CN211612256U

CN211612256U - Catalyst loader and denitration reaction equipment with same

Info

Publication number: CN211612256U
Application number: CN201921991960.3U
Authority: CN
Inventors: 戴旭建; 邓跃云
Original assignee: Hunan Job Energy Technology Co ltd
Current assignee: Hunan Job Energy Technology Co ltd
Priority date: 2019-11-18
Filing date: 2019-11-18
Publication date: 2020-10-02
Anticipated expiration: 2029-11-18

Abstract

The utility model relates to a catalyst loader technical field specifically provides a catalyst loader and have denitration reaction equipment of this catalyst loader, and the capacity that aims at solving catalyst filling container in the current denitration reaction equipment is fixed, can't adjust the packing volume of catalyst and the area of contact's of treating reactant gas problem according to reactant gas's concentration. Mesh structure, the end plate, the sliding plate, first barrel, the second barrel, the third barrel encloses into first catalyst loading space.

Description

Catalyst loader and denitration reaction equipment with same

Technical Field

The utility model relates to a catalyst loader technical field specifically provides a catalyst loader and have denitration reaction equipment of this catalyst loader.

Background

Flue gas discharged by thermal power plants, smelting plants, industrial boilers and the like contains a large amount of NOx, and is a main pollutant for generating acid rain in the atmosphere. Generally, the discharged flue gas and ammonia gas are introduced into a denitration reaction device, and the ammonia gas and NOx in the flue gas are subjected to a reduction reaction under the catalytic action of a catalyst to generate nitrogen and water to be discharged. However, the traditional catalyst is of a honeycomb structure, and the air speed ratio of the honeycomb structure catalyst is 2500-3000h^-1The volume ratio is large. Due to the influence of the catalyst material and process, the honeycomb catalyst is brittle in texture and is easily damaged during transportation and loading.

In view of this, particulate catalysts have been developed, the space velocity ratio of which is typically 6500-9000h^-1Compared with honeycomb catalyst, the volume ratio is greatly reduced. However, during use, the particulate catalyst is packed in a fixed-capacity container of the denitration reactor, the contact area of the particulate catalyst with the gas to be reacted is fixed, and the packing amount of the particulate catalyst and the contact area of the particulate catalyst with the gas to be reacted cannot be adjusted according to the concentration of the reaction gas.

Accordingly, there is a need in the art for a new solution to the above problems.

SUMMERY OF THE UTILITY MODEL

In order to solve the above problems in the prior art, that is, to solve the problems that the capacity of the catalyst-filled container in the prior denitration reactor is fixed, the filling amount of the catalyst and the contact area between the catalyst and the gas to be reacted cannot be adjusted according to the concentration of the gas to be reacted, in one aspect, the present invention provides a catalyst loader, which comprises a first cylinder, wherein an end plate is fixed at a first end of the first cylinder, an opening is formed in the middle of the end plate, a sliding plate which is in sliding fit with the inner wall of the first cylinder is arranged in the first cylinder, a second cylinder and a third cylinder are arranged between the end plate and the sliding plate in a nested manner, the first end of the second cylinder is fixedly connected with the edge of the opening, the first end of the third cylinder is fixedly connected with the sliding plate, and the first cylinder, the second cylinder and the third cylinder are all in mesh structure, the end plate, the sliding plate, the first cylinder, the second cylinder and the third cylinder enclose a first catalyst loading space.

In the preferable technical scheme of the catalyst loader, the third cylinder is sleeved on the outer side of the second cylinder or the second cylinder is sleeved on the outer side of the third cylinder.

In a preferred embodiment of the catalyst loader, at least one filling port is provided in a region of the slide plate corresponding to the first catalyst loading space.

In a preferred embodiment of the catalyst loader, an area of the sliding plate corresponding to the inside of the third cylinder is a mesh structure, and a space between the second end of the first cylinder and the sliding plate forms a second catalyst loading space.

In a preferred embodiment of the catalyst loader, the second end of the second cylinder and/or the second end of the third cylinder are provided with a reinforcing ring.

In a preferred embodiment of the catalyst loader, the first cylinder, the second cylinder, and the third cylinder have the same cross-sectional shape.

In a preferred embodiment of the catalyst loader, the first cylinder, the second cylinder, and the third cylinder are coaxially disposed.

In the preferable technical scheme of the catalyst loader, the distance between the inner wall of the first cylinder and the outer wall of the second cylinder is 50-80 mm.

In a preferred embodiment of the catalyst loader, the mesh structure is a porous plate structure or a mesh structure.

The technical scheme of the utility model, catalyst loader includes first barrel, the first end of first barrel is fixed with the end plate, the end plate middle part has the opening, be provided with the sliding plate rather than inner wall sliding fit in the first barrel, be provided with nested second barrel and third barrel between end plate and the sliding plate, the first end and the open-ended edge fixed connection of second barrel, the first end and the sliding plate fixed connection of third barrel, first barrel, second barrel and third barrel are the mesh structure, the end plate, the sliding plate, first barrel, the second barrel, the third barrel encloses into first catalyst loading space. The third cylinder and the slide plate slide together relative to the first cylinder and the second cylinder, so that the volume of the first catalyst-loading space is changed while the contact area of the particulate catalyst loaded in the catalyst loader with the reaction gas is changed. Through the catalyst loader, the size of the first catalyst loading space in the catalyst loader can be adjusted according to the concentration of the gas required by the reaction equipment to carry out denitration reaction, so that the amount of the catalyst required by reaction of reaction gases with different concentrations and the contact area of the catalyst and the reaction gases are met, and the reaction efficiency is improved.

On the other hand, the utility model also provides a denitration reaction device, denitration device includes the casing, be formed with the reaction chamber in the casing, be formed with import and export on the casing, the reaction intracavity dispose above-mentioned arbitrary any catalyst loader, the opening with import or exit linkage. It should be noted that, the denitration reaction device has all the technical effects of the catalyst loader, and the details are not repeated herein.

Drawings

Preferred embodiments of the present invention are described below with reference to the accompanying drawings, in which:

fig. 1 is a schematic structural diagram of a denitration reaction apparatus according to an embodiment of the present invention;

fig. 2 is a schematic sectional view of a denitration reaction apparatus according to an embodiment of the present invention;

fig. 3 is the utility model discloses a half section schematic diagram of catalyst loader in denitration reaction equipment of embodiment.

List of reference numerals:

1. a housing; 11. a housing; 111. an outer layer structure; 112. an inner layer structure; 12. an inner shell; 131. a first cavity; 132. a second cavity; 2. a feed channel; 3. a discharge channel; 4. an explosion-proof type electric heater; 5. a temperature sensor; 6. a pressure sensor; 7. a partition plate; 71. mounting holes; 8. a catalyst loader; 81. a first cylinder; 82. a second cylinder; 83. a third cylinder; 84. an end plate; 841. an opening; 85. a sliding plate; 851. a fill port; 86. a first catalyst loading space; 87. a second catalyst loading space; 88. a reinforcement ring.

Detailed Description

Preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and are not intended to limit the scope of the present invention. For example, although the present invention has been described with reference to a catalyst loader for a denitration reactor, it can be adjusted as needed by those skilled in the art to suit a particular application, and the catalyst loader of the present invention can also be applied to a desulfurization reactor or other suitable reactors. Obviously, the technical solution after adjustment still falls into the protection scope of the present invention.

It should be noted that in the description of the present invention, the terms "left", "right", "upper", "lower", "inner", "outer", etc. indicate directions or positional relationships based on those shown in the drawings, which are merely for convenience of description, and do not indicate or imply that the apparatus or the components must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In addition, it should be noted that, unless otherwise explicitly stated or limited, the terms "disposed" and "connected" are to be construed broadly and include, for example, fixed connections, detachable connections, or integral connections; either directly or indirectly through intervening media, or through the communication between two elements. The specific meaning of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

Furthermore, in the following detailed description, numerous specific details are set forth in order to provide a better understanding of the present invention. It will be understood by those skilled in the art that the present invention may be practiced without some of these specific details. In some embodiments, methods, means, elements and circuits that are well known to those skilled in the art have not been described in detail so as not to obscure the present invention.

Based on among the background art current denitration response device catalyst fill container's capacity fixed, can't adjust the packing volume of catalyst and the problem of waiting reacting gas's area of contact according to reacting gas's concentration, the utility model provides a catalyst loader, including first barrel, the first end of first barrel is fixed with the end plate, and the end plate middle part has the opening, be provided with in the first barrel rather than inner wall sliding fit's sliding plate, be provided with nested second barrel and third barrel between end plate and the sliding plate, the first end and the open-ended edge fixed connection of second barrel, the first end and the sliding plate fixed connection of third barrel, first barrel, second barrel and third barrel are mesh structure, end plate, sliding plate, first barrel, second barrel, third barrel enclose into first catalyst loading space. The third cylinder and the slide plate are slidable relative to the first cylinder and the second cylinder, so that the volume of the first catalyst-loading space is changed, and the contact area between the particulate catalyst loaded in the catalyst loader and the reaction gas is changed. In the use process, the size of the first catalyst loading space in the catalyst loader can be adjusted according to the concentration of the gas needing denitration reaction in the reaction equipment, so that the catalyst with the amount corresponding to the gas to be reacted is loaded, the contact area of the catalyst and the reaction gas is in a proper range, and the reaction efficiency is improved. Meanwhile, the gas passing sectional area of the reaction gas is changed, and the gas passing time (such as about 0.8 second, 1.5 seconds and the like) of the mixed flue gas and ammonia gas passing through the reaction layer of the catalyst is changed under the condition that the amount of the flue gas to be treated is relatively constant, so that the reaction efficiency is improved.

Referring to fig. 1 to 3, fig. 1 is a schematic structural diagram of a denitration reaction apparatus according to an embodiment of the present invention; fig. 2 is a schematic sectional view of a denitration reaction apparatus according to an embodiment of the present invention; fig. 3 is the utility model discloses a half section schematic diagram of catalyst loader in denitration reaction equipment of embodiment.

As shown in fig. 1 to 3, in a specific embodiment, the denitration reactor includes a casing 1, and the casing 1 includes an outer casing 11 and an inner casing 12. The outer shell 11 includes an outer layer structure 111 and an inner layer structure 112, and a heat insulation layer (not shown in the figure) is disposed between the outer layer structure 111 and the inner layer structure 112, and specifically, the heat insulation layer is a heat insulation material layer filled between the outer layer structure 111 and the inner layer structure 112, such as a rock wool layer, or a ceramic filler layer or a high temperature glass fiber layer. A reaction chamber is formed in the inner shell 12, a partition 7 is disposed in the reaction chamber, and the reaction chamber is divided into an upper first chamber 131 and a lower second chamber 132 by the partition 7. A feed passage 2 is formed between the outer shell 11 and the inner shell 12, one end of the feed passage 2 communicates with the outside, and the other end of the feed passage 2 communicates with the first cavity 131. The shell 1 is further provided with a discharge channel 3 penetrating through the outer shell 11 and the inner shell 12, one end of the discharge channel 3 is communicated with the second cavity 132, and the other end of the discharge channel 3 is communicated with the outside. The partition plate 7 is provided with a plurality of mounting holes 71, and a catalyst loader 8 is mounted at each mounting hole 71. The case 1 is provided with 4 explosion-proof electric heaters 4 externally inserted into the

second cavity

132, 1 temperature sensor 5 externally inserted into the

second cavity

132, and 2 pressure sensors 6 externally inserted into the second cavity 132. In use, the explosion-proof electric heater 4 is used for heating the granular catalyst filled in the catalyst loader 8 to improve the activity of the catalyst, and the temperature sensor 5 and the pressure sensor 6 are respectively used for detecting the temperature and the pressure in the reaction cavity. The denitration reaction apparatus further includes a controller (not shown in the figure) that controls the power of the explosion-proof type electric heater 4 based on the data detected by the temperature sensor 5. The shape of the catalyst particles may be granular, columnar, trilobal, annular, or the like.

As shown in fig. 3, the catalyst loader 8 includes a first cylinder 81 having a circular cross section, an end plate 84 is fixed to a lower end of the first cylinder 81, an opening 841 is formed in a middle portion of the end plate 84, a sliding plate 85 slidably fitted to an inner wall of the first cylinder 81 is provided in the first cylinder 81, a second cylinder 82 and a third cylinder 83 having a circular cross section are provided between the end plate 84 and the sliding plate 85 in a nested manner, a lower end of the second cylinder 82 is fixedly connected to an edge of the opening 841, an upper end of the third cylinder 83 is fixedly connected to the sliding plate 85, the third cylinder 83 is sleeved outside the second cylinder 82, and the first cylinder 81, the second cylinder 82 and the third cylinder 83 are coaxially disposed. The first cylinder 81, the second cylinder 82, and the third cylinder 83 are all mesh structures, 4 filling ports 851 are provided in a region of the sliding plate 85 corresponding to the first catalyst loading space 96, and a region of the sliding plate 85 corresponding to the inside of the third cylinder 83 is mesh structures. For example, the first cylinder 81, the second cylinder 82, and the third cylinder 83 are made of porous plates, and the sliding plate 85 is made of porous plates in the region corresponding to the inside of the third cylinder 83. It is understood that the first cylinder 81, the second cylinder 82 and the third cylinder 83 may be made of metal mesh, and the area of the movable plate 85 corresponding to the inside of the third cylinder 83 is made of metal mesh. The pore diameter of the pore plate structure or the mesh structure is smaller than the particle diameter of the particulate catalyst. The end plate 84, the slide plate 85, the first cylinder 81, the second cylinder 82, and the third cylinder 83 enclose a first catalyst loading space 86, and a space between the upper end of the first cylinder 81 and the slide plate 85 forms a second catalyst loading space 87. In the mounted state, the opening 841 in the middle of the end plate 84 is fixedly connected to the mounting hole 71 in the partition 7. Preferably, the distance between the inner wall of the first cylinder 81 and the outer wall of the second cylinder 82 is 50-80 mm.

In use, the sliding plate 85 and the third cylinder 83 are first moved up and down according to the concentration of the reaction gas to adjust the volume of the first catalyst loading space 86. Then, the first catalyst loading space 86 is filled with the particulate catalyst through the filling port 851, and the second catalyst loading space 87 is filled with a predetermined amount of the particulate catalyst. Preferably, the thickness of the catalyst layer filled in the second catalyst loading space 87 is 50 to 80 mm. The catalyst loader 8 filled with the particulate catalyst is mounted to the mounting hole 71 on the partition plate 7. The ammonia gas and the flue gas containing a large amount of NOx are mixed and introduced from the left end (in the orientation shown in fig. 2) of the feed channel 2, after which the mixed gas flows upward between the outer shell 11 and the inner shell 12 and finally enters the first chamber 131 from the upper part of the inner shell 12. A part of the mixed gas in the first cavity 131 enters the first catalyst loading space 86 from the outer side of the first shell 81 along the radial direction, flows through the catalyst, enters the interior of the second cylinder 82, and finally enters the second cavity 132 from the opening 841; another part of the mixed gas in the first chamber 131 enters the second catalyst loading space 87 of the catalyst loader 8, flows through the catalyst and the sliding plate 85 from top to bottom along the axial direction of the first cylinder 81, enters the second cylinder 82, and finally enters the second chamber 132 through the opening 841. In the process that the mixed gas flows through the catalyst, under the catalytic action of the catalyst, NOx in the flue gas and ammonia gas undergo a reduction reaction to generate nitrogen gas and water, and the reacted mixed gas enters the second cavity 132 and is discharged through the discharge channel 3.

The first cylinder 81, the second cylinder 82 and the third cylinder 83 have the same cross section and are coaxially arranged, so that the radial dimension of the first cylinder 81 is the same at each position of the first catalyst loading space 86, and the mixed gas contacts with a catalyst layer with the same thickness in the process of entering the first catalyst loading space 86 from different positions outside the first shell 81 along the radial direction and flowing through the catalyst, thereby ensuring the catalytic effect of the catalyst. The distance between the inner wall of the first cylinder 81 and the outer wall of the second cylinder 82 is set to be 50-80 mm, the thickness of the catalyst layer filled in the second catalyst loading space 87 is 50-80 mm, the contact area of the mixed gas and the catalyst is ensured, the phenomenon that the mixed gas flows through the catalyst due to overlarge resistance is avoided, and the gas passing pressure head is reduced. The area of the sliding plate 85 corresponding to the inside of the third cylinder 83 is a mesh structure, and a space between the upper end of the first cylinder 81 and the sliding plate 85 forms a second catalyst loading space 87, so that the contact area of the mixed gas and the catalyst is increased, the reaction efficiency is improved, and the mixed gas is ensured to fully react.

It will be understood by those skilled in the art that the number of the filling ports 851 provided to the area of the sliding plate 85 corresponding to the first catalyst loading space 96 is 4 only as an exemplary description, and those skilled in the art can adjust it as necessary, for example, the number of the filling ports 851 may be 1, 2, 3, etc. The shape and size of the filling opening 851 are not limited, and may be square, circular, annular, or the like. In one possible embodiment, the sliding plate 85 may not be provided with the filling port 851. The sliding plate 85 and the third cylinder 83 are detachably connected, and the first catalyst loading space 86 is filled with the catalyst after the sliding plate 85 is removed. In addition, the third cylinder 83 is only a specific embodiment and can be adjusted by those skilled in the art as required, for example, the second cylinder 82 is sleeved outside the third cylinder 83.

Moreover, the first, second and

third cylinders

81, 82, 83 have the same cross-sectional shape and are coaxially arranged only in a preferred embodiment, and can be adjusted as desired by those skilled in the art, such as in a possible embodiment, the first, second and

third cylinders

81, 82, 83 have the same cross-sectional shape, such as circular, and the second and

third cylinders

82, 83 are coaxial but not coaxial with the first cylinder 81; in a possible embodiment, the cross-sectional shapes of the first cylinder 81, the second cylinder 82 and the third cylinder 83 are different, the cross-sectional shapes of the first cylinder 81 and the third cylinder 83 are circular, the cross-sectional shape of the second cylinder 82 is equilateral triangle, square, regular pentagon, etc., and the first cylinder 81, the second cylinder 82 and the third cylinder 83 are coaxially arranged.

In a possible embodiment, the sliding plate 85 is not provided with a mesh structure in a region corresponding to the inside of the third cylinder 83, the sliding plate 85 is a solid plate in a region corresponding to the inside of the third cylinder 83, and only the first catalyst loading space 86 for loading the catalyst is provided in the catalyst loader 8.

With continued reference to FIG. 3, the lower end of the third cylinder 83 is preferably provided with a reinforcement ring 88. By providing the reinforcing ring 88 at the lower end of the third cylinder 83, it is possible to prevent the lower end of the third cylinder 83 from being deformed by heat, which may cause a large friction force or a jam between the third cylinder 83 and the second cylinder 82 due to the squeezing, and thus may affect the movement of the third cylinder 83 relative to the second cylinder 82. It will be understood by those skilled in the art that a reinforcing ring may be provided at the upper end of the second cylinder 82, or both the upper end of the second cylinder 82 and the lower end of the third cylinder 83.

On the other hand, the utility model provides a denitration reaction equipment, denitration reaction equipment include the casing, are formed with the reaction chamber in the casing, are formed with import and export on the casing, and the reaction intracavity disposes the catalyst loader of above-mentioned arbitrary item. An opening 841 in the catalyst loader 8 is connected to an inlet in the housing. The mixed gas flows from the opening 841 into the second cylinder 82, then flows through the catalyst into the reaction chamber, and finally flows out of the outlet on the housing. In another possible embodiment, the opening 841 in the catalyst loader 8 is connected to an outlet in the housing, and the mixed gas entering the reaction chamber flows through the catalyst into the second cylinder 82 and finally out of the outlet in the housing through the opening 841.

It can be seen from the above description that in the technical scheme of the utility model, the catalyst loader includes first barrel, the first end of first barrel is fixed with the end plate, the end plate middle part has the opening, be provided with in the first barrel rather than inner wall sliding fit's sliding plate, be provided with nested second barrel and third barrel between end plate and the sliding plate, the first end and the open-ended edge fixed connection of second barrel, the first end and the sliding plate fixed connection of third barrel, first barrel, second barrel and third barrel are the mesh structure, the end plate, the sliding plate, first barrel, the second barrel, the third barrel encloses into first catalyst loading space. The third cylinder and the slide plate slide together relative to the first cylinder and the second cylinder, so that the volume of the first catalyst-loading space is changed while the contact area of the particulate catalyst loaded in the catalyst loader with the reaction gas is changed. Through the catalyst loader, the size of the first catalyst loading space in the catalyst loader can be adjusted according to the concentration of the gas required by the reaction equipment to carry out denitration reaction, so that the amount of the catalyst required by reaction of reaction gases with different concentrations and the contact area of the catalyst and the reaction gases are met, and the reaction efficiency is improved.

So far, the technical solution of the present invention has been described with reference to the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, a person skilled in the art can make equivalent changes or substitutions to the related technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.

Claims

1. The catalyst loader is characterized by comprising a first cylinder body, wherein an end plate is fixed at the first end of the first cylinder body, an opening is formed in the middle of the end plate, a sliding plate in sliding fit with the inner wall of the first cylinder body is arranged in the first cylinder body, a second cylinder body and a third cylinder body are arranged between the end plate and the sliding plate in a nested mode, the first end of the second cylinder body is fixedly connected with the edge of the opening, the first end of the third cylinder body is fixedly connected with the sliding plate, the first cylinder body, the second cylinder body and the third cylinder body are of mesh structures, and a first catalyst loading space is defined by the end plate, the sliding plate, the first cylinder body, the second cylinder body and the third cylinder body.

2. The catalyst loader of claim 1, wherein the third cylinder is sleeved outside the second cylinder or the second cylinder is sleeved outside the third cylinder.

3. The catalyst loader of claim 2, wherein the area of the slide plate corresponding to the first catalyst loading space is provided with at least one fill port.

4. The catalyst loader of claim 3 wherein the area of the slide plate corresponding to the inside of the third cylinder is a mesh structure,

the space between the second end of the first cylinder and the slide plate forms a second catalyst loading space.

5. The catalyst loader of claim 4, wherein the second end of the second cylinder and/or the second end of the third cylinder is provided with a stiffening ring.

6. The catalyst loader of any one of claims 1 to 5, wherein the cross-sectional shape of the first cylinder, the second cylinder, and the third cylinder are the same.

7. The catalyst loader of claim 6, wherein the first cylinder, the second cylinder, and the third cylinder are coaxially disposed.

8. The catalyst loader of claim 7, wherein the distance between the inner wall of the first cylinder and the outer wall of the second cylinder is 50-80 mm.

9. The catalyst loader of claim 8, wherein the mesh structure is a perforated plate structure or a mesh structure.

10. A denitration reactor, comprising a housing, a reaction chamber formed in the housing, and an inlet and an outlet formed on the housing, wherein the catalyst loader of any one of claims 1 to 9 is disposed in the reaction chamber, and the opening is connected to the inlet or the outlet.