RU2838720C1 - Blade swirler for reaction component for fixed catalyst bed reactor, fixed catalyst bed reactor and method of operation thereof - Google Patents

Abstract

FIELD: mechanical engineering.

SUBSTANCE: group of inventions relates to a blade swirler for a reaction component for a fixed catalyst bed reactor, a fixed catalyst bed reactor comprising a blade swirler and a reactor operation method. Blade swirler comprises a cylindrically oriented part with blades on the outer surface, wherein the part has an axial through channel with a hydraulic resistance means for the reaction component, which comprises a partition, the ratio of the distance from the location of the partition to the inlet section of the through channel to the length of the through channel is from 0.1 to 0.9. Reactor comprises reaction components feed unit with blade swirler. Method is carried out through operation of said reactor.

EFFECT: higher efficiency and reliability of operation of swirler and reactor with fixed bed of catalyst due to increased intensity of vortex formation and mixing of reaction components at required distance from outlet of blade swirler.

20 cl, 6 dwg, 1 tbl, 1 ex

Description

Field of technology

The group of inventions relates to blade swirlers for reaction components used in fixed-bed catalyst reactors, to fixed-bed catalyst reactors that can be used to carry out various catalytic processes, such as steam-air or steam-oxygen reforming of hydrocarbons, and to methods for operating such reactors.

State of the art

The prior art discloses a vane swirler for a fixed-bed catalyst reactor, a fixed-bed catalyst reactor, and a method for operating the same (RU 2385289 C2, published 27.03.2010). The reactor is used for secondary catalytic reforming of hydrocarbons, it comprises a housing with a reaction component input unit, which includes a channel for an oxidizing component and a channel for a fuel component, and a reaction zone that includes a catalyst layer. A vane swirler is installed in the channel for the oxidizing component of the reaction, which is a certain part with vanes. The reaction components are fed to the input unit through the corresponding channels, while the oxidizing component is fed through the vane swirler.

A vane swirler for a fixed-bed reactor, a fixed-bed reactor and a method for its operation (EA 029571 B1, published on 30.04.2018) were selected as a prototype. The reactor is used for secondary catalytic reforming of hydrocarbons, it contains a housing with a reaction component input unit and a reaction zone including a catalyst bed. The said input unit includes a channel for the oxidizing component of the reaction and a channel for the fuel component. A vane swirler is installed in the channel for the oxidizing component, which is a part oriented in the shape of a cylinder with vanes on the outer surface. The reaction components are fed to the input unit through the corresponding channels, while the oxidizing component is fed through the vane swirler.

The disadvantages of the known solutions are in the design and shape of the blade swirlers. The channels for the oxidizing component of the reaction have increased hydraulic resistance due to the placement of swirlers of a standard design in them, in addition, the known swirlers at the design stage have a limited set of capabilities for creating an intensive vortex formation zone at a constant distance from them and, accordingly, a zone of stable mixing of the reaction components. The incorrect shape of the swirler and the height of mixing of the components above the catalyst bed lead to an unstable high-temperature reaction and, consequently, to incomplete reactions and inefficient operation of the plant, as well as to premature wear and damage to the lining of the reactor and the swirler itself. To eliminate such risks, it is necessary to make significant changes to the design of the reactor, the reaction component input unit, or adjust the flow parameters of at least one reaction component.

Disclosure of the essence of the group of inventions

The objective of the inventions is to create a blade swirler for a fixed-bed catalyst reactor, a fixed-bed catalyst reactor and a method for its operation that is free from the above-mentioned disadvantages.

The technical result of the group of inventions consists in increasing the efficiency and reliability of the operation of the swirler and the reactor with a fixed catalyst bed by providing increased intensity of vortex formation and mixing of reaction components at the required distance from the outlet of the blade swirler used for at least one reaction component.

To solve the specified problem and achieve the stated technical result, a blade swirler for a reaction component for a reactor with a fixed catalyst bed is proposed, containing a part oriented in the shape of a cylinder with blades on the outer surface.

In this case, the part has an axial through channel with a means of hydraulic resistance for the specified reaction component.

This design allows achieving high efficiency and reliability of the swirler and fixed-bed reactor and creating a stable zone of swirling and mixing of reaction components at a constant and required distance from the blade swirler, with the specific distance depending on the hydraulic resistance used in the channel for the specified flow.

The through channel allows to create a short path for the flow of the reaction component passing through it, accelerating its passage through the swirler, and the means of hydraulic resistance in the channel allows to slow down a part of the flow passing through this channel, which makes it possible during design and development to more accurately adjust and set the zone of intensive vortex formation and mixing of reaction components at the required distance from the swirler without significantly changing the design of the reactor, the unit for introducing reaction components or the parameters of the flow of the reaction component. Thus, a part of the flow going through the channel passes the swirler faster than the flow going along the blades, and the means of hydraulic resistance allows to precisely adjust the flow speed in the channel so that, breaking out of the swirler, it takes away the flow swirled by the blades to the required distance from the swirler for better mixing.

The hydraulic resistance means may be any means known from the prior art that allows creating hydraulic resistance (obstacle) to the flow of a fluid medium in the form of a reaction component passing through a channel: a protrusion, a narrowing, a partition, etc. It should be noted that the reaction component is understood to mean any fluid medium that is fed into the reactor, with any composition, including containing inert elements.

Mostly the blades have a rotation angle from 60 to 360 degrees.

The above parameters allow achieving higher efficiency and reliability of the swirler and reactor. In the specified range of the blade rotation angle, the reaction component is swirled more efficiently and stably, which means that the intensity of vortex formation and the quality of mixing of the components become even higher and it is possible to set the distance of the vortex formation zone from the exit of the blade swirler more accurately.

Preferably, the through channel has a variable diameter along the length of the through channel.

The above parameters allow achieving higher efficiency and reliability of the swirler and reactor. Using a variable diameter through channel allows better variation of the speed of passage of a part of the reaction component flow through this channel and creating the necessary and constant distance of the vortex formation zone and mixing of components.

By variable diameter along the length of the through channel it is meant that the through channel at different points along its length can have different diameters, for example, at the entrance to the through channel its diameter can be D1, at some distance from the entrance the diameter of the through channel can be D2, while, for example, D1< D2. This allows for the necessary and constant distance of the vortex formation zone and mixing of components from the exit of the swirler.

Preferably, the hydraulic resistance means comprises at least one partition.

The use of one or more of the described partitions contributes to a better achievement of the above technical result depending on the type of reaction component, its parameters and the area of application of the reactor.

Preferably, at least one partition is installed at the entrance to the through channel.

The placement of a partition at the entrance to the through channel allows for higher efficiency and reliability of the swirler and reactor operation, as it allows for a reduction in the flow area of the channel and a more accurate setting of the flow rate of the reaction component in order to ensure the necessary and constant distance from the exit of the swirler of the zone of intense vortex formation and mixing of the reaction components.

Preferably, at least one partition has openings.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it allows reducing the flow cross-section of the channel and more accurately setting the speed of the reaction component flow, as well as uniformly distributing this flow over the cross-section of the through channel in order to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the exit from the blade swirler.

Preferably, at least one partition is a washer containing a hole coaxial with the through channel.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it allows reducing the flow cross-section of the channel and more accurately setting the speed of the reaction component flow, as well as directing this flow at the entrance along the center of the through channel in order to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the exit from the blade swirler.

Preferably, the ratio of the diameter of the washer hole to the diameter of the through channel at the location where the washer is installed is from 0.8 to 0.2, preferably from 0.40 to 0.55.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

Preferably, at least one partition is a plate with openings located along the perimeter of the plate symmetrically relative to the axis of the through channel.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it allows reducing the flow cross-section of the channel and more accurately setting the speed of the reaction component flow, as well as uniformly distributing the flow over the cross-section of the through channel to ensure increased intensity of vortex formation and mixing of reaction components at the required and constant distance from the exit of the blade swirler.

Preferably, at least one partition covers from 20 to 80% of the cross-sectional area of the through channel at the location of the partition installation.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

Preferably, the ratio of the distance from the location of at least one partition to the inlet section of the through channel to the length of the through channel is from 0.1 to 0.9, preferably from 0.2 to 0.5, more preferably from 0.25 to 0.30.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

The inlet section is understood to be the cross-section of the through channel at the point of entry into the through channel.

Preferably, the ratio of the distance from the location of at least one partition to the inlet section of the through channel to the length of the through channel is from 0.5 to 0.8.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

Each of the above-described preferred embodiments of at least one partition contributes to a better achievement of the technical result depending on the type of reaction component, its parameters and the field of application of the reactor. A person skilled in the art will understand the use of any of the presented variants for a higher intensity of vortex formation and mixing of reaction components at the required distance.

Preferably, the ratio of the length of the through channel to the diameter of its inlet section is from 2 to 7, preferably from 4 to 5.

These ratios more accurately allow one to set the required distance of the zone of increased vortex formation and mixing of reaction components for the flow of the reaction component and to ensure the constancy of this distance under conditions determined by the specialist.

Preferably, the hydraulic resistance means comprises

a washer containing a hole coaxial with the through channel,

and a plate with holes located along the perimeter of the plate symmetrically relative to the axis of the through channel.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it allows reducing the flow cross-section of the channel and more accurately setting the speed of the reaction component flow, as well as uniformly distributing the flow over the cross-section of the through channel to ensure increased intensity of vortex formation and mixing of reaction components at the required and constant distance from the exit of the blade swirler.

More preferably, the washer is installed at the entrance to the through channel, wherein the ratio of the diameter of the washer opening to the diameter of the through channel at its entrance is from 0.8 to 0.2, preferably from 0.40 to 0.55,

and the ratio of the distance from the location of the plate with holes to the inlet section of the through channel to the length of the through channel is from 0.1 to 0.9, preferably from 0.2 to 0.5, more preferably from 0.25 to 0.30.

This allows achieving higher efficiency and reliability of the swirler and reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

The above embodiments best contribute to achieving the technical result, since the washer with one coaxial hole allows locally narrowing the through channel and slowing down the flow of the reaction component, and the plate with symmetrical holes relative to the channel axis not only additionally slows down this flow, but also breaks it into parts, simplifying their vortex formation and mixing of the reaction components at a distance from the outlet of the swirler. The flow of the reaction component is thus slowed down and swirled in an accurate and predictable manner. In this case, for the declared parameters of the washer hole and the location of the plate, the technical result is achieved even more effectively.

Also, to solve the above-mentioned problem and achieve the stated technical result, a reactor with a fixed catalyst bed is proposed, containing a reaction component input unit, wherein a blade swirler is installed in the input unit for the reaction component according to any of the above-described preferred options.

This reactor allows achieving higher efficiency and reliability of operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

Preferably, the reactor is a secondary reformer.

The proposed technical solution allows achieving higher efficiency and reliability of operation in a reactor with a fixed catalyst bed, which is a secondary reforming apparatus.

Preferably, the reaction component input unit comprises a channel for the oxidizing component, wherein the swirler is installed in this channel, and/or

the reaction component input unit contains a channel for the fuel component, and the swirler is installed in this channel.

This allows for higher efficiency and reliability of reactor operation, as it creates optimal conditions for ensuring increased intensity of vortex formation and mixing of reaction components at the required and constant distance from the outlet of the blade swirler.

Preferably, the ratio of the distance from the outlet section of the through channel to the outlet section of the channel for the oxidizing component to the height of the swirler is from 0 to 10, preferably from 5 to 8, more preferably from 5.1 to 5.6.

It is also preferable that the ratio of the distance from the outlet section of the through channel to the outlet section of the channel for the fuel component to the height of the swirler is from 0 to 10, preferably from 5 to 8, more preferably from 5.1 to 5.6.

The outlet section of the through channel is understood to be the cross-section of the through channel at the exit point from the through channel, and the outlet section of the channel for the oxidizing component is understood to be the cross-section of the channel for the oxidizing component at the exit point from this channel.

These ratios additionally improve the accuracy of setting the required distance of the zone of increased vortex formation and mixing of reaction components for the flow of the reaction component and ensure the constancy of this distance under conditions determined by the specialist.

Also, to solve the above-mentioned problem and achieve the claimed technical result, a method is proposed for operating a reactor with a fixed catalyst bed according to any of the above-described preferred embodiments, containing a reaction component input unit and a blade swirler installed therein for the reaction component, and including stages at which reaction components are fed into the input unit,

at the same time, at least one component is fed through a vane swirler.

This method allows achieving higher efficiency and reliability of the reactor operation, as it creates an optimal speed mode for the flow of the reaction component to ensure increased intensity of vortex formation and mixing of the reaction components at the required and constant distance from the outlet of the blade swirler.

Thus, a group of inventions is proposed, namely a method (method of reactor operation) and a product (reactor or swirler) developed for implementing this method (reactor) or one of its actions (swirler), while a combination is presented with the subject of the invention as a whole (reactor) and a part of the whole (swirler).

Brief description of the drawings

The best embodiment of the inventions is illustrated graphically by Figures 1-6 and described in detail below. The general case of implementing the claimed solution includes the preferred embodiment, but is not limited to it.

Fig. 1 shows a schematic diagram of a fixed bed catalyst reactor.

Fig. 2 schematically shows a blade swirler with a washer and a plate with holes, installed in a channel for the oxidizing component of the reaction, a side view with a section.

Fig. 3 schematically shows the external appearance of a vane swirler with a washer installed at the entrance to the through channel.

Fig. 4 schematically shows a blade swirler with a washer and a plate with holes, a side view with a section.

Fig. 5 schematically shows a vane swirler with a washer installed at the entrance to the through channel, top view.

Fig. 6 schematically shows a horizontal section of a blade swirler at the location where a plate with holes is installed in the through channel.

All figures show diagrams and are not drawings.

The positions in Fig. 1-6 indicate:

100 - fixed bed reactor;

101 - reaction component input unit;

102 - reactor zone 100 with a fixed catalyst bed;

103 - reaction product outlet unit;

10 - blade swirler for the reaction component;

1 - a part oriented according to the shape of a cylinder;

2 - axial through channel of part 1;

3 - blades on the outer surface of part 1;

4 - a partition in the form of a washer;

5 - a partition, which is a plate with holes;

51 - holes of plate 5;

6 - a channel for supplying a reaction component, in which a swirler 10 is installed;

d1 - diameter of the hole in washer 4;

D - diameter of through channel 2;

L - length of through channel 2;

l is the distance from the location of plate 5 to the inlet section of channel 2;

H is the distance from the outlet section of the through channel 2 to the outlet section of the channel for the oxidizing component;

Y - angle of rotation of the blades.

Implementation of inventions

The proposed group of inventions can be used to implement various catalytic processes, preferably hydrocarbon reforming processes for the purpose of obtaining synthesis gas, steam-air or steam-oxygen reforming of hydrocarbons, but can be used for other processes known to a specialist from the prior art.

The method of operation of the reactor 100 with a fixed catalyst bed is carried out by means of a reactor 100 developed for this purpose, and the blade swirler 10 is part of this reactor 100. The following is a description of preferred examples of the implementation of the group of inventions.

The claimed reactor 100 with a fixed catalyst bed (Fig. 1-2) generally has a zone for introducing reaction components with a corresponding unit 101, a zone 102 with a catalyst, and a zone for removing reaction products 103. Such a reactor 100 can be an adiabatic shaft-type installation used, for example, for reforming hydrocarbons in the form of a secondary reforming apparatus in technologies for producing ammonia, hydrogen, methanol, and others. A person skilled in the art will understand the various areas of application of the proposed reactor.

The reactor 100 includes a reaction component input unit 101, which may contain, for example, a channel 6 for an oxidizing reaction component and a channel for a fuel reaction component and/or a channel for another component (not shown). In one of these channels or in each of them, a vane swirler 10 is installed for the corresponding reaction component. In this case, the ratio of the distance H from the outlet section of the through channel to the outlet section of the channel for the reaction component, for example, oxidizing, to the length L of the through channel (H/L) is from 0 to 10, preferably from 5 to 8, more preferably from 5.1 to 5.6.

In the general case, the vane swirler 10 (Fig. 3-6) comprises a part 1 oriented in the shape of a cylinder made of any material, preferably a metal alloy. Part 1 has an axial through channel 2 and vanes 3 on the outer surface, the number of which can be any, for example, from two to twenty. Vanes 3 are connected to the outer surface of part 1 by any known method, preferably welded, or can be made in the form of a single monolithic structure with part 1. Vanes 3 can have any angle of rotation Y (Fig. 3), preferably the angle is from 60 to 360 degrees. The ratio of the length L of the through channel 2 to the diameter D of its inlet section is preferably from 2 to 7, more preferably from 4 to 5. Channel 2 can have a round or polygonal shape with the same or variable diameter along the length of the channel, i.e. at the entrance to channel 2 it will have one diameter D1, and at some distance from the said entrance the channel will have a different diameter D2, wherein D2 is greater or less than D1. The transition from a smaller diameter to a larger one and vice versa can be smooth or abrupt, as when placing a certain narrowing thin insert.

In general, both the through channel 2 and the blades 3 are manufactured in various shapes and sizes, selected by a specialist depending on the type of reactor 100 and the parameters of the reaction components.

The axial through channel 2 has a means of hydraulic resistance for the same flow of the reaction component for which the swirler 10 is used. The means of hydraulic resistance can be made in the form of any known one or more elements capable of slowing down and/or adjusting the flow rate. In advantageous embodiments, each element used is a partition with an axisymmetric design, for example, the partition can be in the form of a flat solid plate blocking a part of the channel 2 in the center of the cross-section, or the partition can be the entire channel 2 and have openings located symmetrically relative to the axis of the through channel 2, or one opening coaxial with the channel 2. In this case, it is obvious that the area of the upper surface of each of the partitions should be less than the cross-sectional area of the through channel 2 at the location of installation of the corresponding partition so that the flow of the reaction component can pass through the channel 2. Accordingly, at least one partition preferably blocks from 20% to 80% of the cross-sectional area of the through channel at the location of installation.

In addition, in preferred embodiments of the inventions, at least one partition is installed at the inlet of the through channel. Also, one or more partitions can be installed inside the channel and/or at the outlet from it. Thus, for example, the ratio of the distance l from the location of at least one partition to the inlet section of the through channel to the length L of the through channel (l/L) is from 0.1 to 0.9, preferably from 0.2 to 0.5 or from 0.5 to 0.8, more preferably, the mentioned ratio l/L is from 0.25 to 0.30.

Preferably, at least one partition is also a washer containing a hole coaxial with the through channel, wherein the ratio of the diameter of the washer hole to the diameter of the through channel at the location where the washer is installed is preferably from 0.8 to 0.2, more preferably from 0.40 to 0.55.

The mentioned elements can be installed by any known method inside channel 2 (Fig. 4, 6), at the entrance to channel 2 (Fig. 3-5) and/or at the exit from channel 2 (not shown in the Fig.). Also, the mentioned elements can be integral to part 1, i.e. made in the form of a single monolithic structure, which can be obtained, for example, using additive technologies.

The hydraulic resistance means is selected by a specialist depending on the area of application of the reactor 100 and the parameters of the reaction components, as well as the required values of the intensity of swirl and mixing of the reaction components, as well as the distance of the swirl zone from part 1.

Below is an example of the implementation of a group of inventions according to the best option.

A reactor 100 with a fixed catalyst bed in the form of a secondary reforming apparatus for hydrocarbon gas comprises a reaction component input unit 101, which includes a channel for an oxidizing component (process air) and a channel for a fuel component (converted gas). A blade swirler 10 is installed in the channel for the oxidizing component so that the ratio of the distance H from the outlet section of the through channel to the outlet section of the channel for the oxidizing component to the length L of the through channel (H/L) is from 5.1 to 5.6 (Fig. 2).

The swirler 10 contains a part 1 oriented in the shape of a cylinder with an axial through channel 2 having a rounded shape. The ratio of the length L of the channel 2 to the diameter D of its inlet section (L/D) is from 4 to 5 (Fig. 3-4). On the outer surface of the part 1 there are eight blades 3 with a rotation angle Y of 90 degrees.

In this case, the channel contains a means of hydraulic resistance for the oxidizing component, including a plate 5 with holes located along the perimeter of the plate 5 symmetrically relative to the axis of the channel 2, and a washer 4 installed at the entrance to the channel 2 and having a hole coaxial with the channel 2, the diameter of which is smaller than the diameter of the channel 2 at the entrance, which creates the presence of a variable diameter along the length of the channel. The ratio of the diameter d1 of the hole of the washer 4 to the diameter D of the channel 2 at its entrance (d1/D) is from 0.40 to 0.55 (Figs. 3-5).

The ratio of the distance l from the location of plate 5 to the inlet section of channel 2 to the length L of channel 2 itself (l/L) is from 0.25 to 0.30. However, another option is allowed, in which the ratio l/L is from 0.5 to 0.8 (Fig. 4).

Both plate 5 and washer 4 cover from 20% to 80% of the cross-sectional area of channel 2 at the location of their installation, thereby creating the necessary resistance to the flow of fluid.

The described vane swirler 10 is simple, reliable and easy to manufacture, allows for stable and increased intensity of vortex formation and mixing of reaction components at the required and constant distance from the swirler 10, due to the possibility for a specialist to select the shape and number of partitions included in the hydraulic resistance means in the through channel 2, depending on the parameters of the reactor 100 and the reaction components used, as well as the required parameters at the outlet of the reactor 100. Thus, the hydraulic resistance means is capable of not only slowing down part of the flow of the reaction component passing through channel 2, but also, if necessary, breaking it into separate streams, and, in some cases, even additionally swirling this flow and/or accelerating it.

The proposed reactor 100 with a fixed catalyst bed operates according to one of the best embodiments as follows.

The oxidizing component of the reaction in the form of a fluid flow passes through a corresponding channel or pipeline, which is contained in the reaction component input unit 101 of the reactor 100. Similarly, the fuel component of the reaction in the form of a fluid flow passes through a corresponding channel or pipeline, which is contained in the reaction component input unit 101 of the reactor 100.

In each of these two channels or only in one of them, a vane swirler 10 is installed so that the ratio of the distance from the outlet section of the through axial channel 2 to the outlet section of the channel 6 for the oxidizing or fuel component to the length of the through channel 2 is equal to a value from the range from 5.1 to 5.6 (H/L).

The first part of the flow, predominantly the larger one, enters eight blades 3 with a rotation angle of 120 degrees, which impart a better swirling, vortex motion to this part of the flow. The other (second) part of the flow, predominantly the smaller one, enters the through channel 2, at the entrance to which a washer 4 with an opening, the diameter of which is smaller than the diameter of the inlet section of channel 2, is installed. The washer 4 only slows down the second part of the flow, does not block it and practically does not reduce it, as would happen in the case of decreasing the diameter of channel 2 to the diameter of the opening of the washer 4, since channel 2 remains of a larger diameter and is capable of accommodating a larger volume of the reaction component flow. The ratio of the diameter of the opening of the washer 4 to the diameter of channel 2 (d1/D) is equal to a value from the range from 0.40 to 0.55.

Then, part of the reaction component flow encounters plate 5 with holes located along its perimeter symmetrically relative to the axis of channel 2 on its way along channel 2. Plate 5 additionally slows down this flow and, due to the holes located in a similar manner, breaks it into streams that will twist more easily at the exit from channel 2. Thus, due to washer 4 and plate 5, the flow is slowed down in a more precise and predictable manner.

Then a smaller part of the reaction component flow leaves channel 2, having predominantly a straight motion along the path coaxial with channel 2, and a lower speed (V2) than the speed (V) of the entire flow before the swirler (V2 < V). The first, larger part of the flow also leaves blades 3, having a swirling motion and a speed (V1) that differs from the speed of the part of the flow from channel 2 (V1 < V2). Moreover, the speed (V1) of the flow after blades 3 is also less than the speed (V) of the entire flow before the swirler (V1 < V).

The direct flow from channel 2 captures the swirled flow from blades 3 and promotes its movement further along the channel for the reaction component and after exiting the channel into the reactor zone 100 above the catalyst bed with greater force and speed than if the entire flow came off only blades 3. At the same time, a flow of another reaction component, swirled in a similar manner or not, is fed into the said zone of reactor 100, which intensively mixes with the swirled flow of the first reaction component at a distance from it calculated and specified by a specialist due to the design of swirler 10. The mixture ignites and passes through the catalyst bed in zone 102, then leaves reactor 100 through the reaction product outlet unit 103.

For the considered example of the implementation of the hydraulic resistance means, channel 2 creates a smaller pressure drop for the second part of the flow than for the first part of the flow, and allows the flow at the outlet of channel 2 to maintain a higher speed than for the main part of the flow (V2 > V1), and also to direct this main part behind itself at a greater distance from the swirler 10. Due to this, at the required distance from the swirler 10, a zone of intensive vortex formation of the flow is created, for example, the oxidizing component of the reaction, and the flow speed is set in an accurate and stable manner, which improves the mixing of all components and allows for the required temperature distribution throughout the reactor, and therefore improves its operation and increases reliability.

The results of testing the inventions in the apparatus for secondary reforming of hydrocarbon gas according to the most preferred options are presented in the table below.

Table 1. Variants 1-4 for implementing inventions.

Swirler and reactor parameters Option 1 2 3 4 The swirl element is installed in the channel for the reaction component. fuel oxidizing oxidizing oxidizing and fuel Blade rotation angle Y, deg. 60 280 180 360 Channel diameter D variable constant The ratio of the length L of a through channel to the diameter D of its inlet section (L/D) 2 4 5 7 Design of hydraulic resistance means in the form of a partition Washer Plate with holes Washer and plate with holes The ratio of the diameter d1 of the washer hole to the diameter D of the channel at the location of the washer installation (d1/D) 0.2 - 0.8 0.45 Percentage of overlap of the cross-sectional area of the through channel by the partition at the installation site 20% 40% 30% (washer) and 60% (plate with holes) 40% (washer) and 80% (plate with holes) The ratio of the distance l from the location of the plate with holes to the inlet section of the channel to the length L of the channel (l/L) - 0,1 0.27 0.9 Location of the washer In the first half of the channel - At the entrance to the canal In the second half of the channel The ratio of the distance H from the outlet section of the through channel to the outlet section of the channel for the reaction component to the length L of the through channel (H/L) 0 5.1 5.6 10 ensuring increased efficiency and reliability of reactor operation due to the intensity of vortex formation and mixing of reaction components at the required distance from the outlet of the blade swirler
(* - good, ** - very good, *** - excellent) * ** *** **

Claims (28)

1. A blade swirler for a reaction component for a fixed bed reactor comprising a cylindrical oriented part with blades on the outer surface, characterized in that the part has an axial through channel with a means of hydraulic resistance for the specified reaction component, the hydraulic resistance means comprises at least one partition, the ratio of the distance from the location of at least one partition to the inlet section of the through channel to the length of the through channel is from 0.1 to 0.9. 2. A swirler according to item 1, characterized in that the blades have a rotation angle of 60 to 360°. 3. A swirler according to item 1, characterized in that the through channel has a variable diameter along the length of the through channel. 4. A swirler according to item 1, characterized in that at least one partition is installed at the entrance to the through channel. 5. The swirler according to item 1, characterized in that at least one partition has openings. 6. A swirler according to claim 1, characterized in that at least one partition is a washer containing an opening coaxial with the through channel. 7. A swirler according to item 6, characterized in that the ratio of the diameter of the washer opening to the diameter of the through channel at the location where the washer is installed is from 0.8 to 0.2, preferably from 0.40 to 0.55. 8. A swirler according to claim 1, characterized in that at least one partition is a plate with holes located along the perimeter of the plate symmetrically relative to the axis of the through channel. 9. A swirler according to item 1, characterized in that at least one partition covers from 20 to 80% of the cross-sectional area of the through channel at the location where the partition is installed. 10. A swirler according to claim 1, characterized in that the ratio of the distance from the location of at least one partition to the inlet section of the through channel to the length of the through channel is from 0.2 to 0.5, more preferably from 0.25 to 0.30. 11. A swirler according to claim 1, characterized in that the ratio of the distance from the location of at least one partition to the inlet section of the through channel to the length of the through channel is from 0.5 to 0.8. 12. A swirler according to claim 1, characterized in that the ratio of the length of the through channel to the diameter of its inlet section is from 2 to 7, preferably from 4 to 5. 13. A swirler according to item 1, characterized in that the hydraulic resistance means includes a washer containing a hole coaxial with the through channel, and a plate with holes located along the perimeter of the plate symmetrically relative to the axis of the through channel. 14. The swirler according to item 13, characterized in that the washer is installed at the entrance to the through channel, and the ratio of the diameter of the washer opening to the diameter of the through channel at its entrance is from 0.8 to 0.2, preferably from 0.40 to 0.55, and the ratio of the distance from the location of the plate with holes to the inlet section of the through channel to the length of the through channel is from 0.1 to 0.9, preferably from 0.2 to 0.5, more preferably from 0.25 to 0.30. 15. A reactor with a fixed catalyst bed, comprising a reaction component input unit, characterized in that a blade swirler for the reaction component according to any one of paragraphs 1-14 is installed in the input unit. 16. The reactor according to item 15, characterized in that the reactor is a secondary reforming apparatus. 17. The reactor according to item 15, characterized in that the reaction component input unit contains a channel for the oxidizing component, and the swirler is installed in this channel and/or the reaction component input unit contains a channel for the fuel component, and the swirler is installed in this channel. 18. The reactor according to claim 17, characterized in that the ratio of the distance from the outlet section of the through channel to the outlet section of the channel for the oxidizing component to the height of the swirler is from 0 to 10, preferably from 5 to 8, more preferably from 5.1 to 5.6. 19. The reactor according to claim 17, characterized in that the ratio of the distance from the outlet section of the through channel to the outlet section of the channel for the fuel component to the height of the swirler is from 0 to 10, preferably from 5 to 8, more preferably from 5.1 to 5.6. 20. A method for operating a fixed-bed catalyst reactor according to any one of paragraphs 15-19, comprising a reaction component input unit and a blade swirler installed therein for the reaction component, comprising the steps of feed the reaction components into the input unit, at the same time, at least one component is fed through a vane swirler.