KR20230068634A - Catalytic combustion reactor with improved rheology - Google Patents

Abstract

One embodiment of the present invention is a catalytic combustion reactor with improved fluidity, which is formed on an inlet into which gaseous reactants are introduced, and reacts into the catalytic combustion reactor by mixing the reactants having various composition materials. A line mixer for passing materials, a gas mixer for redistributing passages of reactants passing through the line mixer, a monolith catalyst for promoting combustion of reactants passing through the gas mixer, and front and rear ends of the monolith catalyst and a mesh layer for forming turbulent flow in the passage of the reactant, wherein the diameter of the inlet in which the line mixer is disposed is smaller than the diameter of the main body of the catalytic combustion reactor in which the catalyst and the mesh layer are disposed. It provides a catalytic combustion reactor with improved fluidity, characterized in that.

Description

Catalytic combustion reactor with improved fluidity {CATALYTIC COMBUSTION REACTOR WITH IMPROVED RHEOLOGY}

The present invention relates to a catalytic combustion reactor, and more particularly, to a catalytic combustion reactor for burning unreacted gas discharged from a solid oxide fuel cell.

Demand for energy has grown exponentially over the past several centuries. As the demand for energy increases, many different energy sources have been explored and developed.

Combustion of hydrocarbons is one of the basic energy sources, but due to pollutants generated during combustion of hydrocarbons, recently, as the demand for clean energy sources increases, research on fuel cells is increasing.

Fuel cells use electrochemical energy conversion to convert hydrogen and oxygen into electricity and heat. Fuel cells are similar to batteries, but they can be charged while providing power. In many cases, fuel cells are expected to replace primary and secondary batteries as a portable power source.

A solid oxide fuel cell (SOFC), a type of fuel cell, uses hydrogen as an energy source, generates electricity from a stack composed of an anode, an electrolyte, and a cathode, and uses a solid oxide as an electrolyte. Such a solid oxide fuel cell operates at a high temperature of 600° C. or more, thus showing the highest efficiency among fuel cells, minimizing the use of noble metal-based catalysts, and reducing CO ₂ emissions.

At this time, the high-temperature unreacted gas (N ₂ , CO ₂ , O ₂ , CO, CH ₄ , etc.) remaining after the reaction at the cathode and anode of the SOFC is transferred to the reactor in the presence of a catalyst. to treat unreacted gas.

Some of the unreacted gas (fuel) is combustible, but complete combustion is difficult due to different composition ratios, and there is an emission standard that allows only exhaust gases below a certain concentration to be discharged under the Clean Air Conservation Act. Combustion process is required.

However, the conventional catalytic combustion reactor has a problem that a rapid temperature gradient is generated on the surface of the monolith catalyst and the channel portion due to uneven high-temperature fluid during the combustion process of unreacted gas, and thus the complete combustion efficiency using the monolith catalyst is reduced. there was

A technical problem to be achieved by the present invention is to provide a catalytic combustion reactor with improved fluidization capable of suppressing hot spots and eddy currents of the monolithic catalyst channel in a catalytic combustion reaction using a monolithic catalyst and uniform supply of raw materials .

The technical problem to be achieved by the present invention is not limited to the above-mentioned technical problem, and other technical problems not mentioned can be clearly understood by those skilled in the art from the description below. There will be.

In order to achieve the above technical problem, one embodiment of the present invention is formed on an inlet into which gaseous reactants are introduced, and mixes the reactants having various composition materials to introduce the reactants into the catalytic combustion reactor. A line mixer for passing through the line mixer, a gas mixer for redistributing the passage of the reactants passing through the line mixer, a monolithic catalyst for promoting combustion of the reactants passing through the gas mixer, and disposed in front and rear of the monolith catalyst , A mesh layer for forming turbulent flow in the passage of the reactant, characterized in that the diameter of the inlet in which the line mixer is disposed is smaller than the diameter of the main body of the catalytic combustion reactor in which the catalyst and the mesh layer are disposed. To provide a catalytic combustion reactor with improved fluidity.

In an embodiment of the present invention, the line mixer includes an inlet region disposed toward the inlet into which the reactant flows, and a discharge region discharging the introduced reactant toward the gas mixer, The inlet region may be formed in a circular shape along the circumference of the line mixer by having a plurality of inlet holes spaced apart at a predetermined interval on one surface disposed toward the inlet into which the reactant is introduced.

In an embodiment of the present invention, the discharge area is formed with a step so that the height from the one surface to the central portion of the discharge area is lower than the height from the one surface to the edge of the discharge area, and the edge and A plurality of discharge holes may be spaced apart from each other by a predetermined interval on the inner surface of the edge formed by the step of the central portion.

In an embodiment of the present invention, the line mixer further comprises a connection passage forming a passage for the reactant introduced through the inlet hole as the connection between the inlet hole and the outlet hole is made, The angle may be formed at least 45° or more.

In an embodiment of the present invention, the size of the discharge hole may be formed to be 8 to 10% of the diameter of the body of the catalytic combustion reactor.

In an embodiment of the present invention, the gas mixer is formed in a cylindrical shape, the inner tube is formed in a shape in which the diameter size decreases from both ends toward the central portion, and the gas mixer is formed with a reactive material flowing into the central portion. In order to forcibly mix, it may include a first type mixer that rotates and a rotation shaft that forms an axis of the first type mixer and is connected to an external rotation gear to rotate the first type mixer.

In an embodiment of the present invention, the first type mixer is a ribbon mixer or a paddle mixer, and may rotate at a speed of 150 to 200 RPM.

In an embodiment of the present invention, the gas mixer is formed in a cylindrical shape, and forms a second type mixer that rotates on an axis to forcibly mix reactants flowing into the central portion, and an axis of the second type mixer, , A rotation shaft connected to an external rotation gear to rotate the second type mixer, and coupled to the second type mixer and the rotation shaft, so that the second type mixer rotates itself separately from the rotation by the rotation shaft This may include an auxiliary mixer.

In an embodiment of the present invention, the second type mixer rotates at a speed of 100 to 200 RPM, and the auxiliary mixer may be formed of a rotary blade.

In an embodiment of the present invention, the gas mixer is formed of a perforated plate including perforated holes spaced apart at predetermined intervals on the front surface, and the central perforated hole formed in the center of the perforated holes is different in size from other perforated holes. may be formed differently.

In an embodiment of the present invention, 50 to 200 mesh holes may be formed in the mesh layer.

According to an embodiment of the present invention, in a catalytic combustion reaction using a monolith catalyst, hot spots and eddy currents of the monolith catalyst channel are suppressed, and raw materials can be uniformly supplied, thereby improving the combustion reaction of unreacted gas. there is.

The effects of the present invention are not limited to the above effects, and should be understood to include all effects that can be inferred from the description of the present invention or the configuration of the invention described in the claims.

1 is a diagram schematically showing a catalytic combustion reactor having improved fluidity according to an embodiment of the present invention.
2 is a diagram schematically showing a line mixer according to an embodiment of the present invention.
3 is a cross-sectional view showing a cross section of a line mixer according to various embodiments of the present invention.
4 is a diagram schematically showing a gas mixer according to a first embodiment of the present invention.
5 is a diagram schematically showing a gas mixer according to a second embodiment of the present invention.
6 is a diagram schematically showing a gas mixer according to a third embodiment of the present invention.
7 is a diagram for explaining a first mesh layer and a second mesh layer according to an embodiment of the present invention.
8 is a three-dimensional view of a catalytic combustion reactor according to an embodiment of the present invention.
FIG. 9 is a diagram for comparing the shear force (pressure) of a small area where the pressure generated as raw materials are supplied is applied to each device inside the catalytic combustion reactor.
Fig. 10 is a diagram for comparing pressures when mixed raw materials reach each device inside the catalytic combustion reactor.
11 is a diagram for explaining the speed of the fluid before the mixed raw material is supplied to the monolith catalyst.
12 is a diagram for comparing turbulence intensities when mixed raw materials pass through each device inside the catalytic combustion reactor.

Hereinafter, the present invention will be described with reference to the accompanying drawings. However, the present invention may be embodied in many different forms and, therefore, is not limited to the embodiments described herein. And in order to clearly explain the present invention in the drawings, parts irrelevant to the description are omitted, and similar reference numerals are attached to similar parts throughout the specification.

Throughout the specification, when a part is said to be "connected (connected, contacted, combined)" with another part, this is not only "directly connected", but also "indirectly connected" with another member in between. "Including cases where In addition, when a part "includes" a certain component, it means that it may further include other components without excluding other components unless otherwise stated.

Terms used in this specification are only used to describe specific embodiments, and are not intended to limit the present invention. Singular expressions include plural expressions unless the context clearly dictates otherwise. In this specification, terms such as "include" or "have" are intended to indicate that there is a feature, number, step, operation, component, part, or combination thereof described in the specification, but one or more other features It should be understood that the presence or addition of numbers, steps, operations, components, parts, or combinations thereof is not precluded.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a diagram schematically showing a catalytic combustion reactor having improved fluidity according to an embodiment of the present invention.

Referring to FIG. 1, a catalytic combustion reactor according to an embodiment of the present invention includes a line mixer 100, a gas mixer 200, a first mesh layer 300, a monolith catalyst 400, and a second It may be configured to include the mesh layer 500.

The line mixer 100 is formed on the inlet 11 of the catalytic combustion reactor into which gaseous reactants are introduced, mixes reactants having various composition materials, and passes the mixed reactants into the catalytic combustion reactor. can make it

Here, the gaseous reactant is a high-temperature unreacted gas remaining after reaction at the cathode and anode of the solid oxide fuel cell (SOFC), for example, the unreacted gas is N ₂ , CO ₂ , O ₂ , CO, CH ₄ and the like.

The gas mixer 200 may redistribute flow paths of the reactants passing through the line mixer 100 . That is, the gas mixer 200 of the present invention serves to re-mix the reactants uniformly primarily distributed into the catalytic combustion reactor through the line mixer 100 and secondarily distribute them toward the monolith catalyst 400.

The first mesh layer 300 may be disposed between the gas mixer 200 and the monolithic catalyst 400 to form a turbulent flow in a flow path of the reactants redistributed from the gas mixer 200 .

In addition, the monolithic catalyst 400 burns the reactants passing through the first mesh layer 300 through the line mixer 100 and the gas mixer 200 .

The second mesh layer 500 is disposed at the rear end of the monolith catalyst 400 to form a turbulent flow in the flow path of the burned reactants, and the reactants passing through the second mesh layer 500 of the catalytic combustion reactor It can be discharged through the outlet (15).

Referring to Figure 1, the inlet 11 of the catalytic combustion reactor according to an embodiment of the present invention has a smaller diameter than the main body 13, and the line mixer 100 of the present invention has a smaller diameter than the main body 13 Disposed on the inlet 11, reactants having various composition materials introduced through the inlet 11 may be mixed and then uniformly distributed toward the main body 13.

2 is a diagram schematically showing a line mixer according to an embodiment of the present invention. Figure 2 (a) is a perspective view of the line mixer 100, Figure 2 (b) is a bottom view of the line mixer 100.

First, referring to (a) of FIG. 2, the line mixer 100 according to an embodiment of the present invention has a cylindrical structure, and is directed toward the inlet 11 of the catalytic combustion reactor, which is the direction in which the reactants are introduced. It may include an inlet area 110 disposed therein and an exhaust area 130 which is an area for discharging a reactant towards the gas mixer 200.

As shown in (b) of FIG. 2, the inlet region 110 according to the present embodiment has a plurality of inlet holes 111 at predetermined intervals on one surface disposed toward the inlet 11 into which the reactants are introduced. It may be formed in a circular shape along the circumference of the line mixer 100 spaced apart by a distance.

And, as shown in (a) of FIG. 2, the discharge area 130 according to this embodiment is higher than the height from one side of the inlet area 110 to the edge 131 of the discharge area 130, A step may be formed such that a height from one surface of the inflow region 110 to the central portion 133 of the discharge region 130 is lower.

That is, the edge 131 may be formed in a highly protruding shape, the protruding surface may be disposed to face the main body 13 of the catalytic combustion reactor, and the central portion 133 may be formed in a recessed shape.

Referring to (a) of FIG. 2, a plurality of discharge holes 135 are formed on the inner surface of the edge 131 formed by the step difference between the edge 131 and the central portion 133 of the discharge area 130. It may be formed spaced apart at an interval distance of.

3 is a cross-sectional view showing a cross section of a line mixer according to various embodiments of the present invention.

The discharge holes 135 according to the present embodiment function as discharge ports for discharging reactants mixed into the line mixer 100 through the inlet holes 111 to the outside.

For example, the size of the discharge hole 135 is about 10% of the size of the body 13 (inner diameter of the body portion) of the catalytic combustion reactor, considering the flow rate of the fluid and the pressure difference between the front and rear ends of the line mixer 100. It is preferable to form in size. If the diameter of the discharge hole 135 is formed to a size smaller than 8 to 10% of the size of the main body 13, the generation of differential pressure increases, so there may be a problem in that the effect of uniform distribution through the discharge hole 135 is reduced. there is.

The discharge area 130 of the line mixer 100 of the present invention includes the inlet hole 111 and the discharge hole 135 so that the reactant introduced through the inlet hole 111 can be discharged through the discharge hole 135. It may further include a connection passage 137 connecting them to form a passage.

Figure 3 (a) is a cross-sectional view of the line mixer 100 according to the first embodiment, Figure 3 (b) is a cross-sectional view of the line mixer 100 according to the second embodiment, Figure 3 (c) is a cross-sectional view of the line mixer 100 according to the third embodiment.

The connection passage 137 may be formed at a right angle as shown in (a) of FIG. 3 according to the first embodiment, or in (b) of FIG. 3 according to the second embodiment and FIG. 3 according to the embodiment. As shown in (c) of 3, it may be formed inclined so as to be formed at an angle of 45°. At this time, as a method of forming the slope of the connection passage 137 at an angle of 45 °, the slope may be formed in the middle of the connection passage 137 as in the second embodiment, or the connection passage (as in the third embodiment) 137) may be implemented as forming an inclination angle in an inclined form.

3, the connection passage 137 of the present invention is located between the edge 131 and the central portion 133, so that parallelism can be achieved. In addition, the center line of the connection passage 137 based on the central portion 133 of the discharge area 130 forms a right angle, but is not limited thereto and may be formed in a range of at least 45° or more. As the angular size of the connecting passage 137 decreases, the mixing of reactants passing through each discharge hole 135 in the central portion 133 increases.

As described above, since the line mixer 100 of the present invention should not be deformed or destroyed at high temperatures, it may be implemented with a heat-resistant material. For example, the line mixer 100 may be made of a material such as stainless steel (SUS) or Inconel.

4 is a diagram schematically showing a gas mixer according to a first embodiment of the present invention.

Referring to FIG. 4, which is the first embodiment of the present invention, the gas mixer 200 may include an outer tube 210, an inner tube 220, a rotating shaft 230, and a first type mixer 251. .

According to this embodiment, the exterior 210 of the gas mixer may be formed in a cylindrical shape, and the inner tube 220 may be formed in an hourglass-shaped orifice tube shape whose diameter size decreases toward the center from both ends.

At this time, the central part of the inner pipe 220 where the first type mixer 251 is installed is formed in an angular shape as shown in FIG. 4, and the taper angle, which increases in diameter from the central part to both ends, It is preferable to form an angle of 30 ° to 45 ° in consideration.

And, as shown in FIG. 4, a rotational shaft 230 is formed at the center of the gas mixer 200, and the first type mixer 251 is coupled to the rotational shaft and can be rotated by the rotational shaft 230. .

More specifically, the rotating shaft 230 (shaft) according to the present embodiment rotates by being connected to the external rotating gear 20 operated by receiving power from the external power supply source 30, and is of the first type. As the mixer 251 is coupled with the rotational shaft 230 as a central axis, the rotational shaft 230 rotates to forcibly mix the reactants introduced from the lower portion.

The first type mixer 251 according to the present embodiment may be implemented as, for example, a ribbon mixer or a paddle mixer, and may rotate at a speed of 150 to 200 RPM.

5 is a diagram schematically showing a gas mixer according to a second embodiment of the present invention.

Referring to FIG. 5, which is the second embodiment of the present invention, the gas mixer 200 includes a cylindrical single tube, a rotating shaft 230, a second type mixer 253, and an auxiliary mixer auxiliary mixer 260. can be configured.

A rotation shaft 230 is formed at the center of the gas mixer 200 of the second embodiment, and the second type mixer 253 is coupled to the rotation shaft 230 and can be rotated by the rotation shaft 230 .

The rotating shaft 230 (shaft) according to the present embodiment rotates in connection with the external rotating gear 20 operated by receiving power from the external power supply source 30, as in the first embodiment, and is of the second type. As the mixer 253 is coupled with the rotational shaft 230 as a central axis, the rotational axis 230 rotates and the reactants introduced from the lower portion can be forcibly mixed.

In addition, the auxiliary mixer 260 according to the present embodiment is coupled to the second type mixer 253 and the rotating shaft 230, so that the second type mixer 253 rotates itself separately from the rotation by the rotating shaft 230. exercise is possible

That is, the second type mixer 253 according to the present embodiment performs axis rotation (first axis rotation) about the rotation axis 230 as a central axis, and is formed at the bottom of the second type mixer 253 The auxiliary mixer 260 has a larger diameter than the second type mixer 253 and can independently rotate (rotate on a second axis).

For example, as shown in FIG. 5, the second type mixer 253 according to the second embodiment may be implemented as a handle shape mixer and may rotate at a speed of 100 to 500 RPM, , most preferably at a speed of 100 to 200 RPM.

The second type mixer 253 driven together with the auxiliary mixer 260 according to the present embodiment rotates at a low speed and forcibly mixes the reactants introduced from one side to uniformly distribute them to the other side.

When the second type mixer 253 rotates at high speed, a vortex phenomenon may be accompanied and an empty space may be formed in the center where the reactant (gas) cannot move, so a low speed (e.g., 100 to 200 RPM) ) is preferred.

6 is a diagram schematically showing a gas mixer according to a third embodiment of the present invention. As shown in FIG. 6, the gas mixer 200 according to the third embodiment of the present invention may be implemented as a perforated plate including perforated holes spaced at predetermined intervals on the front surface.

At this time, among the perforated holes formed on the front surface of the gas mixer 200 implemented as a perforated plate, the central perforated hole formed in the center may be formed to have a different size from the other perforated holes.

In the catalytic combustion reactor according to the present embodiment, it is preferable to provide two or more gas mixers 200 as shown in FIG. 6 in terms of a mixing effect of reactants. The spacing between the mixers 200 should be properly adjusted and arranged.

In addition, when two or more gas mixers 200 according to the present embodiment are formed, if the perforated holes of the first stage gas mixer and the second stage gas mixer are all configured with the same concentricity and coaxiality based on the center line inside the catalytic combustion reactor, Since a laminar flow is formed in the fluid, which is not suitable for mixing the fluid, it is preferable that the sizes of perforated holes of each of the plurality of gas mixers are different from each other.

The gas mixer 200 according to the third embodiment as described above may be implemented with, for example, stainless steel (SUS 310) or Inconel material.

7 is a diagram for explaining a first mesh layer and a second mesh layer according to an embodiment of the present invention.

Referring to FIG. 7 , the first mesh layer 300 may be positioned in front of the monolithic catalyst 400, and the second mesh layer 500 may be positioned in the rear end of the monolithic catalyst 400.

As shown in FIG. 7, the first mesh layer 300 and the second mesh layer 500 according to an embodiment of the present invention may be implemented in the same form, and the first and second mesh layers 300 and 500 ) may be formed with 50 to 200 mesh holes in order to minimize the generation of differential pressure.

The first mesh layer 300 may prevent laminar flow from being formed in a fluid when reactants enter the monolithic monolithic catalyst 400 using mesh holes, and may allow sufficient turbulent flow to be formed in the reactants.

As described above, the reactants can be uniformly distributed over the area of the monolithic catalyst 400 as they pass through the line mixer 100, the gas mixer 200, and the first mesh layer 300 to contact the monolithic catalyst. It is possible to improve the catalytic combustion reaction by suppressing hot spots and eddy currents in the channel.

8 is a three-dimensional view of a catalytic combustion reactor according to an embodiment of the present invention. As a result of the catalytic combustion experiment using the catalytic combustion reactor of the present invention as shown in FIG. 8, the formation of turbulence in the fluid from the gas mixer 200 increased, compared to the case of catalytic combustion without the configuration of the gas mixer 200. Turbulence mixing increased by 15%.

FIG. 9 is a diagram for comparing the shear force (pressure) of a small area where the pressure generated as raw materials are supplied is applied to each device inside the catalytic combustion reactor. Figure 9 (a) is a diagram showing the shear force when mixed raw materials (reactants) are supplied to a catalytic combustion device composed of only a mesh layer and a monolith catalyst (hereinafter, a first comparative example), and Figure 9 (b) ) is a diagram showing the shear force when mixed raw materials (reactants) are supplied to a catalytic combustion device composed of a line mixer, a mesh layer, and a monolith catalyst (hereinafter, a second comparative example), and FIG. 9 (c ) is a diagram showing the shear force when mixed raw materials (reactants) are supplied to the catalytic combustion reactor according to the present invention.

Referring to FIG. 9, in the first comparative example, a lot of shear force was applied around the mesh layer, but in the case of the second comparative example and the catalytic combustion reactor according to the present invention, the shear force was uniformly transmitted to all objects, so that in the internal reactor It can be seen that it can be used stably.

Fig. 10 is a diagram for comparing pressures when mixed raw materials reach each device inside the catalytic combustion reactor. Figure 10 (a) is a diagram showing the pressure when the raw material (reactant) mixed in the first comparative example is supplied, and Figure 10 (b) is the raw material (reactant) mixed in the second comparative example (reactant). ) is a diagram showing the pressure when supplied, and FIG. 10(c) is a diagram showing the pressure when mixed raw materials (reactants) are supplied to the catalytic combustion reactor according to the present invention.

And, Figure 11 is a diagram for explaining the speed of the fluid until the mixed raw material is supplied to the monolith catalyst. Figure 11 (a) is a diagram showing the speed when the raw material (reactant) mixed in the first comparative example is supplied, Figure 11 (b) is a graph showing the mixed raw material (reactant) in the second comparative example ) is a diagram showing the speed when supplied, and FIG. 11(c) is a diagram showing the speed when mixed raw materials (reactants) are supplied to the catalytic combustion reactor according to the present invention.

10 and 11, in the first comparative example, a dead zone to which fluid is not supplied is formed on the outer portion of the surface of the monolith catalyst, but in the case of the second comparative example and the catalytic combustion reactor according to the present invention, the monolith It can be confirmed that the fluid is uniformly supplied to the catalyst as a whole. In addition, in the first comparative example, the fluid passes at a high speed in the center of the mesh layer, but in the second comparative example and the catalytic combustion reactor according to the present invention, the velocity of the fluid is uniformly distributed. In addition, in the first comparative example, the reactants are properly mixed in the mesh layer at a speed lower than that of the second comparative example and the present invention, and in the case of the present invention, the reactants are mixed by reducing the speed of the reactants from the gas mixer 200 It can be seen that this is done properly.

12 is a diagram for comparing the intensity of turbulence when mixed raw materials pass through each device inside the catalytic combustion reactor. Referring to FIG. 12, it can be seen that the intensity of turbulence in Comparative Example 1 is mainly concentrated in the mesh layer, and then turbulent flow, not laminar flow, is also formed in the front part of the monolithic catalyst. In the case of the second comparative example, the intensity of turbulence increased in the mesh layer in the line mixer 100, and then the raw material was uniformly supplied to the monolith catalyst. In addition, in the case of the catalytic combustion reactor according to the present invention, the intensity of turbulence increased in the line mixer 100, and in particular, the intensity of turbulence also increased in the gas mixer 200, so that raw materials were uniformly supplied to the mesh layer and the front of the monolith catalyst. As a result, a constant laminar flow was created in the monolithic channel.

The above description of the present invention is for illustrative purposes, and those skilled in the art can understand that it can be easily modified into other specific forms without changing the technical spirit or essential features of the present invention. will be. Therefore, the embodiments described above should be understood as illustrative in all respects and not limiting. For example, each component described as a single type may be implemented in a distributed manner, and similarly, components described as distributed may be implemented in a combined form.

The scope of the present invention is indicated by the following claims, and all changes or modifications derived from the meaning and scope of the claims and equivalent concepts should be interpreted as being included in the scope of the present invention.

11: inlet
13: body
15: outlet
100: line mixer
200: gas mixer
300: first mesh layer
400: monolith catalyst
500: second mesh layer

Claims (11)

In the catalytic combustion reactor with improved fluidity,
A line mixer formed on an inlet into which gaseous reactants are introduced, mixing the reactants having various composition materials and passing the reactants into the catalytic combustion reactor;
A gas mixer for redistributing a flow path of the reactants passing through the line mixer;
A monolithic catalyst that promotes combustion of reactants passing through the gas mixer;
A mesh layer disposed at the front and rear ends of the monolith catalyst to form a turbulent flow in the flow path of the reactant,
The catalytic combustion reactor with improved fluidity, characterized in that the diameter of the inlet in which the line mixer is disposed is smaller than the diameter of the main body of the catalytic combustion reactor in which the catalyst and the mesh layer are disposed.
According to claim 1,
The line mixer,
An inlet region disposed toward the inlet through which the reactant is introduced;
Including a discharge area for discharging the introduced reactant toward the gas mixer side,
The inlet region has improved fluidity, characterized in that a plurality of inlet holes are formed in a circular shape along the circumference of the line mixer with a plurality of inlet holes spaced apart at a predetermined interval on one side disposed toward the inlet into which the reactant is introduced. catalytic combustion reactor.
According to claim 2,
The discharge area is
A step is formed such that a height from the one surface to a central portion of the discharge area is lower than a height from the one surface to an edge of the discharge area,
A catalytic combustion reactor with improved fluidity, characterized in that a plurality of discharge holes are formed at a predetermined interval on the inner surface of the edge formed by the step difference between the edge and the central portion.
According to claim 3,
The line mixer,
Further comprising a connection passage forming a passage for a reactant flowing through the inlet hole as it connects between the inlet hole and the outlet hole,
Catalytic combustion reactor with improved fluidity, characterized in that the angle of the connection passage is formed at least 45 ° or more.
According to claim 3,
The catalytic combustion reactor with improved fluidity, characterized in that the size of the discharge hole is formed to a size of 8% to 10% of the diameter of the body of the catalytic combustion reactor.
According to claim 1,
The gas mixer,
The exterior is formed in a cylindrical shape, and the inner tube is formed in a shape in which the diameter size decreases from both ends to the center,
The gas mixer,
A first-type mixer that rotates on an axis to forcibly mix the reactants flowing into the central portion;
A catalytic combustion reactor with improved fluidity, characterized in that it comprises a rotational shaft forming a shaft of the first-type mixer and connected to an external rotational gear to rotate the first-type mixer.
According to claim 6,
The first type mixer,
A ribbon mixer or a paddle mixer,
A catalytic combustion reactor with improved fluidity, characterized in that it rotates at a speed of 150 to 200 RPM.
According to claim 1,
The gas mixer,
formed in the shape of a cylinder,
In order to forcibly mix the reactants flowing into the central part, a second type mixer that rotates on an axis;
A rotation shaft forming a shaft of the second type mixer and connected to an external rotation gear to rotate the second type mixer;
The fluidity is improved, characterized in that it comprises an auxiliary mixer coupled to the second type mixer and the rotational shaft to transmit power so that the second type mixer can rotate itself independently of rotation by the rotational shaft. Catalytic Combustion Reactor.
According to claim 8,
The second type mixer,
Rotating at a speed of 100 to 500 RPM,
The auxiliary mixer,
A catalytic combustion reactor with improved fluidity, characterized in that it is formed as a rotary blade.
According to claim 1,
The gas mixer,
It is formed of a perforated plate including perforated holes spaced apart at predetermined intervals on the front surface,
A catalytic combustion reactor with improved fluidity, characterized in that the central perforated hole formed in the center of the perforated holes is formed differently from the size of the other perforated holes.
According to claim 1,
The mesh layer,
A catalytic combustion reactor with improved fluidity, characterized in that 50 to 200 mesh holes are formed.

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