectively, for introducing the reducing gas 15 and the inert gas 16, as well as a branch pipe 17 for the output of the regenerated catalyst through the pipeline 42 to the reactor located in the upper part of the reducer beaker 11, the chamber 18 for collecting off-gases of the reduction-desorption preparation of the catalyst, consisting of a cylindrical shell 19 with holes 20 for the overflow of the circulating catalyst from the regenerator to the reducing beaker 11 and a top cover 21 in the form of a truncated cone with a large base adjacent to the upper edge of the cylindrical shell 19 and with a smaller base directed upwards, to which a gas pipe 22 is connected to remove exhaust gases from catalyst preparation to the upper part of the fluidized bed generator, the regeneration gas outlet pipeline 52 through the pipe 55 in the upper part of the regenerator housing 1, while the regenerator may include a burner 58 for afterburning the exhaust gases of catalyst preparation, including a transport pipe 7 located inside the gas pipe 22 in such a way that the upper end 63 of the transport pipe 7 can be located below the upper end 64 of the gas pipe 22 or that the upper end 63 of the transport pipe 7 is located in the fluidized bed in the heating zone of the catalyst 9 at the same level with the upper end 64 of the gas pipe 22, both pipes are installed coaxially with the body 1 of the regenerator with the formation of an annular annular space 65, and on the upper end 64 of the gas pipe 22, the first disk 23 is installed, surrounding the opening of the gas pipe 22 and the second disk 24, located at some distance upwards from the first disk 23 and rigidly connected to it to form an open annular space 25 between disks 23, 24, which is a mixture 39 and a gas suspension from the spent catalyst in the reactor and transport air 46.

The burner 58 for afterburning the exhaust gases of the catalyst preparation may include a third disk 61 surrounding the opening of the transport pipe 7 on its upper end 63, mounted horizontally and having an outer diameter less than the diameter of the opening of the gas pipe 22, forming between the said third disk 61 and the gas pipe 22 an annular slot 62 for the inlet of exhaust gases from catalyst preparation 39 into the gas suspension flow from the catalyst spent in the reactor and transport air 46.

The upper part of the gas pipe 22 can be made in the form of a narrowing, which is a truncated cone 59 with a smaller base directed upwards, which forms the upper end 64 of the gas pipe 22 and creates an annular slot 60 between the specified end and the transport pipe 7 for the inlet of exhaust gases of catalyst preparation 39 into the flow of gas suspension from the catalyst spent in the reactor and transport air 46.

The burner 58 for afterburning the off-gases of catalyst preparation may comprise a distributing chamber 43 connected to the pipeline for introducing additional air 28 in the form of an annular box 47 surrounding the gas pipe 22, having dosing holes 45 in the wall of the gas pipe 22 for air inlet into the off-gases of the preparation catalyst 46, thus forming between these holes and the first disk 23 an annular annulus 57 pre-mixing of the supplied air and exhaust gases of the catalyst preparation.

Dosing holes 29, 45 for air inlet into the catalyst preparation exhaust gas stream can be located below the first disk 23 at a distance from it of at least 40*d, where d is the diameter of one dosing hole 29, 45.

In the top cover 21 of the cup-reductant 11 and/or in the gas pipe 22 can be located fitting 41 to enter the gas pipe 22 purge air.

The burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 may contain a cone-reflector 6 attached with its base to the second disk 24, and the cone-reflector 6 is directed with its apex down and is centrally located above the opening of the gas pipe 22 or transport pipe 7 for input gas suspension from the catalyst spent in the reactor and transport air 46.

The first disk 23 of the burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 can be installed horizontally.

The first disk 23 of the burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 may be in the form of a truncated cone with an inclination of the generatrix of the cone at an angle in the range from 30° downward from the horizontal position to 30° upward from the horizontal position.

The second disk 24 of the burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 can be installed horizontally.

The second disk 24 of the burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 may be in the form of a cone or a truncated cone with an inclination of the generatrix of the cone at an angle in the range from 30° upwards from the horizontal position to 45° downwards from the horizontal position and is mounted with the top down or up in the center above the opening of the transport pipe 7 for introducing gas suspension from the catalyst spent in the reactor and transport air 46.

The ratio of the diameter of the first disk 23 of the burner device 31, 58 for afterburning the exhaust gases of the preparation of the catalyst 39 to the diameter of the regenerator body 1 can range from 0.1 to 0.3.

In the burner 31, 58 for afterburning the off-gases of the preparation of the catalyst 39, the ratio of the diameter of the first disk 23 to the diameter of the second disk 24 can be in the range of 0.8 to 1.25.

The ratio of the diameter of the base of the cone-reflector 6 to the diameter of the opening of the transport pipe 7 can be in the range of values from 0.3 to 1.0.

The second disk 24 can be rigidly connected to the first disk 23 by means of baffles 34.

The number of partitions 34 may range from 3 to 12.

The baffles 34 can be evenly distributed around the circumference of the discs 23, 24, dividing the open annular space 25 into independent flow channels 51.

Baffles 34 may be flat, radially directed plates.

Partitioning grates 32 in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst 9 by burning fuel gas and burning coke, can have a free cross section larger than the partitioning grates 8 in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst 10 supplied to the regenerator oxygen-containing gas.

The distance between the partitioning grates 32 in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst 9 by burning fuel gas and burning coke, can be greater than the distance between the partitioning grates 8 in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst 10 by the supplied oxygen-containing gas.

The burner device 31, 58 may be located below the level of the fluidized bed 38 above or below one or more upper sectional grates 32.

An additional air distributor 30 can be located below the main air distributor 3 under the holes 20 for the overflow of the circulating catalyst from the regenerator into the reducing glass 11.

The main air distributor 3 can be located above or below the holes 20 for the overflow of the circulating catalyst from the regenerator to the reducing glass 11.

Additional grids 67 can be installed between the distributors of the reducing gas 13 and nitrogen as an inert gas 14 in the reducing glass 11.

As feedstock for dehydrogenation plants, paraffinic hydrocarbons C ₃ -C ₅ can be used, such as, for example, isobutane, n-butane, isopentane, propane with a paraffin content in the feedstock, preferably 95-99 wt. %, as well as mixtures of these paraffinic hydrocarbons.

In the implementation of the proposed method of regeneration of the catalyst in the reactor-regenerator system can be loaded chromium-aluminum catalyst containing Cr ₂ O ₃ - 13.0-25.0 wt. %, K ₂ O - 1.0-3.0 wt. %, SiO ₂ - 1.0-10.0 wt. %, Al ₂ O ₃ - the rest, when the content in the oxidized state of CrO ₃ - 0.25-3.5 wt. %.

For example, an industrial catalyst of the AOK-73-24 type.

By spent catalyst is meant the catalyst that was used in the dehydrogenation reactor, was desorbed, for example, using nitrogen to remove hydrocarbons from the catalyst, and cooled by the endothermic dehydrogenation reaction, coked and reduced, sent to the regenerator.

When implementing the proposed invention, natural gas, preferably containing methane, off-gas from dehydrogenation processes, containing up to 25 wt. %. hydrogen or light paraffinic hydrocarbons, etc. To increase the degree of reduction and, accordingly, the activity of the catalyst, it is preferable to supply the reducing gas in excess compared to that necessary for the complete reduction of the catalyst in accordance with the stoichiometry of the reduction reactions. Nitrogen is preferred for desorption.

Air, air enriched with oxygen (for example, by mixing air and oxygen) can be used as the oxygen-containing gas for catalyst regeneration. The oxygen concentration in the oxygen-containing gases supplied to the catalyst regeneration is limited (up to 50 wt %) by the process safety conditions.

As the purge gas supplied to the fitting 41 on the gas pipe 22 and/or the top cover 21 of the collection chamber 18, the air supply is preferred.

In FIG. 1 shows a diagram of the first version of the regenerator according to the invention. In FIG. 2 - 3 show other possible layouts of the proposed burner devices for afterburning exhaust gases of catalyst preparation according to the first variant.

In FIG. 4 shows a diagram of the regenerator of the proposed invention according to the second variant with the combined arrangement of the transport 7 and gas 22 pipes - a pipe in a pipe. In FIG. 5-8 show possible layouts of the proposed burner devices according to the second option for afterburning exhaust gases of catalyst preparation in the air flow supplied to transport the catalyst into the transport pipe 7 with the possible addition of additional air to the specified flow through the pipeline 28 through the distributing chamber 43 in the form of an annular box 47 , as well as purge air through pipelines 36.

Shown in FIG. 1, the regenerator has a cylindrical body 1, an air supply pipeline 2 through a distributor 3, a fuel gas supply unit 44, a fuel gas input pipeline 4 through the burner device 5 in the form of a perforated pipe, a transport pipe 7 for introducing the catalyst exhausted in the reactor and transport air, partitioning grids 8 , 32, catalyst heating zone 9, catalyst oxidation and oxidation products desorption zone 10, catalyst reduction-desorption preparation unit 11 in the form of a cup built into the lower part of the regenerator housing 1. The reducing glass 11 consists of a cylindrical shell 19 with holes 20 in the upper part of the cylindrical shell 19 for the overflow of the circulating catalyst from the regenerator into the reducing glass 11 and the top cover 21 in the form of a truncated cone, forming a collection chamber 18 for collecting off-gases of reduction-desorption preparation catalyst connected to the gas pipe 22, for exhaust gases of the preparation of the catalyst in the upper part of the fluidized bed of the regenerator. The reducing glass 11 has partitioning grids 12, distributors 13, 14 connected to pipelines for introducing reducing gas 15 and inert gas 16, as well as a branch pipe 17 for outputting the regenerated and prepared catalyst to the reactor. The proposed regenerator is equipped with a burner device 31 for afterburning the exhaust gases of the catalyst preparation. The burner 31 shown in FIG. 1, contains a gas pipe 22, mounted on the upper end 64 of the gas pipe 22, the first disk 23, surrounding the opening of the gas pipe 22 and the second disk 24, located at some distance upwards from the first disk 23 and rigidly connected to it (Fig. 2) using radially directed baffles 34 (not shown in FIG. 1) to form an open annular space 25 between the disks 23, 24. As shown in FIG. 2 (section A-A), baffles 34 divide the open annular space 25 into independent flow channels 51 (not shown in FIG. 1). The variant of the burner device 31 shown in FIG. 1, has a distributing chamber 26 in the form of a distributing pipe 27 connected to a pipeline 28 for supplying air, attached to the second disk 24 and located inside the gas pipe 22 coaxially with it and having dosing holes 29 in the wall of the distributing pipe 27 for air inlet into the exhaust stream. catalyst preparation gases. The annular channel 50 between the gas 22 and distributing 27 pipes in the area between the metering holes 29 and the first disk 23 of the burner device 31 is a mixing chamber of the burner device 31 for pre-mixing the exhaust gases of the catalyst preparation and the supplied air. The final mixing of these streams is carried out during their passage in the open annular space 25 between the discs 23 and 24 and subsequent release into the fluidized bed. The gas pipe 22 and the collection chamber 18 have fittings 41 for introducing purge air. A cone-divider 49 is attached to the lower end of the distributing pipe 27 (Fig. 1). Under the air distributor 3, below the overflow holes 20, there is an additional air distributor 30, which ensures the mobility of the catalyst in the area of the overflow holes 20.

Shown in FIG. 2 and 3, the burners comprise a dispensing chamber 43 formed by an annular box 47 surrounding the gas pipe 22 and dosing holes 45 in the wall of the gas pipe 22. The embodiment of the burner device 31 shown in FIG. 2, has an annular channel 50 for pre-mixing the exhaust gases of the preparation of the catalyst 39 and the supplied air in the form of a cylindrical channel at the end of the gas pipe 22 between the metering holes 45 and the first disc 23 of the burner device 31. The final mixing of these flows is carried out when they pass through an open annular space 25 between disks 23 and 24 and subsequent release into the fluidized bed. A cone-reflector 6 is attached to the second disk 24 of the burner device 31.

In the embodiment of the burner device 31 shown in FIG. 3, the transport pipe 7 is coaxially positioned within the gas pipe 22 to form an annular channel 50 between the pipes, which is a mixing chamber for pre-mixing the off-gases from catalyst preparation 39 and fed through conduit 28 to introduce additional air. The final mixing of these streams is carried out during their passage in the open annular space 25 between the discs 23 and 24 and subsequent release into the fluidized bed. In this case, the transport pipe 7 passes the second disk 24 in its central part with the location of the upper open end 63 of the transport pipe 7, equipped with a distributor of catalyst and transport air 40, above or below the level of the fluidized bed 38.

Shown in FIG. 4, the regenerator according to the second version comprises a cylindrical body 1, an air supply pipeline 2 through the main distributor 3 in the lower part of the fluidized bed, a fuel gas input pipeline 4 through the burner device 5 in the form of a system of perforated pipes in the upper part of the fluidized bed, cyclones 53 with dust risers 54 in the upper separation zone of the regenerator, connected to the branch pipe 55 and pipeline 52 for regeneration gas outlet, transport pipe 7 for introducing into the upper part of the fluidized bed a mixture of the catalyst spent in the reactor and transport air 46, partitioning grids 8 dividing the fluidized bed into sections arranged in series from top to bottom, the heating zone of the catalyst 9 by burning the fuel gas supplied to the burner 5 and burning coke from the catalyst in the upper part of the fluidized bed and the zone of oxidation of the catalyst and desorption of the oxidation products 10 by the air supplied to the regenerator in the lower part of the fluidized bed above the air distributor ear 3, which also contains a glass built into the lower part of the body 1 of the regenerator, a glass for the reduction-desorption preparation of the catalyst 11 with a fluidized bed, partitioned by gratings 12, having distributors 13, 14 in the lower part, connected to pipelines, respectively, for introducing the reducing gas 15 and the inert gas 16 , as well as a branch pipe 17 for outputting the regenerated catalyst to the reactor, located in the upper part of the reducing glass 11, a chamber 18 for collecting off-gases of the reduction-desorption preparation of the catalyst, consisting of a cylindrical shell 19 with holes 20 in its upper part for the overflow of the circulating catalyst from regenerator into a reducing glass 11 and a top cover 21 in the form of a truncated cone with a large base connected to a cylindrical shell 19 and with a smaller base directed upwards to which a gas pipe 22 is connected to remove exhaust gases from catalyst preparation to the upper part of the fluidized bed regenerator a. The proposed regenerator is equipped with a burner 58 for afterburning exhaust gases of catalyst preparation. The burner device 58 contains a transport pipe 7 located inside the gas pipe 22 in such a way that its upper end 63 is located in the fluidized bed in the heating zone of the catalyst 9 at the same level as the upper end 64 of the gas pipe 22, both pipes being installed coaxially with the regenerator body 1 with the formation of an annular annular space 57, and on the upper end 64 of the gas pipe 22, the first disk 23 is installed, surrounding the opening of the gas pipe 22 and the second disk 24, located at some distance up from the first disk 23 and rigidly connected to it (Fig. 5) with by means of radially directed baffles 34 to form an open annular space 25 between the discs 23, 24. As shown in FIG. 5 (section A-A), plate-shaped baffles 34 divide the open annular space 25 into independent flow channels 51. The burner device 58 shown in FIG. 4, contains a distributing chamber 43 in the form of an annular box 47 surrounding the gas pipe 22, connected to the pipeline 28 for introducing additional air and having metering holes 45 in the wall of the gas pipe 22 for inlet additional air into the exhaust gas flow of catalyst preparation, as well as an annular annulus 57 for pre-mixing the feed air and exhaust gases from catalyst preparation. The final mixing of these streams is carried out during their passage in the open annular space 25 between the discs 23 and 24 and subsequent release into the fluidized bed.

Shown in FIG. 6 burner device for the second version of the regenerator, contains a third disk 61, surrounding the opening of the transport pipe 7 having an outer diameter less than the diameter of the opening of the gas pipe 22, forming an annular slot 62 between the said disk and the gas pipe 22 for the inlet of exhaust gases of catalyst preparation into the flow of gas suspension from the catalyst and conveying air 46.

The gas pipe 22 shown in FIG. 7 of the burner device, contains in the upper part a narrowing in the form of a truncated cone 59, while the smaller base of the truncated cone 59 forms the upper end 56 of the gas pipe 22, connected to the first disk 23, forming an annular slot 60 between the inner wall of the smaller base of the cone and the transport pipe 7 for the inlet of exhaust gases of catalyst preparation into the flow of catalyst gas suspension and transport air 46.

In the shown in FIG. 8 of the burner device, the upper end 63 of the transport pipe 7 is located below the upper end 64 of the gas pipe 22, forming between the said upper ends 63, 64 a mixing chamber 66 of the exhaust gas streams of catalyst preparation and the gas suspension of the catalyst and transport air. The final mixing of these streams is carried out during their passage in the open annular space 25 between the discs 23 and 24 and subsequent release into the fluidized bed.

The proposed variants of the regenerator in various designs as part of the installations for the dehydrogenation of paraffinic hydrocarbons C ₃ -C ₅ with a fluidized bed of a finely dispersed alumina-chromium catalyst, for example, type AOK-73-24, operate under the following thermal conditions of the regenerator heating zone. The temperature of the flow of the gas suspension of the catalyst and the transport air coming from the reactor through the transport pipe 7 is mainly 500-560°C. The temperature of the exhaust gases of the preparation of the catalyst, sent to the burner device 31, is mainly 640-680°C. The temperature of the air sent to the burner is 50-100°C. The temperature of the heating zone of the catalyst 9 in the regenerator is maintained in the range of 640-690°C and is provided by the combustion of coke on the catalyst, the fuel gas supplied to the heating zone of the catalyst 9 through the burner device 5, and the afterburning of the exhaust gases of the preparation of the catalyst supplied through the gas pipe 22 to the burner device 31, 58. The composition of the catalyst preparation exhaust gases depends on the content of hexavalent chromium in the catalyst supplied from the regenerator oxidation zone to the catalyst preparation zone, as well as on the composition and amount of the reducing gas supplied for reduction. The use of modern efficient high-chromium dehydrogenation catalysts (with a high content of hexavalent chromium in the oxidized catalyst) requires an increase in the supply of reducing gas. The use of the proposed burner device 31 makes it possible to supply the reducing gas to the reducing glass 11 with an excess ratio equal to 1.1-2.5 compared to that required for complete recovery of the catalyst. The data presented in Table 1 were obtained using production off-gases or natural gas as a reducing gas when it was supplied to the reducing glass 11 with an excess coefficient equal to 1.5 compared to the stoichiometry required for the reduction reactions of hexavalent chromium oxides on the catalyst supplied from the oxidation zone of the regenerator, to trivalent after the recovery of the catalyst in the reducing glass 11. The content of hexavalent chromium in the oxidized catalyst was maintained in the range of 0.5-1.0 wt. % characteristic of modern high-chromium catalysts. As can be seen from Table 1, the exhaust gases of catalyst preparation in dehydrogenation processes are characterized by a high content of combustible hydrocarbon part, which provides a significant share in the heat balance of the regenerator during afterburning. So, for example, in the process of isobutane dehydrogenation, the share of the thermal power of the proposed afterburner burner, which allows the operation of the catalyst preparation unit in the range of change in the coefficient of natural gas supply excess for catalyst reduction, which is 1.5-2.5, reaches 4-13% of the total heat output of the regenerator heating zone with a corresponding reduction in the supply of natural gas to the existing burner 5. At the same time, the catalyst preparation gases are ballasted with a significant amount of non-combustible gases (nitrogen, CO ₂ ) and contain a large amount of reaction water to be removed from the system, which makes additional requirements for the organization of afterburning of the exhaust gases of the preparation of the catalyst in comparison with the combustion of these gases according to the prototype. These requirements are provided by the proposed design of the afterburner burner, its location in a fluidized bed, the layout of the regenerator heating zone, containing the proposed burner, partitioning grates and the existing burner for burning the supplied fuel gas.

The proposed regenerator (Fig. 1-3) according to the first version works as follows. Under the fluidized bed of the regenerator from the collector 33 through pipeline 2 to the main distributor 3 and through pipeline 35 to the additional distributor 30 air is supplied. The spent catalyst from the reactor, coked, reduced and cooled during the endothermic dehydrogenation reaction, mixed with transport air (in the form of a gas suspension) is fed through the transport pipe 7 through the distributor 40 to the upper part of the fluidized bed 38 of the regenerator. The air passes the fluidized bed 38 of the regenerator, partitioned by horizontal gratings 8 countercurrent to the descending circulating catalyst. To heat the circulating catalyst in order to provide heat for the endothermic dehydrogenation reaction, fuel gas is supplied through pipeline 4 to the upper part of the fluidized bed of the regenerator through the burner device 5 located in the heating zone of catalyst 9 for combustion in the flow of air supplied to the regenerator while simultaneously burning coke on the catalyst. The catalyst sequentially passes the heating zone of the catalyst 9, oxidation and desorption of the catalyst from the oxidation products 10, and then the reduction of the catalyst and desorption of the reduction products in the glass 11 of the reduction-desorption preparation of the catalyst. The oxidized catalyst passes through the reducing glass 11 to remove adsorbed oxygen and reduce hexavalent chromium to trivalent. The regenerated, heated and reduced catalyst is transported from the lower part of the reducing glass 11 through the branch pipe 17 to the reactor. The resulting regeneration gases enter the above-layer space of the regenerator and, after trapping fine fractions of the catalyst carried away from the fluidized bed in cyclones (not shown in Figs. 1, 2, 3), they leave the regenerator. The flow of exhaust gases from the preparation of the catalyst, containing a significant part of the residual gas-reducing agent, is directed through the gas pipe 22 to afterburn the combustible part of the flow into the burner 31, where also through the pipeline 28 through the distributing chamber 26 in the form of a distributing pipe 27 and dosing holes 29 into the waste stream catalyst preparation gases, air is supplied in an amount that provides the necessary excess air for complete combustion of the combustible part of the exhaust gases of catalyst preparation. The off-gases from the catalyst preparation contain some of the catalyst captured from the collection chamber 18, pass in the form of a gas suspension gas pipe 22 and enter in the upward flow mode into the annular channel 50 of the burner device 31. The specified annular channel 50 is a mixing chamber of the burner device 31 for pre-mixing the exhaust preparation gases and supply air. For effective mixing of these gases, air is introduced into the exhaust gas stream of catalyst preparation by a system of small jets centrally (Fig. 1) or peripherally (Fig. 2 and 3). Provided that the length of the mixing chamber of the burner device in the form of an annular channel 50 is not less than 40 * d where d is the diameter of the dosing holes 29, and also with sequential mixing of flows in the mixing chamber and in the open annular space 25 between the disks 23 and 24, complete mixing is ensured specified streams. When partitioning the open annular space 25 partitions 34, the specified space is divided into independent channels of the expiration of flows 51, which ensures the preservation of uniform distribution of flows when they flow along the channels. In this case, the resulting gas suspension passes through an open annular space 25 and enters the fluidized bed along the entire outer edge of the disks 23, 24 of the burner device 31 in the form of a continuous, fan-shaped, radially directed jet. In the initial section of the open annular space 25, there is first some delay in the flow and then a significant increase in the flow rate of the gas mixture and the trapped catalyst in the final section of the specified space of the burner device 31. This situation is provided by the inventive range of sizes of the structural elements of the burner device 31. Under the influence of the catalyst present in the flow , the gas mixture, consisting of the exhaust gases of the catalyst preparation and the supplied air, is dispersed in the burner 31 and at the point of entry into the fluidized bed is in the state of small bubbles, creating conditions for the formation of a torch with stable combustion of the combustible part of the exhaust gases of the catalyst preparation at the exit from the open of the annular space 25 of the burner device 31 into the high-temperature (650-690°C) heating zone of the fluidized bed of the catalyst 9. The annular space 25 of the burner device 31 allows the gas and catalyst to be released from the open annular space 25 of the burner device 31 at a significant distance from the outer edge of the disks 23, 24, forming a developed combustion flame in this space. The proposed burner device 31 makes it possible to maintain the gas flow rate at the exit from the open annular space 25 of the burner device 31, which exceeds the maximum speed of flame propagation and prevents the flame from flashing into the annular channel 50 in the form of a mixing chamber of the burner device 31. Uniform distribution of the gas-air mixture achieved using the invention and the captured catalyst around the circumference of the discs 23, 24 of the burner device 31 at the exit from the open annular space 25 ensures uniform distribution of the flame around the circumference of the discs and, in combination with the high intensity of heat and mass transfer processes in the upper part of the fluidized bed in the heating zone of the catalyst 9, a high level isothermality of the fluidized bed in the zone of existence of the torch, stable and sustainable combustion, high rate of combustion reactions and completeness of combustion of the combustible part of the exhaust gases of catalyst preparation. The proposed burner device 31 is characterized by ease of control with high efficiency of the afterburning process, provided by the ability to work with a large excess of air (with an excess ratio of 1.5 or more). Excess air after the burner device 31 enters the fluidized bed for further use in the heating zone of the catalyst 9 of the regenerator. At the same time, the heating zone of the catalyst 9, equipped with the existing burner device 5, plays the role of the second stage of afterburning the exhaust gases of the catalyst preparation, ensuring the complete combustion of the latter. When the torch of the proposed afterburner burner 31 interacts with the existing burner 5 for burning the supplied natural gas in the heating zone of the catalyst 9, the stability and stability of the burner operation is increased.

The proposed regenerator (Fig. 4-8) according to the second version works as follows. Under the fluidized bed of the regenerator from the collector 33 through the pipeline 2 through the main distributor 3 and through the pipeline 35 through the additional distributor 30 air is supplied. The spent catalyst from the reactor in a coked and reduced form, mixed with transport air, is fed through a transport pipe 7 through a burner device 58 (simultaneously being a distributor of catalyst and transport air flows) to the upper part of the fluidized bed. The air supplied to the regenerator passes the fluidized bed of the regenerator, sectioned by horizontal gratings 8 countercurrently to the circulating catalyst descending. To heat the circulating catalyst and provide heat for the endothermic dehydrogenation reaction in the reactor, fuel gas is supplied to the upper part of the fluidized bed of the regenerator through the burner 5 located in the heating zone of the catalyst 9 through pipeline 4 for combustion in the flow of air supplied to the regenerator while simultaneously burning coke on the catalyst . The catalyst sequentially passes the heating zone of the catalyst 9, oxidation and desorption of the catalyst from the oxidation products 10, and then the reduction of the catalyst and desorption of the reduction products in the reducing glass 11 of the reduction-desorption preparation of the catalyst. The oxidized catalyst passes through the reducing glass 11 to remove adsorbed oxygen and reduce hexavalent chromium to trivalent. The regenerated, heated and reduced catalyst is transported from the lower part of the reducing glass 11 through the branch pipe 17 to the reactor. The resulting regeneration gases enter the above-layer space of the regenerator and, after trapping fine fractions of the catalyst carried away from the fluidized bed in cyclones 53, leave the regenerator. The small fractions of the catalyst caught in the 53 cyclones are returned to the upper part of the fluidized bed of the regenerator through the dust risers 54. Further, through pipeline 52, the regeneration gas enters for cooling, sanitary cleaning from catalyst dust and then is discharged through the chimney into the atmosphere. From the collector 33 through the pipeline 28 through the distributing chamber 43 in the form of an annular box 47 and through the dosing holes 45 into the flow of exhaust gases of the preparation of the catalyst, air is supplied in an amount sufficient to provide (in a mixture with the air transporting the catalyst also entering the burner device) the necessary excess air for complete combustion of the combustible part of the exhaust gases of catalyst preparation. In this case, the excess air after the burner device 58 enters the fluidized bed for additional use in the heating zone of the regenerator. In the flow path of the burner device 58, including the upper sections of the gas 22, transport 7 pipes and an open annular space 25 between the first 23 and second 24 disks of the burner devices (Fig. 4-8), the above flows are mixed and the subsequent combustion in the torch of the burner devices (at the outlet of the open annular space 25) the combustible part of the exhaust gases of the catalyst preparation. Provided that the length of the distributing chamber 43 in the form of an annular box 47 is not less than 40 * d, where d is the diameter of the dosing holes 45, and also with sequential mixing of flows in the mixing chamber and in the open annular space 25 between the disks 23 and 24, complete mixing is ensured specified streams. The efficiency of mixing streams can be increased by increasing the exhaust gas flow rate of the catalyst preparation when they are introduced into the flow of the catalyst gas suspension and transport gas in the initial section of the open annular space 25 by installing the third disk 61 or by narrowing the gas pipe 22 in the form of a truncated cone 59 (Fig. .6 and 7). In FIG. 8 shows a variant of increasing the efficiency of mixing flows due to the possible increase in the length of the pre-mixing chamber 66 while simplifying the design of the burner device. It is also possible to simplify the design when partitioning the open annular space 25 with partitions 34, the specified space is divided into independent channels for the flow of flows 51, which ensures that the distribution of flows remains uniform when they flow along the channels. In this case, the resulting gas suspension passes through an open annular space 25 and enters the fluidized bed along the entire outer edge of the disks 23, 24 of the burner device 58 in the form of a continuous, fan-shaped, radially directed jet. In the initial section of the open annular space 25, there is first some delay in the flow and then a significant increase in the flow rate of the gas mixture and the catalyst captured by the exhaust gases from the pipe 22 and transported from the pipe 7 in the final section of the specified space of the burner device 58. This situation is provided by the claimed range of sizes of structural elements burner device 58. Under the influence of the catalyst present in the stream, the gas mixture, consisting of exhaust gases from the preparation of the catalyst and the supplied air, is dispersed in the burner device 58 and is in the state of small bubbles at the point of entry into the fluidized bed, creating conditions for the formation of a torch with stable combustion the combustible part of the exhaust gases of the catalyst preparation at the exit from the annular slot 48 of the burner device 58 into the high-temperature (640-660°C) heating zone of the fluidized catalyst bed. An increase in the rate of outflow of the mixture of gas and catalyst in the final section of the open annular space 25 of the burner device 58 allows the gas and catalyst to be released from the annular slot 48 of the burner device 58 at a significant distance from the outer edge of the disks 23, 24, forming a developed combustion flame in the specified space. The proposed burner device 58 makes it possible to maintain the gas flow rate at the exit from the annular slot 48 of the burner device 58, which exceeds the maximum flame propagation speed and prevents the flame from flashing into the distributing chamber 43 of the burner device 58. disks 23, 24 of the burner device 58 at the exit from the annular slot 48 ensures uniform distribution of the flame around the circumference of the disks 23, 24 and, in combination with the high intensity of heat and mass transfer processes in the upper part of the fluidized bed in the heating zone of the catalyst 9, a high level of isothermality of the fluidized bed in the zone of existence of the torch, stable and stable combustion, high rate of combustion reactions and completeness of combustion of the combustible part of the exhaust gases of catalyst preparation. The proposed burner device 58 is characterized by ease of control with high efficiency of the afterburning process, provided by the ability to work with a large excess of air (with an excess factor of up to 1.5 or more). Excess air after the burner 58 enters the fluidized bed for further use in the heating zone of the regenerator. In this case, the heating zone of the catalyst 9, equipped with a standard burner, plays the role of the second stage of afterburning the exhaust gases of the catalyst preparation, ensuring the completeness of combustion of the latter. When the torch of the proposed afterburner burner interacts with the existing burner for burning the supplied natural gas in the heating zone of the catalyst 9, the stability and stability of the burner 58 is increased.

The use of the proposed burner device 31 and 58 for afterburning exhaust gases of the reduction-desorption preparation of the catalyst by supplying air with a large excess factor to the burner device 31 and 58 contributes to an increase in the oxygen concentration in the upper part of the fluidized bed of the regenerator, which leads to an increase in the efficiency of catalyst regeneration processes and, respectively, to increase the activity of the regenerated catalyst.

When using the proposed design of the regenerator, the efficiency of afterburning of the combustible part of the products of the reduction-desorption preparation of the catalyst in the fluidized bed of the heating zone of the regenerator is improved, with the improvement of the safe process conditions compared to the prototype. This opens up the possibility of increasing the capacity of the dehydrogenation unit and also increasing the activity of the catalyst by forcing the mode of the catalyst preparation unit by increasing the flow rate of the reducing gas and inert gas in the glass of the reduction-desorption preparation of the catalyst 11 with a corresponding increase in the air supply to the burner device 31 and 58.

Fittings 41 installed in the upper cover 21 of the reducing vessel 11 and in the gas pipe 22 for purging the gas pipe 22 with a small amount of air make it possible to prevent clogging of the gas pipe 22 with catalyst and, accordingly, to stabilize the operation of the regenerator in the optimal mode of afterburning the exhaust gases of catalyst preparation in the upper part of the boiling regenerator layer (in the heating zone of the catalyst 9).

The increase in the free section of the partitioning grates 32 and the distance between them in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst 9, in comparison with the partitioning grates 8 in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst 10 by the supplied air, ensures the optimal hydrodynamic regime of the boiling layer in these areas, as well as safe and stable combustion of the fuel gas and the combustible part of the exhaust gases of the reduction-desorption preparation of the catalyst in the heating zone of the catalyst 9.

The additional air distributor 30 ensures the fluidity of the catalyst layer in the area of the overflow holes 20 and, accordingly, improves the conditions for the flow of the circulating catalyst from the regenerator to the reducing glass 11, while reducing the entrainment into the reducing glass 11, which is uncontrolled during pressure pulsations in the fluidized bed, and, accordingly, into the gas pipe 22 of the gas from the oxidation zone of the regenerator, which stabilizes the operation of the burner device 31 and 58 and the reducing glass 11.

The installation between the distributors of the reducing gas 13 and nitrogen 14 in the reducing glass 11 additional gratings 67 increases the heat and mass transfer in the specified zone and, accordingly, the efficiency of desorption of the catalyst by the supplied nitrogen before the release of the catalyst into the reactor.

The use of the proposed design of the burner device 31, 58, which allows simultaneously to provide a more uniform distribution of the catalyst, gas flows and heat in the cross section of the upper part of the fluidized bed of the regenerator, as well as the location of the burner device 31, 58 under the level of the fluidized bed 38 above or below the upper partitioning grate 32 reduces catalyst carryover.

Thus, when using the proposed options for the design of the regenerator, the following technical result is provided: increasing the efficiency of afterburning the combustible part of the products of the reduction-desorption preparation of the catalyst in the fluidized bed of the regenerator heating zone, with improving the conditions for the safe conduct of the process, increasing the technical and economic indicators of the processes of dehydrogenation of paraffin hydrocarbons by reducing catalyst consumption, reducing air consumption for regeneration, increasing catalyst activity, stabilizing operation and expanding the possibilities for increasing the capacity of dehydrogenation units.

Claims (48)

1. Regenerator system for the dehydrogenation of paraffinic hydrocarbons C ₃ -C ₅ with a fluidized bed of a fine alumina-chromium catalyst, having a cylindrical body (1), an air supply pipeline (2) through a distributor (3) in the lower part of the fluidized bed, a fuel gas inlet pipeline (4) through the burner device (5) in the upper part of the fluidized bed, the transport pipe (7) for introducing into the upper part of the fluidized bed a gas suspension from the catalyst exhausted in the reactor and transport air (46), sectioning grids (8) located along the height of the fluidized bed, containing at this is the catalyst heating zone (9) by burning the fuel gas supplied to the burner (5) and burning coke from the catalyst in the upper part of the fluidized bed, the zone of catalyst oxidation and desorption of oxidation products (10) by the air supplied to the regenerator in the lower part of the fluidized bed above the distributor air (3), as well as a glass of reduction-desorption preparation of the catalyst (11) at the bottom regenerator body (1), having overflow openings (20) in the upper part for the catalyst flow from the regenerator to the reducing glass (11), distributors (13), (14) for supplying the reducing gas through the pipeline (15), respectively, and inert gas through the pipeline (16), partitioning grids (12) located along the height of the reducing glass (11), a gas pipe (22) for removing exhaust gases from the catalyst preparation to the upper part of the fluidized bed of the regenerator, attached to the upper cover (21) of the glass - reducing agent (11), and a branch pipe (17) in the lower part of the reducing glass (11) for the output of the regenerated and prepared catalyst to the reactor through the pipeline (42), as well as the branch pipe for the outlet of regeneration gases (55) in the upper part of the body (1) of the regenerator , characterized in that in the heating zone of the catalyst (9) there is a burner device (31) for afterburning the exhaust gases of the preparation of the catalyst (39), containing a gas pipe (22) with an open upper end ( 64) directed upwards, mounted on the upper end (64) of the gas pipe (22), the first disk (23), surrounding the opening of the gas pipe (22), and the second disk (24), located at some distance upwards from the first disk (23) and rigidly connected to it with the formation of an open annular space (25) between the disks (23), (24), while the burner device (31) has a distributing chamber (26), (43) connected to the air inlet pipeline (28), made in the form of a distributing pipe (27) attached to the second disk (24) and located coaxially inside the gas pipe (22) or in the form of an annular box (47) surrounding the gas pipe (22), with the distributing chambers (26), (43) have, respectively, in the wall of the distributing pipe (27) or in the wall of the gas pipe (22) located below the first disk (23) of the burner device (31) dosing holes (29), (45) for air inlet into the exhaust gas flow of catalyst preparation ( 39) with the formation of a gas pipe section (22) between doses openings (29), (45) and the first disk (23) of the burner device (31) of the annular channel (50) or cylindrical channel (37), which is a mixing chamber for pre-mixing the exhaust gases of catalyst preparation and the air supplied through the pipeline (28) . 2. The regenerator according to claim 1, characterized in that the burner device (31) with an annular channel (50) contains a cone-divider (49) attached with its base to the lower end of the distributing pipe (27) of the distributing chamber (26) with a top, downward. 3. The regenerator according to claim 1, characterized in that the burner device (31) with a cylindrical channel (37) contains a cone-reflector (6) attached with its base to the second disk (24), and the cone-reflector (6) is directed by the top down and centered above the gas pipe opening (22). 4. The regenerator according to claim 1, characterized in that in the burner device (31), which has a distribution chamber (43) connected to the air inlet pipeline (28), made in the form of an annular box (47) surrounding the gas pipe (22), having in the wall of the gas pipe (22) metering holes (45) located below the first disk (23) of the burner device (31) for air inlet into the exhaust gas flow of catalyst preparation (39), the transport pipe (7) is located coaxially inside the gas pipe (22 ) with the formation of an annular channel (50) between the pipes, which is a mixing chamber for pre-mixing the exhaust gases of catalyst preparation (39) and air supplied through the pipeline (28), while the transport pipe (7) passes the second disk (24) in its central part with the location of the upper open end (63) of the transport pipe (7), equipped with a catalyst and transport air distributor (40), above or below the level of the fluidized bed (38). 5. The regenerator according to claim 1, characterized in that the metering holes (29), (45) for air inlet into the exhaust gas stream of catalyst preparation (39) are located below the first disk (23) at a distance from it of at least 40 ⋅d, where d is the diameter of one dosing hole (29), (45). 6. The regenerator according to claim 1, characterized in that in the upper cover (21) of the reducing glass (11) and/or in the gas pipe (22) there are fittings (41) for introducing purge air into the gas pipe (22). 7. The regenerator according to claim 1, characterized in that the burner device (31) for afterburning the exhaust gases of the preparation of the catalyst (39) contains a cone-reflector (6) attached with its base to the second disk (24), and the cone-reflector (6 ) is directed with its top down and installed in the center above the opening of the gas pipe (22) or transport pipe (7) for introducing gas suspension from the catalyst spent in the reactor and transport air (46). 8. The regenerator according to claim 1, characterized in that the first disk (23) of the burner device (31) for afterburning the exhaust gases of the catalyst preparation (39) is installed horizontally. 9. The regenerator according to claim 1, characterized in that the first disk (23) of the burner device (31) for afterburning the exhaust gases of catalyst preparation (39) has the shape of a truncated cone with the inclination of the generatrix of the cone at an angle ranging from 30° down from the horizontal position up to 30° up from horizontal. 10. The regenerator according to claim 1, characterized in that the second disk (24) of the burner device (31) for afterburning the exhaust gases of the catalyst preparation (39) is installed horizontally. 11. The regenerator according to claim 1, characterized in that the second disk (24) of the burner device (31) for afterburning the exhaust gases of catalyst preparation (39) has the shape of a cone or a truncated cone with the inclination of the generatrix of the cone at an angle in the range from 30° upwards from horizontal position up to 45° down from the horizontal position and is installed with its top down or up in the center above the opening of the transport pipe (7) for introducing gas suspension from the catalyst exhausted in the reactor and transport air (46). 12. The regenerator according to claim 1, characterized in that the ratio of the diameter of the first disk (23) of the burner device (31) for afterburning the exhaust gases of catalyst preparation (39) to the diameter of the body (1) of the regenerator is in the range of values from 0.1 to 0 ,3. 13. The regenerator according to claim 1, characterized in that in the burner (31) for afterburning the exhaust gases of the preparation of the catalyst (39), the ratio of the diameter of the first disk (23) to the diameter of the second disk (24) is in the range of values from 0.8 to 1.25. 14. The regenerator according to claim 1, characterized in that the ratio of the diameter of the base of the reflective cone (6) to the diameter of the opening of the transport pipe (7) is in the range of values from 0.3 to 1.0. 15. The regenerator according to claim. 1, characterized in that the second disk (24) is rigidly connected to the first disk (23) using partitions (34). 16. Regenerator according to claim 15, characterized in that the number of partitions (34) is in the range from 3 to 12. 17. The regenerator according to claim 15, characterized in that the partitions (34) are evenly distributed around the circumference of the disks (23), (24), dividing the open annular space (25) into independent flow channels (51). 18. Regenerator according to claim 15, characterized in that the baffles (34) are flat radially directed plates. 19. The regenerator according to claim 1, characterized in that the partitioning grids (32) in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst (9) by burning fuel gas and burning coke, have a free cross section larger than the sectioning grids (8) in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst (10) supplied to the regenerator by oxygen-containing gas. 20. The regenerator according to claim. 1, characterized in that the distance between the partitioning grates (32) in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst (9) by burning fuel gas and burning coke, is greater than the distance between the partitioning grates (8 ) in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst (10) by the supplied oxygen-containing gas. 21. The regenerator according to claim 1, characterized in that the burner device (31) is located below the level of the fluidized bed (38) above or below one or more upper partition grates (32). 22. The regenerator according to claim 1, characterized in that below the main air distributor (3) under the holes (20) for the flow of the circulating catalyst from the regenerator into the reducing glass (11) there is an additional air distributor (30). 23. The regenerator according to claim 1, characterized in that the main air distributor (3) is located above or below the holes (20) for the overflow of the circulating catalyst from the regenerator to the reducing glass (11). 24. The regenerator according to claim 1, characterized in that between the distributors of the reducing gas (13) and nitrogen as an inert gas (14) in the reducing glass (11) additional grids (67) are installed. 25. Regenerator system for the dehydrogenation of paraffinic hydrocarbons С ₃ -С ₅ with a fluidized bed of a finely dispersed alumina-chromium catalyst, including a cylindrical body (1), a pipeline (2) for supplying oxygen-containing gas through the main distributor (3) in the lower part of the fluidized bed, a fuel gas inlet pipeline ( 4) through the burner device (5) in the upper part of the fluidized bed, the transport pipe (7) for introducing into the upper part of the fluidized bed a gas suspension from the catalyst exhausted in the reactor and transport air (46), sectioning grids (8), dividing the fluidized bed into sections , arranged in series from top to bottom, a catalyst heating zone (9) by burning the fuel gas supplied to the burner (5) and burning coke from the catalyst in the upper part of the fluidized bed, and a catalyst oxidation zone and desorption of oxidation products (10) by oxygen-containing gas supplied to the regenerator in lower part of the fluidized bed above the main distributor (3) oxygen-containing its gas, which also contains a cup for reduction-desorption preparation of the catalyst (11) built into the lower part of the regenerator body (1) with a fluidized bed, partitioned by gratings (12), having distributors (13), (14) in the lower part, connected to pipelines, respectively for introducing the reducing gas (15) and inert gas (16), as well as a branch pipe (17) for withdrawing the regenerated catalyst through the pipeline (42) into the reactor, located in the upper part of the reducing glass (11) chamber (18) for collecting waste gases of reduction-desorption preparation of the catalyst, consisting of a cylindrical shell (19) with holes (20) for the overflow of the circulating catalyst from the regenerator into the reducing glass (11) and a top cover (21) in the form of a truncated cone with a large base adjacent to the upper edge cylindrical shell (19), and with a smaller base pointing upwards, to which a gas pipe (22) is attached to remove the off-gases of the preparation catalyst into the upper part of the fluidized bed of the regenerator, the regeneration gas outlet pipeline (52) through the branch pipe (55) in the upper part of the regenerator body (1), characterized in that the regenerator includes a burner device (58) for afterburning the exhaust gases of catalyst preparation, including a transport pipe (7) located inside the gas pipe (22) in such a way that the upper end (63) of the transport pipe (7) is located below the upper end (64) of the gas pipe (22) or that its upper end (63) of the transport pipe (7) is located in the fluidized bed in the heating zone of the catalyst (9) at the same level with the upper end (64) of the gas pipe (22), both pipes being installed coaxially with the body (1) of the regenerator to form an annular annulus (65), and on the upper end (64) of the gas pipe (22) the first disk (23) is installed, surrounding the opening of the gas pipe (22), and the second disk (24), located at some distance up from the first disk (23) and rigidly connected to it with a by creating an open annular space (25) between disks (23), (24), which is a mixing chamber for mixing exhaust gases of catalyst preparation (39) and gas suspension from the catalyst exhausted in the reactor and transport air (46). 26. The regenerator according to claim 25, characterized in that the burner device (58) for afterburning exhaust gases of catalyst preparation contains a third disk (61) surrounding the opening of the transport pipe (7) on its upper end (63), installed horizontally and having an external the diameter is smaller than the diameter of the opening of the gas pipe (22), forming between the specified third disk (61) and the gas pipe (22) an annular slot (62) for the inlet of the exhaust gases of the preparation of the catalyst (39) into the gas suspension flow from the catalyst exhausted in the reactor and the transport air ( 46). 27. The regenerator according to claim 25, characterized in that the upper part of the gas pipe (22) is made in the form of a narrowing, which is a truncated cone (59) with a smaller base directed upwards, which forms the upper end (64) of the gas pipe (22) and creates an annular slot (60) between the specified end and the transport pipe (7) for the inlet of exhaust gases of catalyst preparation (39) into the gas suspension flow from the catalyst exhausted in the reactor and transport air (46). 28. The regenerator according to claim 25, characterized in that the burner device (58) for afterburning the exhaust gases of catalyst preparation (39) contains a distributing chamber (43) connected to the pipeline for introducing additional air (28) in the form of a surrounding gas pipe (22) an annular box (47) having dosing holes (45) in the wall of the gas pipe (22) for air inlet into the exhaust gas flow of catalyst preparation (46), while forming an annular annular annular space (57) between these holes and the first disk (23) pre-mixing of the supplied air and exhaust gases of catalyst preparation (39). 29. The regenerator according to claim 25, characterized in that the metering holes (45) for air inlet into the exhaust gas flow of catalyst preparation (39) are located below the first disk (23) at a distance from it of at least 40⋅d, where d is the diameter of one dosing hole (45). 30. The regenerator according to claim 25, characterized in that in the upper cover (21) of the reducing glass (11) and / or in the gas pipe (22) there are fittings (41) for introducing purge air into the gas pipe (22). 31. The regenerator according to claim 25, characterized in that the burner device (58) for afterburning the exhaust gases of the preparation of the catalyst (39) contains a cone-reflector (6) attached with its base to the second disk (24), and the cone-reflector (6 ) is directed with its top down and installed in the center above the opening of the gas pipe (22) or transport pipe (7) for introducing gas suspension from the catalyst spent in the reactor and transport air (46). 32. The regenerator according to claim 25, characterized in that the first disk (23) of the burner device (58) for afterburning the exhaust gases of the catalyst preparation (39) is installed horizontally. 33. The regenerator according to claim 25, characterized in that the first disk (23) of the burner device (58) for afterburning the exhaust gases of catalyst preparation (39) has the shape of a truncated cone with the inclination of the generatrix of the cone at an angle in the range of 30° downward from the horizontal position up to 30° up from horizontal. 34. The regenerator according to claim 25, characterized in that the second disk (24) of the burner device (58) for afterburning the exhaust gases of catalyst preparation (39) is installed horizontally. 35. The regenerator according to claim 25, characterized in that the second disk (24) of the burner device (58) for afterburning the exhaust gases of catalyst preparation (39) has the shape of a cone or a truncated cone with the inclination of the generatrix of the cone at an angle in the range of 30° upward from horizontal position up to 45° down from the horizontal position and is installed with its top down or up in the center above the opening of the transport pipe (7) for introducing gas suspension from the catalyst exhausted in the reactor and transport air (46). 36. The regenerator according to claim 25, characterized in that the ratio of the diameter of the first disk (23) of the burner device (58) for afterburning the exhaust gases of the catalyst preparation (39) to the diameter of the regenerator body (1) is in the range of values from 0.1 to 0 ,3. 37. The regenerator according to claim 25, characterized in that in the burner device (58) for afterburning the exhaust gases of the preparation of the catalyst (39), the ratio of the diameter of the first disk (23) to the diameter of the second disk (24) is in the range of values from 0.8 to 1.25. 38. The regenerator according to claim 25, characterized in that the ratio of the diameter of the base of the reflective cone (6) to the diameter of the opening of the transport pipe (7) is in the range of values from 0.3 to 1.0. 39. The regenerator according to claim 25, characterized in that the second disk (24) is rigidly connected to the first disk (23) using partitions (34). 40. The regenerator according to claim 39, characterized in that the number of partitions (34) is in the range from 3 to 12. 41. The regenerator according to claim 39, characterized in that the partitions (34) are evenly distributed around the circumference of the disks (23), (24), dividing the open annular space (25) into independent flow channels (51). 42. The regenerator according to claim 39, characterized in that the partitions (34) are flat radially directed plates. 43. The regenerator according to claim 25, characterized in that the partitioning grids (32) in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst (9) by burning fuel gas and burning coke, have a free section larger than the sectioning grids (8) in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst (10) supplied to the regenerator by oxygen-containing gas. 44. The regenerator according to claim 25, characterized in that the distance between the partitioning grates (32) in the upper part of the fluidized bed of the regenerator, including the heating zone of the catalyst (9) by burning fuel gas and burning coke, is greater than the distance between the partitioning grates (8 ) in the lower part of the fluidized bed of the regenerator, including the zone of oxidation and desorption of the catalyst (10) by the supplied oxygen-containing gas. 45. The regenerator according to claim 25, characterized in that the burner device (58) is located below the level of the fluidized bed (38) above or below one or more upper partition grates (32). 46. The regenerator according to claim 25, characterized in that an additional air distributor (30) is located below the main air distributor (3) under the holes (20) for the flow of the circulating catalyst from the regenerator into the reducing glass (11). 47. The regenerator according to claim 46, characterized in that the main air distributor (3) is located above or below the holes (20) for the overflow of the circulating catalyst from the regenerator to the reducing glass (11). 48. The regenerator according to claim 25, characterized in that additional grids (67) are installed between the distributors of the reducing gas (13) and nitrogen as an inert gas (14) in the reducing glass (11).

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