Ammonia synthesis reactor

Abstract

The invention discloses an ammonia synthesis reactor which comprises at least one catalytic bed layer, at least one heat exchanger, a shell and a gas distributor, an inlet gas channel is formed between the outer wall of the catalytic bed layer and the inner wall of the shell; an outlet gas channel is formed between the inner wall of the catalytic bed and the outer wall of the heat exchanger; the gas distributor comprises at least one flow guide distribution element; the flow guide distribution element is a spiral strip-shaped body, and a mounting cavity is formed in the flow guide distribution element; the flow guide distribution element is mounted in the inlet gas channel and / or the outlet gas channel so as to form a spiral flow guide channel in the inlet gas channel and / or the outlet gas channel; according to the ammonia synthesis reactor, a spiral flow guide channel is provided for reaction gas in the gas channel, axial disturbance to the flowing reaction gas is increased, uneven distribution and gas bias flow of the reaction gas in the gas channel are prevented, then uneven temperature of the reaction gas in the ammonia synthesis reactor is avoided, and stable ammonia synthesis reaction is guaranteed.

Description

Technical Field

[0001] The invention relates to the field of chemical reaction equipment, in particular to an ammonia synthesis reactor. Background Art

[0002] The ammonia synthesis reactor is a key equipment for synthesizing ammonia, with a complex internal structure and high technical requirements. Due to the large size of the internal parts of the ammonia synthesis reactor, the axial gas in the tower is easily unevenly distributed, which will lead to a large temperature difference in the same plane. Uneven temperature in the same plane will cause uneven ammonia synthesis reaction and reduce the service life of the catalyst. One or more catalytic beds and heat exchangers in the catalytic beds inside the ammonia synthesis reactor are all axisymmetric structures. Uneven gas distribution may occur in various parts of the ammonia synthesis reactor. If uneven gas distribution occurs at the top of the ammonia synthesis reactor, the uneven distribution will not be alleviated during the downward flow, reaction and heat exchange of the gas, and the uneven temperature will continue and may be amplified with the flow of the gas. Summary of the invention

[0003] In order to enrich the product types of an ammonia synthesis reactor and enrich the selection space of gas distribution methods in an ammonia synthesis reaction, an embodiment of the present invention proposes an ammonia synthesis reactor.

[0004] An embodiment of the present invention provides an ammonia synthesis reactor, comprising at least one catalytic bed, at least one heat exchanger, a shell and a gas distributor;

[0005] An inlet gas channel is formed between the outer wall of the catalyst bed and the inner wall of the shell; an outlet gas channel is formed between the inner wall of the catalyst bed and the outer wall of the heat exchanger;

[0006] The gas distributor includes at least one flow distribution element;

[0007] The flow guide distribution element is a spiral strip body with an installation cavity formed inside;

[0008] The flow guide distribution element is installed in the inlet gas channel and / or the outlet gas channel to form a spiral flow guide channel in the inlet gas channel and / or the outlet gas channel.

[0009] In one or some optional embodiments, the gas distributor further comprises a plurality of guide distribution elements;

[0010] The plurality of guide distribution elements are evenly distributed in a circumferential shape at the inlet and / or outlet of the heat exchanger.

[0011] In one or some optional embodiments, the flow distribution element is fixed to the inner wall and / or outer wall of the catalytic bed.

[0012] In one or some optional embodiments, the volume of the flow distribution element does not exceed 1 / 2 of the inlet gas channel and / or the outlet gas channel.

[0013] In one or some optional embodiments, the strip spacing of the flow distribution element is 10 times to 50 times the width of the strip of the flow distribution element.

[0014] In one or some optional embodiments, the thickness of the strip body of the flow distribution element is 10%-60% of the radial width of the inlet gas channel or the outlet gas channel.

[0015] In one or some optional embodiments, the guiding distribution element is plate-shaped.

[0016] In one or some optional embodiments, the arrangement direction of a single guide distribution element is between the axial direction and the tangential direction of the outer wall of the heat exchanger.

[0017] In one or some optional embodiments, a single guide distribution element forms an angle of 30° to 60° with the tangent direction of the heat exchanger;

[0018] An included angle of 30° to 60° is formed between a single guide distribution element and the axial direction of the heat exchanger.

[0019] In one or some optional embodiments, the plurality of guiding distribution elements are arranged in a clockwise or counterclockwise direction.

[0020] In one or some optional embodiments, the plurality of guide distribution elements are symmetrically distributed with the center of the heat exchanger as the center point.

[0021] In one or some optional embodiments, the width of a single guide distribution element is 5%-10% of the outer diameter of the heat exchanger.

[0022] The beneficial effects of the above technical solution provided in the embodiments of the present invention include at least:

[0023] The ammonia synthesis reactor provided by the embodiment of the present invention provides a spiral guide channel for the reaction gas in the gas channel by arranging a guide distribution element in the inlet gas channel and / or the outlet gas channel, thereby increasing the axial disturbance of the flowing reaction gas, preventing the reaction gas from being unevenly distributed in the gas channel and gas deviation, thereby avoiding uneven temperature of the reaction gas in the ammonia synthesis reactor and ensuring stable progress of the ammonia synthesis reaction.

[0024] The ammonia synthesis reactor provided by the embodiment of the present invention provides a guide distribution element at the outlet or inlet of the heat exchanger, so that the reaction gas is mixed more evenly after passing through the guide distribution element, thereby reducing the axial uneven distribution of the reaction gas during the flow process.

[0025] Other features and advantages of the present invention will be described in the following description, and partly become apparent from the description, or understood by practicing the present invention. The purpose and other advantages of the present invention can be realized and obtained by the structures particularly pointed out in the written description and the accompanying drawings.

[0026] The technical solution of the present invention is further described in detail below through the accompanying drawings and embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the embodiments of the present invention, they are used to explain the present invention and do not constitute a limitation of the present invention. In the accompanying drawings:

[0028] Figure 1 This is a schematic diagram of the internal structure of an ammonia synthesis reactor provided in an embodiment of the present invention;

[0029] Figure 2 A schematic diagram of the structure of a flow guide distribution element provided in an embodiment of the present invention;

[0030] Figure 3 It is a schematic diagram of the expansion of the flow guide distribution element provided in an embodiment of the present invention;

[0031] Figure 4 A schematic diagram of the arrangement of flow guide distribution elements at an inlet gas channel provided in an embodiment of the present invention;

[0032] Figure 5 A schematic diagram of the arrangement of flow guide distribution elements at an outlet gas channel provided in an embodiment of the present invention;

[0033] Figure 6 A schematic diagram of the structure of a guide distribution element provided in an embodiment of the present invention;

[0034] Figure 7 A schematic diagram of the flow velocity distribution of a first gas provided in an embodiment of the present invention;

[0035] Figure 8 Schematic diagram of the flow rate distribution of the second gas provided in an embodiment of the present invention.

[0036] In the figure:

[0037] 1 is a catalytic bed, 2 is a heat exchanger, 21 is an inlet of the heat exchanger, 22 is an outlet of the heat exchanger, 3 is a shell, 4 is a flow guide distribution element, 5 is an inlet gas channel, 6 is an outlet gas channel, and 7 is a guide distribution element. DETAILED DESCRIPTION

[0038] The exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. Although the exemplary embodiments of the present disclosure are shown in the accompanying drawings, it should be understood that the present disclosure can be implemented in various forms and should not be limited by the embodiments set forth herein. On the contrary, these embodiments are provided to enable a more thorough understanding of the present disclosure and to fully convey the scope of the present disclosure to those skilled in the art.

[0039] In the description of the present invention, it should be noted that the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside", "far", "near", "front", "back" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance.

[0040] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0041] The inventors have discovered that the reaction gas in the ammonia synthesis reactor may deviate due to uneven catalyst activity and other reasons. After the deviate flow, the uneven distribution of the reaction gas will continue to accumulate during the gas flow, affecting the normal progress of the ammonia synthesis reaction.

[0042] Based on this, an embodiment of the present invention provides an ammonia synthesis reactor, which is described in detail below through specific embodiments.

[0043] Embodiment 1

[0044] The embodiment of the present invention provides an ammonia synthesis reactor, referring to Figure 1-Figure 5 As shown, it includes at least one catalytic bed 1, at least one heat exchanger 2, a shell 3 and a gas distributor;

[0045] An inlet gas channel 5 is formed between the outer wall of the catalyst bed 1 and the inner wall of the shell 3; an outlet gas channel 6 is formed between the inner wall of the catalyst bed 1 and the outer wall of the heat exchanger 2;

[0046] The gas distributor comprises at least one flow distribution element 4;

[0047] The flow distribution element 4 is a spiral strip-shaped body, and a mounting cavity is formed inside;

[0048] The flow guide distribution element 4 is installed in the inlet gas channel 5 and / or the outlet gas channel 6 to form a spiral flow guide channel in the inlet gas channel 5 and / or the outlet gas channel 6 .

[0049] In a specific embodiment, the number of catalyst beds 1 is generally 1-3, and the number of heat exchangers 2 is 1-3. In order to improve the uniformity of the reaction gas, a flow guide distribution element 4 can be separately provided at the inlet gas channel 5, or a flow guide distribution element 4 can be separately provided at the outlet gas channel 6, or a flow guide distribution element 4 can be provided at the inlet gas channel 5 and the outlet gas channel 6 at the same time, so that the reaction gas flows in the inlet gas channel 5 and / or the outlet gas channel 6 along the flow guide channel formed by the flow guide distribution element 4, increasing the axial disturbance of the gas and realizing uniform mixing and distribution of the reaction gas.

[0050] In a specific embodiment, referring to Figure 2 and Figure 3 As shown, the flow distribution element 4 is obtained by spirally bending a strip body, and the whole is spiral. The cross section of the strip body can be semicircular, rectangular, triangular, etc., which can be selected and set according to actual needs. In this embodiment, refer to Figure 1 , Figure 4 and Figure 5 As shown, the flow guide distribution element 4 is obtained by spirally bending a semicircular strip body with a cross section, so as to allow the reaction gas passing through to flow smoothly.

[0051] In a specific embodiment, the strip width of the diversion distribution element 4 can be determined according to the actual size of the ammonia synthesis reactor. If the strip width is too small, the diversion effect will not be obvious. If the strip width is too large, it will occupy too much space in the inlet gas channel 5 and / or the outlet gas channel 6, affecting the flow of the reaction gas. Therefore, the width can be set to 1cm-5cm. While not affecting the flow of the reaction gas, the reaction gas can be diverted, thereby making the reaction gas mixing more uniform.

[0052] In a specific embodiment, the upper and lower spacing of the strips of the flow-guiding distribution element 4 can be determined according to the actual size of the ammonia synthesis reactor and the width of the strips. To ensure that the reaction gas can flow smoothly, the upper and lower spacing of the strips should not be too narrow. Therefore, its size can be set to 10-50 times the width, which does not affect the flow of the reaction gas and makes the reaction gas mixing more uniform.

[0053] In a specific embodiment, the thickness of the strip of the flow-guiding distribution element 4 can be determined according to the actual size of the ammonia synthesis reactor and the size of the gas channel. In order to prevent the flow-guiding distribution element 4 from occupying too much space, the strip should not be too thick. Therefore, the thickness of the strip can be set to 10% or 60% of the radial width of the inlet gas channel 5 or the outlet gas channel 6, so that the reaction gas is mixed more evenly without occupying a large space.

[0054] In a specific embodiment, by reasonably setting the width, thickness and upper and lower spacing of the flow guide distribution element 4, the volume of the flow guide distribution element 4 does not exceed 1 / 2 of the inlet gas channel 5 and / or the outlet gas channel 6, and the space occupied by the flow guide distribution element 4 is controlled within a reasonable range to avoid obstructing the circulation of the reaction gas.

[0055] In a specific embodiment, referring to Figure 1 , Figure 4 and Figure 5 As shown, the flow distribution element 4 can be fixed to the inner wall and the outer wall of the catalyst bed 1 by welding, so as to prevent the flow distribution element 4 from loosening in the ammonia synthesis reactor. Obviously, the fixing method of the flow distribution element 4 is not limited to welding, and the details can be referred to in the prior art, which will not be repeated here.

[0056] The ammonia synthesis reactor provided in the embodiment of the present invention provides a spiral guide channel for the reaction gas in the gas channel by arranging the guide distribution element 4 in the inlet gas channel 5 and / or the outlet gas channel 6, thereby increasing the axial disturbance of the flowing reaction gas, preventing the reaction gas from being unevenly distributed in the gas channel and the gas from being biased, thereby avoiding uneven temperature of the reaction gas in the ammonia synthesis reactor and ensuring stable progress of the ammonia synthesis reaction.

[0057] In a specific embodiment, referring to Figure 1 and Figure 6 As shown, the gas distributor further includes a plurality of guide distribution elements 7, which are uniformly distributed in a circumferential shape at the heat exchanger inlet 21 and / or the heat exchanger outlet 22. A single guide distribution element 7 is plate-shaped and fixed to the side wall of the inlet section or outlet section of the heat exchanger 2, with a direction between the axial direction and the tangential direction of the side wall of the heat exchanger 2, so that the reaction gas changes its flow direction after passing through the heat exchanger outlet 22 or the heat exchanger inlet 21, realizes axial disturbance of the gas, and makes the reaction gas mixed more uniformly.

[0058] In a specific embodiment, a single guiding distribution element 7 may be in the shape of a rectangular plate, a semicircular plate, or a triangular plate, etc., and may be reasonably configured according to actual needs, and is not limited here.

[0059] In a specific embodiment, referring to Figure 6As shown, a single guide distribution element 7 forms an angle of 30° to 60° with the tangent direction of the heat exchanger 2, and forms an angle of 30° to 60° with the axial direction of the heat exchanger 2, so that the guide distribution element 7 can be changed while changing the flow direction of the reaction gas to avoid being too tilted to hinder the flow of the reaction gas, maximize the gas guiding effect, and make the reaction gas distribution more uniform. Obviously, the angle direction of the single guide distribution element 7 relative to the heat exchanger 2 is not limited to the above method, and can be adjusted according to the actual size of the ammonia synthesis reactor and the flow rate of the reaction gas.

[0060] In a specific embodiment, the height of a single guide distribution element 7 can be determined according to the size of the outlet gas channel 6 and the actual size of the heat exchanger 2. To ensure that the reaction gas can flow smoothly, the guide distribution element 7 should not be too high, preferably 5cm-20cm, so that the reaction gas is mixed more evenly without taking up a large space.

[0061] In a specific embodiment, the width of a single guide distribution element 7 can be determined according to the size of the outlet gas channel 6 and the outer diameter of the heat exchanger 2. In order to prevent the guide distribution element 7 from occupying too much space, the width of the guide distribution element 7 should not be too large and can be set to 5%-10% of the outer diameter of the heat exchanger 2. This allows the reaction gas to be mixed more evenly without occupying a large space.

[0062] In a specific embodiment, the thickness of a single guide distribution element 7 can be determined according to the actual size of the ammonia synthesis reactor and the outer diameter of the heat exchanger 2, and must also meet the installation requirements. If the guide distribution element 7 is too thin, it is not only not conducive to installation, but also lacks stability; if the guide distribution element 7 is too thick, it will occupy too much gas flow space and hinder gas circulation.

[0063] In a specific embodiment, the number of the guide distribution elements 7 can be set according to the actual size of the ammonia synthesis reactor and the flow rate of the reaction gas, and generally 6-20 guide distribution elements are set and evenly arranged along the circumference of the outer wall of the heat exchanger 2. Obviously, the number of the guide distribution elements 7 is not limited to 6-20, and can be adjusted according to actual conditions.

[0064] In a specific embodiment, referring to Figure 6 As shown, the plurality of guide distribution elements 7 can be arranged in a clockwise direction or a counterclockwise direction at the heat exchanger outlet 22, and can be arranged in a clockwise direction or a counterclockwise direction at the heat exchanger inlet 21. The specific arrangement can be reasonably made according to the actual situation, and is not limited here. For example, the heat exchanger outlet 22 can be arranged in a clockwise direction, and the heat exchanger inlet 21 can be arranged in a clockwise direction to enhance the gas guiding effect.

[0065] In a specific embodiment, referring to Figure 6As shown, the plurality of guide distribution elements 7 must be symmetrically distributed around the center of the heat exchanger 2 to avoid biased flow of the reaction gas.

[0066] In a specific embodiment, the methods of fixing the plurality of guide distribution elements 7 to the outer wall of the heat exchanger 2 include but are not limited to welding, bolt connection, etc., as long as the guide distribution elements 7 can be firmly fixed. For details, please refer to the detailed records in the prior art, which will not be repeated here.

[0067] In a specific embodiment, the material of the flow distribution element 4 and the guide distribution element 7 can be high temperature resistant stainless steel. For details, please refer to the detailed records in the prior art, which will not be repeated here.

[0068] In the embodiment of the present invention, the specific process of the ammonia synthesis reactor for ammonia synthesis production may include: the reaction gas is introduced into the ammonia synthesis reactor to reach the inlet gas channel 5, flows along the guide distribution element 4 in the inlet gas channel 5 to be evenly mixed, and then enters the catalyst bed 1 from the inlet gas channel 5 for catalytic reaction, exits the catalyst bed 1 after the reaction, reaches the outlet gas channel 6, enters the heat exchanger 2 after passing through the guide distribution element 7 at the inlet 21 of the heat exchanger, and then enters the next process after passing through the guide distribution element 7 at the inlet 21 of the heat exchanger. The inventors have calculated through simulation that when the unevenness of the inlet gas in the same plane is 5% (the ratio of the maximum point to the minimum point flow), the unevenness can be reduced to less than 0.5%.

[0069] The ammonia synthesis reactor provided in the embodiment of the present invention increases the axial disturbance of the flowing reaction gas by arranging the guide distribution element 4 in the inlet gas channel 5 and / or the outlet gas channel 6 and arranging the guide distribution element 7 at the heat exchanger outlet 22 or the heat exchanger inlet 21, so that the reaction gas is mixed more evenly after passing through the guide distribution element 7, removes or weakens the gas inhomogeneity, prevents the reaction gas from deviating in the gas channel, and thus avoids the uneven temperature of the reaction gas in the ammonia synthesis reactor, thereby ensuring the stable progress of the ammonia synthesis reaction.

[0070] Embodiment 2

[0071] In order to explain the present invention more clearly and in detail, an embodiment of the present invention further provides an ammonia synthesis reactor, comprising three catalytic beds 1, two heat exchangers 2, a shell 3 and a gas distributor;

[0072] The gas distributor comprises a flow distribution element 4 .

[0073] The output of the ammonia synthesis reactor provided in this embodiment is 1 million tons / year. The overall diameter of the ammonia synthesis reactor is 3.2m, the outer diameter of the middle catalytic bed 1 is 3.06m, and the height is 7.2m. The inlet gas channel 5 on the inner wall of the middle catalytic bed 1 is provided with a flow distribution element 4 with a width of 40mm and a height of 20mm. The upper and lower spacing of the flow distribution element 4 is 360mm, and the entire wall plate is provided with 10 circles. Figure 7 As shown, finite element models are established for the cases where the flow guide distribution element 4 is set and the cases where the flow guide distribution element 4 is not set. After comparison, it can be obtained that: when the flow guide distribution element 4 is not set, the velocity difference at the 10°C position and the 180°C position of the middle catalytic bed is large. After the flow guide distribution element 4 is set, the velocity distribution at the two positions is basically the same. Furthermore, it can be calculated that: when the flow unevenness of the inlet gas channel 5 is 10%, the unevenness in the outlet gas channel 6 can be reduced to 1.3%.

[0074] Embodiment 3

[0075] In order to explain the present invention more clearly and in detail, an embodiment of the present invention further provides an ammonia synthesis reactor, comprising three catalytic beds 1, two heat exchangers 2, a shell 3 and a gas distributor;

[0076] A heat exchanger 2 is provided in the middle catalyst bed 1;

[0077] The gas distributor comprises a flow distribution element 4 .

[0078] The ammonia synthesis reactor provided in this embodiment has an annual output of 180,000 tons, and the overall diameter of the ammonia synthesis reactor is 1.8 m. A guide distribution element 7 is provided at the outlet of the heat exchanger 2 inside the middle catalytic bed 1. The guide distribution element 7 has a width of 50 mm, a height of 100 mm, and an angle of 45 degrees tangential to the outer wall of the heat exchanger 2. Ten guide distribution elements 7 are provided along the circumferential direction of the heat exchanger 2. After the reaction gas flows out of the heat exchanger 2 in the middle catalytic bed 1, the flow uniformity is improved, and the gas is mixed evenly before entering the next catalytic bed 1 for reaction, which can improve the distribution uniformity. Figure 8 As shown, finite element models are established for the cases where the guide distribution element 7 is set and the cases where the guide distribution element 7 is not set, respectively. After comparison, it can be obtained that: when the guide distribution element 7 is not set, the velocity difference at the 0°C position and the 180°C position at the outlet of the heat exchanger 2 in the middle catalytic bed 1 is large. After the guide distribution element 7 is set, the velocity distributions at the two locations are basically consistent. Furthermore, it can be calculated that: the degree of unevenness of the gas flow before flowing through the guide distribution element 7 is 5%, and the degree of unevenness of the gas flow after flowing through the guide distribution element 7 can be reduced to 0.5%.

[0079] Obviously, various changes and modifications may be made to the present invention by those skilled in the art without departing from the spirit and scope of the present invention. The present disclosure is not limited to the precise structure described above and shown in the accompanying drawings, and various changes and modifications may be made without departing from the scope thereof. The scope of the present disclosure is limited only by the appended claims. Thus, if these changes and modifications of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these changes and modifications.

Claims

1. An ammonia synthesis reactor, characterized in that: comprising at least one catalytic bed, at least one heat exchanger, a housing and a gas distributor; An inlet gas channel is formed between the outer wall of the catalyst bed and the inner wall of the shell; an outlet gas channel is formed between the inner wall of the catalyst bed and the outer wall of the heat exchanger; The gas distributor includes at least one flow distribution element; The flow guide distribution element is a spiral strip body with an installation cavity formed inside; The flow guide distribution element is installed in the inlet gas channel and / or the outlet gas channel to form a spiral flow guide channel in the inlet gas channel and / or the outlet gas channel.

2. The ammonia synthesis reactor according to claim 1, characterized in that: The gas distributor also includes a plurality of guide distribution elements; The plurality of guide distribution elements are evenly distributed in a circumferential shape at the inlet and / or outlet of the heat exchanger.

3. The ammonia synthesis reactor according to claim 1, characterized in that: The flow guide distribution element is fixed to the inner wall and / or outer wall of the catalytic bed.

4. The ammonia synthesis reactor according to claim 1, characterized in that: The volume of the flow distribution element does not exceed 1 / 2 of the inlet gas channel and / or the outlet gas channel.

5. The ammonia synthesis reactor according to claim 1, characterized in that: The strip spacing of the flow distribution element is 10 to 50 times the width of the strip of the flow distribution element.

6. The ammonia synthesis reactor according to claim 1, characterized in that: The strip thickness of the flow distribution element is 10%-60% of the radial width of the inlet gas channel or the outlet gas channel.

7. The ammonia synthesis reactor according to claim 2, characterized in that: The guiding and distributing element is in a plate shape.

8. The ammonia synthesis reactor according to claim 7, characterized in that: The arrangement direction of a single guide distribution element is between the axial direction and the tangential direction of the outer wall of the heat exchanger.

9. The ammonia synthesis reactor according to claim 8, characterized in that: An angle of 30° to 60° is formed between a single guide distribution element and the tangent direction of the heat exchanger; An included angle of 30° to 60° is formed between a single guide distribution element and the axial direction of the heat exchanger.

10. The ammonia synthesis reactor according to claim 9, characterized in that: The plurality of guiding distribution elements are arranged in a clockwise or counterclockwise direction.

11. The ammonia synthesis reactor according to claim 10, characterized in that: The plurality of guide distribution elements are centrally symmetrically distributed with the center of the heat exchanger as the center point.

12. The ammonia synthesis reactor according to claim 2, characterized in that: The width of a single guide distribution element is 5%-10% of the outer diameter of the heat exchanger.

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