WO2023009031A1

WO2023009031A1 - Regenerator for a с3-с5 paraffin dehydrogenation system (variants)

Info

Publication number: WO2023009031A1
Application number: PCT/RU2022/000202
Authority: WO
Inventors: Станислав Михайлович КОМАРОВ; Александра Станиславовна ХАРЧЕНКО
Original assignee: Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор"
Priority date: 2021-07-26
Filing date: 2022-06-28
Publication date: 2023-02-02

Abstract

Claimed is a regenerator for a C3-C5 paraffin dehydrogenation system, having a fluidized bed of a finely dispersed chromia-alumina catalyst, wherein, for more efficient afterburning of the combustible part of the products of the reduction-desorption preparation of the catalyst, a specific design for an afterburning burner device (31) is envisaged, together with the positioning thereof in the fluidized bed, as well as the layout of a catalyst heating zone (9) of the regenerator, said zone containing the afterburning burner device (31), partitioning grids (12), and a burner device (5) for burning a fuel gas supplied.

Description

REGENERATOR OF THE SYSTEM OF DEHYDROGENATION OF PARAFFIN HYDROCARBONS C ₃ -C ₅ (VERSIONS)

Technical field

The invention relates to the field of petrochemistry, in particular to installations for the dehydrogenation of C3-C5 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.

Prior Art

Typical installations for the dehydrogenation of paraffinic hydrocarbons (I. L. Kirpichnikov, V. V. Beresnev, L. M. Popov "Album of technological schemes of the main production facilities 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 disk 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 air transporting the catalyst, sectioning 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 cup for reduction-desorption preparation of a catalyst with a fluidized bed built into the lower part of the body, divided by gratings into sections, having in the lower part nozzles for inlet of reducing gas for catalyst reduction, inert gas for desorption of reduction products and a transport pipe for output of 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, N ° 5, p. 677, Tyuryaev I. Ya., “Theoretical foundations for the production of butadiene and isoprene by dehydrogenation methods”, Kyiv, “Naukova Dumka”, 1973, p. 153), comes out of the glass reductively - 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 treatment, 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 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 reduction-desorption preparation of the catalyst leads to incomplete combustion of the residual gas-reductant contained in the preparation products catalyst, its entry into the separation zone of the regenerator with a deterioration in the conditions for safe operation of the process, which requires an increase in the volume of the heating zone and, accordingly, the amount of catalyst loaded into the regenerator, which leads 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 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 a narrow channel of the gas pipe, which is accompanied by rapid clogging of the pipe with catalyst and practically leads to the operation of the analogue with the ingress 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 regime by increasing the consumption of the reducing gas and inert gas in the reduction-desorption preparation of the catalyst.

Disclosure of invention

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 aluminum-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 layer, the 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 exhausted catalyst in the reactor and the transport air 46, sectioning grids 8 located along the height of the fluidized bed, containing at the same time 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; - 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 overflow of the catalyst from the regenerator into 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 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 reducing glass And and a branch pipe 17 in the lower part of the reducing glass 11 for output to the reactor of the regenerated and prepared catalyst through pipeline 42, as well as the regeneration gas outlet pipe 55 in the upper part of the regenerator body 1, in which a burner device 31 can be installed in the heating zone of the catalyst 9 for afterburning the exhaust gases of catalyst preparation 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 between the disks 23, 24 open annulus 25 , while the burner device 31 has a distribution chamber 26, 43 connected to the air inlet pipeline 28, made in the form of a distribution 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, moreover, 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 stream catalyst preparation gases 39 with the formation of an annular channel 50 or a cylindrical channel 37 in the section of the gas pipe 22 between the metering holes 29, 45 and the first disk 23 of the burner device 31, which is a mixing chamber for pre-mixing the exhaust gases of the catalyst preparation and air supplied through the pipeline 28.

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 apex 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 C3-C5 paraffinic hydrocarbon dehydrogenation system with a fluidized bed of a finely dispersed aluminum-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 part of the fluidized bed. layer, 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 separating the boiling a layer 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 zone for oxidizing the catalyst and desorbing the oxidation products 10 with oxygen-containing gas supplied to the regenerator in the lower part of the fluidized bed layer above the main distributor 3 of oxygen-containing gas, which also contains a glass built into the lower part of the body 1 of the regenerator for the recovery-desorption preparation of the catalyst 11 with a fluidized bed, partitioned by grids 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 outputting the regenerated catalyst through pipeline 42 to the reactor, located in the upper part of the reducing glass 11, chamber 18 for collecting off-gases of the reduction-desorption preparation of the catalyst, consisting of qi a cylindrical shell 19 with holes 20 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 with a large base adjacent to the upper edge of the cylindrical shell 19 and with a smaller base directed upwards, to which the gas pipe 22 is connected for exhaust gases of catalyst preparation to the upper part of the fluidized bed of the regenerator, 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 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 a 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 t the 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 him with the formation of an open annular space 25 between the disks 23, 24, which is a mixing chamber for mixing the exhaust gases of the preparation catalyst 39 and gas suspension from the spent catalyst in the reactor and transport air 46.

The burner device 58 for afterburning the exhaust gases of 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 smaller 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 device 58 for afterburning the exhaust gases of the preparation of the catalyst may contain 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 exhaust gas stream preparation of the catalyst 46, thus forming between the said holes and the first disk 23 an annular annulus 57 for preliminary 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 by the top down and installed in the center above the opening of the gas pipe 22 or the transport pipe 7 to enter the gas suspension from the spent catalyst in the reactor and transport air 46.

The first disk 23 of the burner of the internal 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 be in the range of 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 range from 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 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.

C ₃ -C ₅ paraffinic hydrocarbons, 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, can be used as feedstock for dehydrogenation plants. .

When implementing the proposed method of catalyst regeneration, an aluminum-chromium catalyst containing SG2O3 - 13.0-25.0 wt.%, K2O - 1.0-3.0 wt.%, S1O2 - 1.0- 10.0 wt.%, AI2O3 - the rest, with the content in the oxidized state of CrO3 - 0.25-3.5 wt.%. For example, an industrial catalyst of the AOK-73-24 type. Spent catalyst is understood to mean 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.%, can be used as a fuel gas and a reducing gas. 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.

Brief description of the figures of the drawings

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

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

The regenerator shown in figure 1 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 spent in the reactor and transport air , partitioning grids 8, 32, catalyst heating zone 9, zone of catalyst oxidation and desorption of oxidation products 10, unit for reduction-desorption preparation of catalyst 11 in the form of a cup built into the lower part of 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 upper 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 device 31, shown in figure 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 up from the first disk 23 and rigidly connected to him (Fig.2) using radially directed partitions 34 (not shown in Fig.1) with the formation between the disks 23, 24 of an open annular space 25. As shown in Fig.2 (section along A-A), the partitions 34 divide the open the annular space 25 on independent channels of the expiration of flows 51 (not shown in figure 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 the pipeline 28 for supplying air, attached to the second disk 24 and located inside the gas pipe 22 coaxially with it and having in the wall distributing pipe 27 metering holes 29 for air inlet into the exhaust gas flow of catalyst preparation. 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 disks 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 (figure 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.

The burners shown in FIGS. 2 and 3 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 variant of the burner device 31 shown in FIG. 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 disk 23 of the burner device 31. release into the fluidized bed. A cone-reflector 6 is attached to the second disk 24 of the burner device 31.

In the variant of the burner device 31 shown in Fig.3, 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 the preparation of the catalyst 39 and supplied through the pipeline 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 disks 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 provided with a distributor of catalyst and conveying air 40, above or below the level of the fluidized bed 38.

The regenerator shown in figure 4 according to the second variant contains a cylindrical body 1, an air supply pipeline 2 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 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 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 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 air distributor 3, which also contains a cup for reduction-desorption preparation of catalyst 11 with a fluidized bed, sectioned by grates 12, built into the lower part of the regenerator body 1, 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 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 of the regenerator into the reducing glass 11 and the top cover 21 in the form of a truncated cone with a large base connected to the cylindrical shell 19 and with a smaller base directed upwards to which a gas pipe 22 is connected to remove exhaust gases from the preparation of the catalyst to the upper part of the boiling its regenerator layer. The proposed regenerator is equipped with a combustion device 58 for the 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 a fluidized bed in the heating zone catalyst 9 is flush with the upper end 64 of the gas pipe 22, both pipes are installed coaxially with the regenerator body 1 to form an annular annular space 57, and the first disk 23 is 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 (Fig.5) using radially directed partitions 34 with the formation between the disks 23, 24 of an open annular space 25. As shown in Fig.5 (section along A- A), partitions 34 in the form of plates divide the open annular space 25 into independent flow channels 51. The burner 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 input additional air and having dosing holes 45 in the wall of the gas pipe 22 for the admission of additional air into a catalyst preparation off-gas stream; and an annular annulus 57 for pre-mixing the feed air and catalyst preparation off-gases. The final mixing of these streams is carried out during their passage in the open annular space 25 between the disks 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 smaller than the diameter of the opening of the gas pipe 22, forming between the specified disk and the gas pipe 22 an annular slot 62 for the inlet of exhaust gases of catalyst preparation into gas suspension flow from the catalyst and conveying air 46.

The gas pipe 22 shown in Fig.7 burner device, contains in the upper part of the 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 between the inner wall of the smaller base of the cone and a transport pipe 7 an annular slot 60 for the inlet of exhaust gases of catalyst preparation into the flow of catalyst gas suspension and transport air 46.

In the burner device shown in FIG. 8, the upper end 63 of the transport pipe 7 is located below the upper end 64 of the gas pipe 22, forming between said upper ends 63, 64 a mixing chamber 66 of the exhaust gas streams of catalyst preparation and catalyst gas suspension and conveying air. The final mixing of these streams is carried out during their passage in the open annular space 25 between the disks 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 gas suspension of the catalyst and 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 coming 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 regenerator oxidation zone to trivalent after reduction of the catalyst in the reducing glass 11. At the same time, the content of hexavalent chromium in the oxidized catalyst was maintained in the range of 0.5-1.0 wt.%, typical for 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 excess supply of natural gas for catalyst recovery, which is 1.5-2.5, reaches 4-13% of the total thermal power of the regenerator heating zone with a corresponding decrease 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, CO2) and contain a large amount of reaction water to be removed from the system, which imposes additional requirements for the organization of afterburning of exhaust gases of catalyst preparation 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 (figure 1-3) according to the first variant works as follows. Air is supplied under the fluidized bed of the regenerator from collector 33 through pipeline 2 to the main distributor 3 and through pipeline 35 to the additional distributor 30. 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 through the fluidized bed 38 of the regenerator, partitioned by horizontal gratings 8 countercurrently to the descending circulating catalyst. For heating the circulating catalyst to provide heat for the endothermic dehydrogenation reaction through pipeline 4 to the upper part of the fluidized bed of the regenerator through the burner 5 located in the heating zone of the catalyst 9, fuel gas is supplied for combustion in the flow of air supplied to the regenerator with simultaneous burning of 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 capturing fine fractions carried away from the fluidized bed of the catalyst in cyclones (not shown in Fig.1, 2, 3) leave the regenerator. The flow of exhaust gases from the preparation of the catalyst, containing a significant part of the residual gas-reductant, is directed through the gas pipe 22 to afterburn the combustible part of the flow into the burner 31, where it is 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 catalyst preparation contain some of the catalyst captured from the collection chamber 18, pass as a gas suspension through the gas pipe 22, and enter in the upward flow mode into the annular channel 50 of the burner device 31. Said annular channel 50 is the 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 mixing of said 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 the 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 exits into 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 device 31 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 of the combustible part of the exhaust gases of the catalyst preparation at the exit from the open 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 outlet of the open annular space 25 ensures uniform distribution of the flame around the circumference of the discs and, in combination with a high intensity of processes heat and mass transfer 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 flame zone, stable and stable combustion, high speed 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. In this case, the heating zone of the catalyst 9, equipped with the existing burner 5, plays the role of the second stage of afterburning the exhaust gases of the catalyst preparation, ensuring the complete combustion of the latter. The interaction of the torch of the proposed burner device 31 afterburning with the existing burner device 5 combustion of supplied natural gas in the heating zone of the catalyst 9 increases the stability and stability of the burner.

The proposed regenerator (Fig.4-8) according to the second version works as follows. Air is supplied 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. 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 grates 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 device 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 catalyst heating zone 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 into beaker-reductant 11 recovery-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 capturing 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 cyclones 53 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 metering holes 45 into the exhaust gas flow of the catalyst preparation, 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 amount of 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 rate of exhaust gases of catalyst preparation when they are introduced into the stream of catalyst gas suspension and carrier gas in the initial section of the open annular space 25 by installing the third disk 61 or narrowing in the form of a truncated cone 59 of the gas pipe 22 (Fig.6 and 7). On Fig shows a variant of improving 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. 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 outflow 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 flow delay 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 rate of gas outflow 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. The uniform distribution of the gas-air mixture achieved using the invention and of the captured catalyst around the circumference of the 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, high the 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 a high efficiency of the burner 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. At the same time, the heating zone of the catalyst 9, equipped with a standard burner, plays the role of the second stage of exhaust gases of the catalyst preparation, ensuring the complete combustion of the latter. When the flame 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, accordingly, to increase the activity of the regenerated catalyst.

When using the proposed design of the regenerator, the efficiency of the 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 is improved, with the improvement of the conditions for safe conduct of the process 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 consumption 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 a catalyst and, accordingly, to stabilize the operation of the regenerator in the optimal mode after the exhaust gases of the 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 into 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 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 of additional grids 67 between the reducer gas distributors 13 and nitrogen 14 in the reducer beaker 11 increases the heat and mass transfer in this zone and, accordingly, the efficiency of catalyst desorption by the supplied nitrogen before the catalyst is released 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.

Industrial Applicability

The proposed regenerator can find application in the field of petrochemistry, in 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.

Table 1.

Claims

CLAIM

1. Regenerator system for the dehydrogenation of paraffinic hydrocarbons СЗ-С ₅ with a fluidized bed of a finely dispersed aluminum-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 a burner device (5) in the upper part 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), sectioning grids (8) located along the height of the fluidized bed, containing at the same time 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 air supplied to the regenerator 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 and the body (1) of the regenerator, having overflow holes (20) in the upper part for the overflow of the catalyst from the regenerator into 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) located along the height of the reducing vessel (11), a gas pipe (22) for removing exhaust gases from catalyst preparation to the upper part of the fluidized bed of the regenerator, connected to the upper cover (21) of the reducing vessel (11) and branch pipe (17) in the lower part of the reductant vessel (11) for the output of the regenerated and prepared catalyst into the reactor through the pipeline (42), as well as the regeneration gas outlet pipe (55) in the upper part of the regenerator housing (1), characterized in that in the catalyst heating zone ( 9) a burner device (31) is installed for afterburning the exhaust gases of catalyst preparation (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 up from the first disk (23) and rigidly connected to it with the formation between the disks (23), (24) of an open ring open space (25), while the burner device (31) is connected to the pipeline for air inlet (28) distributing chamber (26), (43), 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 gas pipe (22) surrounding box (47), moreover, 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 flow of exhaust gases of catalyst preparation (39) with the formation of an annular channel ( 50) or a 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 splitter cone (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 reflective cone (6) attached with its base to the second disk (24), and the reflective cone (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 flow of exhaust gases 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 distributor catalyst and conveying air (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 flow of the 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 metering 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 (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 exhaust gases of catalyst preparation

(39) 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 in the range of 30° downward 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 the preparation of the catalyst (39) has the shape of a cone or a truncated cone with an inclination of the generatrix of the cone at an angle in the range of 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 surviving the exhaust gases of the preparation of the catalyst (39) to the diameter of the body (1) of the regenerator is in the range from 0.1 to 0 ,3.

13. The regenerator according to claim 1, characterized in that in the burner device (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. Regenerator according to claim 15, characterized in that the baffles (34) are evenly distributed around the circumference of the disks (23), (24), dividing the open annular space (25) into independent flow channels (51).

18. Distributor 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 sectioning 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 sectioning 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 (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 overflow 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 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).

25. Regenerator system for the dehydrogenation of paraffinic hydrocarbons СЗ-С ₅ with a fluidized bed of a finely dispersed aluminum-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, located sequentially from top to bottom, 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 and the zone of catalyst oxidation and desorption of oxidation products (10) by oxygen-containing gas supplied to the regenerator in the lower part of the fluidized bed above the main distributor (3) oxygen-containing th 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 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 into the reducing glass (11) and the 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 of the regenerator; upper part of the body (1) of the regenerator, characterized in that the regenerator includes a burner (58) for afterburning 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) is 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), and both pipes are 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 formation of 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 the 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 an annular slot (62) between the specified third disk (61) and the gas pipe (22) 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).

27. The regenerator according to claim 5, 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 from the preparation of the catalyst (39) into the flow of gas suspension from the spent in the reactor catalyst and conveying 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 annulus between the said holes and the first disk (23) ( 57) 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 metering hole (45).

30. The regenerator according to claim 25, characterized in that in the upper cover (21) of the reducing glass (I) 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 combustion device (58) for afterburning the exhaust gases of catalyst preparation (39) is installed horizontally.

33. The regenerator according to claim 25, characterized in that the first disk (23) of the burner of the internal device (58) for afterburning the exhaust gases of the preparation of the catalyst (39) has the shape of a truncated cone with an inclination of the generatrix of the cone at an angle of range from 30° down from horizontal 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 surviving 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 the catalyst preparation (39) has the shape of a cone or a truncated cone with an 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 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.

37. The regenerator according to claim 25, characterized in that in the burner (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 baffles (34).

40. 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. Distributor according to claim 39, characterized in that the baffles (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 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.

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 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), an additional air distributor (30) is located.

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 gratings (67) are installed between the distributors of the reducing gas (13) and nitrogen as an inert gas (14) in the reducing glass (11).