Green ammonia synthesis column gas distributor and green ammonia synthesis column

Abstract

The present application relates to green ammonia synthesis technical field, disclose green ammonia synthesis tower gas distributor and green ammonia synthesis tower, wherein the green ammonia synthesis tower gas distributor, it mainly includes: orifice plate assembly, flow guide assembly, flow rate detector and controller, orifice plate assembly is equipped with a plurality of orifice plates, a plurality of through holes are formed on each orifice plate, flow guide assembly includes a plurality of flow guide vanes, a plurality of flow guide vanes are spaced apart along the circumference of the tower body, one end of each flow guide vane is connected with the first driving member through the transmission part;The controller is electrically connected with the first driving member, flow rate detector respectively, is configured to control the first driving member to drive the transmission part based on the size of the inlet air flow rate, to adjust the included angle between the flow guide vane and the radial of the tower body.The green ammonia synthesis tower gas distributor of the present application can effectively control the airflow velocity impacting the surface of the catalyst bed, reduce the risk of catalyst particle breakage and pulverization, reduce catalyst bed wear, thereby reducing production cost and improving production efficiency.

Description

Technical Field

[0001] This invention relates to the field of green ammonia synthesis technology, specifically to a gas distributor for a green ammonia synthesis tower and a green ammonia synthesis tower. Background Technology

[0002] In the green ammonia synthesis industry, the fixed-bed catalytic reactor (i.e., the synthesis tower) is the core equipment of the entire process. The uniformity of gas distribution in the catalyst bed directly determines the reaction conversion efficiency, catalyst lifespan, and continuous operation cycle of the unit. To simplify the equipment structure and reduce manufacturing costs and installation difficulty, in existing technologies, whether it is a conventional large-scale ammonia synthesis tower or an emerging skid-mounted green ammonia synthesis tower, the feed gas is usually introduced from the central inlet at the top of the tower or the upper side wall of the tower body and then directly impacts the upper surface of the catalyst bed.

[0003] However, the flow velocity of the feed gas at the inlet can typically reach 15 m / s to 25 m / s. After the gas flow directly impacts the surface of the catalyst bed, the catalyst particles in localized areas of the bed are easily worn down under the continuous high-speed gas flow shearing and collision, resulting in breakage and pulverization. The fine powder generated by catalyst wear gradually fills the pore channels inside the bed, reducing the effective flow area and causing a rapid increase in bed pressure differential. Therefore, frequent bed sieving and cleaning or surface catalyst replenishment are required, significantly increasing equipment maintenance costs and catalyst consumption, and reducing the production efficiency of green ammonia synthesis. Summary of the Invention

[0004] This invention provides a gas distributor and a green ammonia synthesis tower to solve the problem that the inlet flow rate of the raw material gas in the green ammonia synthesis tower is too high, directly impacting the catalyst bed, which easily causes the catalyst particles to break and pulverize, resulting in increased operating costs and reduced production efficiency.

[0005] In a first aspect, the present invention provides a gas distributor for a green ammonia synthesis tower, the gas distributor for the green ammonia synthesis tower being adapted to be installed inside the green ammonia synthesis tower along the flow direction of the raw material gas, the gas distributor for the green ammonia synthesis tower comprising, in sequence, an orifice plate assembly and a flow guiding assembly; The orifice plate assembly is provided with multiple orifice plates at intervals along the flow direction of the raw gas, and each orifice plate is provided with multiple through holes. The orifice plate assembly is used to reduce the flow rate of the raw gas. The flow guiding assembly includes multiple flow guiding blades, which are distributed circumferentially along the tower body to guide the raw material gas to diffuse radially along the tower body of the green ammonia synthesis tower and flow to the catalyst bed inside the green ammonia synthesis tower. One end of each flow guiding blade is connected to the first driving component through a transmission part, and each flow guiding blade is inclined toward the catalyst bed. The gas distributor of the green ammonia synthesis tower also includes a flow rate detector and a controller. The flow rate detector is adapted to be installed at the feed inlet of the green ammonia synthesis tower to detect the inlet flow rate of the raw material gas. The controller is electrically connected to the first drive unit and the flow rate detector respectively. The controller is configured to control the first drive unit to drive the transmission unit based on the magnitude of the inlet flow rate to adjust the included angle between the guide vanes and the radial direction of the tower body.

[0006] Beneficial effects: The gas distributor of the green ammonia synthesis tower of the present invention initially slows down and uniformly diffuses the raw gas through the orifice plate assembly, and guides the raw gas radially along the tower body using the flow guiding assembly. With the help of the flow velocity detector and controller, it can automatically adjust the tilt angle of the flow guide vanes according to the magnitude of the inlet flow velocity. When the inlet flow velocity is low, it can improve the radial diffusion capacity of the flow guide vanes. When the inlet flow velocity is high, it can increase the resistance of the flow guide vanes to the raw gas and guide the airflow to diffuse rapidly. This reduces the force of the airflow impacting the catalyst bed, effectively controls the force of the raw gas impacting the catalyst bed, significantly reduces the risk of catalyst particle breakage and pulverization caused by violent collisions, reduces catalyst wear, alleviates the problem of bed pore blockage, thereby reducing maintenance costs and catalyst consumption, and significantly improving the production efficiency of green ammonia synthesis.

[0007] In one alternative implementation, the controller is configured to control the angle between the guide vanes and the radial direction of the tower body to be negatively correlated with the intake air velocity.

[0008] Beneficial effects: When the inlet gas velocity is high, corresponding to high output load conditions, the radial angle between the guide vanes and the tower body is reduced, increasing the contact area between the guide vanes and the gas flow, thus increasing resistance and reducing the impact force of the gas flow on the catalyst bed. When the inlet gas velocity is low, corresponding to low output load conditions, the radial angle between the guide vanes and the tower body is increased. This increases the radial diffusion capacity of the gas flow while reducing the resistance of the guide vanes to the gas flow, preventing gas flow deviation under low output load conditions, which could lead to localized impact on the catalyst, exacerbate local wear, and reduce reaction efficiency.

[0009] In one alternative embodiment, the orifice ratio on the orifice plate gradually decreases along the flow direction of the feed gas, and the orifice plate assembly is used to progressively reduce the flow rate of the feed gas.

[0010] Beneficial effects: By limiting the orifice plate opening ratio to decrease along the airflow direction, the feed gas is decelerated step by step, which can gradually reduce the flow rate of the feed gas at the top of the tower, weaken the impact energy of the airflow on the catalyst bed, and at the same time, initially distribute the airflow evenly, avoid the formation of local high-speed zones, and significantly reduce the wear risk of the catalyst bed.

[0011] In one optional embodiment, the orifice plate assembly includes a first sub-plate, a second sub-plate, and a third sub-plate sequentially along the flow direction of the raw gas, wherein the orifice ratio of the first sub-plate is Φ1, the orifice ratio of the second sub-plate is Φ2, and the orifice ratio of the third sub-plate is Φ3, satisfying 30%≤Φ1≤40%, 20%≤Φ2≤30%, and 10%≤Φ3≤20%.

[0012] Beneficial effects: By setting up a first, second, and third sub-plate with successively decreasing opening ratios, the high-speed airflow at the feed inlet can be smoothly and progressively reduced, avoiding airflow rebound, turbulence, or local energy concentration caused by a sudden increase in resistance. The first sub-plate initially distributes and decelerates the high-speed airflow, the second sub-plate further decelerates it and eliminates local high-speed zones, and the third sub-plate achieves precise speed control.

[0013] In one optional embodiment, the orifice plate assembly includes at least three orifice plates, each orifice plate having a through hole of the same size. Along the flow direction of the raw gas, at least one orifice plate in the middle is connected to a rotating shaft, and the rotating shaft is connected to a second driving member, which drives the rotating shaft to rotate the corresponding orifice plate.

[0014] Beneficial effects: It limits the number of orifice plates to at least three, and the middle orifice plate is adjustable, which can dynamically adjust the degree of overlap of the through holes between the orifice plates to adapt to the deceleration requirements under different airflow velocities and improve the flexibility of use.

[0015] In one alternative embodiment, the second drive member is electrically connected to the controller, which is configured to control the orifice plate connected to the rotating shaft to rotate to a first position when the inlet air velocity detected by the flow velocity detector is smaller, and to control the orifice plate connected to the rotating shaft to rotate to a second position when the inlet air velocity detected by the flow velocity detector is larger. At the first position, along the flow direction of the raw gas, the projection of the through hole on the orifice plate connected to the rotating shaft at least partially overlaps with the projection of the through hole on the adjacent orifice plate; In the second position, along the flow direction of the raw gas, the projections of the through holes on the orifice plate connected to the rotating shaft are misaligned with the projections of the through holes on the adjacent orifice plates.

[0016] Beneficial effects: When the orifice plate is rotated to the first position at a lower flow rate, corresponding to a low output load, the through holes of adjacent orifice plates at least partially overlap, allowing some airflow to directly pass through the overlapping part and flow directly to the guide vanes, reducing the resistance of the orifice plate to the airflow. At a higher flow rate, corresponding to a high output load, the orifice plate is rotated to the second position, causing the through holes of adjacent orifice plates to be misaligned, increasing the resistance of the orifice plate to the airflow, lengthening the airflow path, enhancing the deceleration effect, further optimizing the uniform distribution of flow velocity on the catalyst bed surface under different inlet flow rates, and reducing the wear rate.

[0017] In one optional embodiment, along the flow direction of the raw gas, a base is provided at one end of the rotating shaft near the downstream orifice plate, the base is connected to the downstream orifice plate, and the downstream orifice plate is fixedly connected to the inner wall of the tower body.

[0018] Beneficial effects: By limiting the connection between the rotating shaft and the downstream orifice plate through the base, the downstream orifice plate can support the rotating shaft and the base, ensuring that the rotatable orifice plate is installed firmly and rotates reliably, and maintaining the stability of the orifice plate assembly in terms of gradual deceleration and uniform airflow.

[0019] In one alternative embodiment, the downstream orifice plate, the guide vane, and the inner wall of the tower body form a buffer cavity.

[0020] Beneficial effects: By forming a buffer cavity between the downstream orifice plate, the guide vanes and the inner wall of the tower, the airflow that has been slowed down by the orifice plate assembly can be fully mixed in the buffer cavity, eliminating local high-speed zones, reducing the direct impact of the airflow on the guide vanes, and ensuring that the airflow velocity distribution reaching the guide assembly is uniform.

[0021] In one optional embodiment, the height of the buffer chamber is H along the flow direction of the raw gas, satisfying 50mm≤H≤100mm.

[0022] Beneficial effects: By controlling H within a suitable range, the airflow can be sufficiently decelerated and mixed in the buffer chamber, avoiding insufficient airflow mixing due to an insufficient height of the buffer chamber, and avoiding wasted space due to an excessively large height of the buffer chamber.

[0023] Secondly, the present invention also provides a green ammonia synthesis tower, comprising: The tower body is equipped with a feed inlet for the raw material gas and a power system; A new energy power generation device is used to generate electrical energy. The new energy power generation device is electrically connected to the power system to provide power to the power system. The inlet flow rate of the raw material gas is positively correlated with the output load of the new energy power generation device. The aforementioned green ammonia synthesis tower gas distributor is located inside the tower body along the flow direction of the raw material gas. The tower body also contains a catalyst bed located downstream of the flow guiding component.

[0024] Beneficial Effects: The green ammonia synthesis tower of this invention is powered by a new energy power generation system. Affected by fluctuations in the output load of the new energy power generation equipment, the inlet gas flow rate fluctuates accordingly. The flow guiding components within the tower can adaptively adjust the airflow distribution according to load changes. The orifice plate assembly initially slows down and uniformly diffuses the raw gas. The flow guiding components guide the raw gas radially along the tower body. Combined with a flow velocity detector and controller, the tilt angle of the guide vanes can be automatically adjusted according to the inlet gas flow rate, i.e., the output load of the new energy power generation equipment. This enhances the radial diffusion capacity of the guide vanes when the inlet gas flow rate is low (i.e., under low output load conditions), and increases the resistance of the guide vanes to the raw gas when the inlet gas flow rate is high (i.e., under high output load conditions), guiding the airflow to diffuse rapidly. This reduces the force of the airflow impacting the catalyst bed, effectively controlling the impact force of the raw gas on the catalyst bed, significantly reducing the risk of catalyst particle breakage and pulverization due to violent collisions, alleviating bed pore blockage problems, thereby reducing maintenance costs and catalyst consumption, and significantly improving the production efficiency of green ammonia synthesis. Attached Figure Description

[0025] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0026] Figure 1 This is a schematic diagram of a green ammonia synthesis tower according to an embodiment of the present invention; Figure 2 This is another schematic diagram of a green ammonia synthesis tower according to an embodiment of the present invention; Figure 3 This is a top view of a first type of orifice plate in a green ammonia synthesis tower according to an embodiment of the present invention; Figure 4 This is a top view of a second type of orifice plate in a green ammonia synthesis tower according to an embodiment of the present invention; Figure 5 This is a top view of a third type of orifice plate in a green ammonia synthesis tower according to an embodiment of the present invention; Figure 6 This is a top view of a fourth type of orifice plate in a green ammonia synthesis tower according to an embodiment of the present invention; Figure 7 This is a schematic diagram of a flow guiding component of a green ammonia synthesis tower according to an embodiment of the present invention.

[0027] Explanation of reference numerals in the attached figures: 1. Tower body; 101. Feed inlet; 2. Orifice plate assembly; 201. Orifice plate; 2011. First sub-plate; 2012. Second sub-plate; 2013. Third sub-plate; 202. Through hole; 203. Rotating shaft; 204. Base; 3. Flow guiding assembly; 301. Flow guiding blades; 302. Transmission unit; 303. Mounting frame; 4. Catalyst bed; 5. Buffer chamber. Detailed Implementation

[0028] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0029] When the green ammonia synthesis tower utilizes renewable energy sources such as wind power for electricity, the inlet gas flow rate is easily affected by fluctuations in the output load of the renewable energy power generation equipment, which varies between 20% and 110%. When the output load is 40%, the feed gas flow rate is approximately 2200 Nm³. 3 The inlet gas velocity is approximately 7.4 m / s; when the output load is 110%, the feed gas flow rate is approximately 6050 Nm³ / h. 3 / h, the intake airflow velocity is approximately 20.4 m / s.

[0030] Currently, green ammonia synthesis towers generally use a single-layer grid or a simple radial distributor as the inlet gas distribution structure. After the feed gas is introduced from the top or side wall of the tower, it passes through the inlet gas distribution structure and directly impacts the surface of the catalyst bed. Under low input load conditions, the inlet gas velocity is significantly reduced, making it difficult to maintain effective radial diffusion. This causes the gas flow to deflect to one side, which exacerbates local wear on the catalyst bed and reduces reaction efficiency. Under high input load conditions, the inlet gas velocity is significantly increased, and the impact force of the gas flow on the catalyst bed increases sharply, further worsening the erosion and wear of the catalyst bed.

[0031] Tests revealed that the annual catalyst wear rate of traditional green ammonia synthesis towers can reach over 8%, and the annual increase in bed pressure difference exceeds 15%. In severe cases, the towers need to be shut down for cleaning the sieve powder or replenishing the surface catalyst in less than 6 months, significantly shortening the effective operating time.

[0032] The following is combined with Figures 1 to 7 The following describes embodiments of the present invention.

[0033] According to an embodiment of the present invention, in one aspect, a gas distributor for a green ammonia synthesis tower is provided, suitable for skid-mounted, miniaturized green ammonia synthesis towers with wide load fluctuations. The gas distributor is located inside the green ammonia synthesis tower. The tower body of the green ammonia synthesis tower is an axial or radial flow ammonia synthesis reactor, with an operating pressure of approximately 7 MPa to 15 MPa, and a catalyst bed temperature of approximately 330 °C to 530 °C, compatible with various ammonia synthesis catalysts such as iron-based, ruthenium-based, and cobalt-based catalysts.

[0034] For ease of description later, refer to Figure 1 The flow direction of the raw material gas in the green ammonia synthesis tower is defined as a vertical direction from top to bottom. The tower body 1 of the green ammonia synthesis tower is cylindrical in shape, and the radial direction of the tower body 1 is a horizontal direction perpendicular to the vertical direction.

[0035] Reference Figure 1 Along the flow direction of the raw gas, the gas distributor of the green ammonia synthesis tower includes an orifice plate assembly 2 and a flow guiding assembly 3 in sequence.

[0036] The orifice plate assembly 2 is provided with multiple orifice plates 201 spaced apart along the flow direction of the raw gas. Each orifice plate 201 has multiple through holes 202. The orifice plate assembly 2 is used to reduce the flow rate of the raw gas. The material of the orifice plate 201 can be metal plate, plastic plate, etc., as needed.

[0037] The flow guiding assembly 3 includes multiple flow guiding blades 301, which are spaced apart circumferentially along the tower body 1. These blades guide the raw material gas radially along the tower body 1 and uniformly flow towards the catalyst bed 4 within the green ammonia synthesis tower, while also reducing the gas flow velocity. One end of each flow guiding blade 301 is connected to a first driving component (not shown in the figure) via a transmission unit 302, and each flow guiding blade 301 is inclined towards the catalyst bed 4. The material of the flow guiding blades 301 can be metal plates, plastic plates, etc., as needed, and the number of flow guiding blades 301 can be two, three, or more, as needed. The first driving component can be a drive motor, and the transmission unit 302 can be any existing structure, such as a telescopic rod, linkage mechanism, etc.

[0038] The gas distributor for the green ammonia synthesis tower also includes a flow rate detector and a controller (not shown in the figure).

[0039] A flow rate detector is installed at the feed inlet 101 of the green ammonia synthesis tower to detect the flow rate of the raw material gas at the feed inlet 101.

[0040] The controller is electrically connected to the first drive unit and the flow rate detector, respectively. The controller is configured to control the first drive unit to drive the transmission unit 302 based on the inlet airflow velocity, thereby adjusting the radial angle between the guide vane 301 and the tower body 1. The radial angle between the guide vane 301 and the tower body 1 is an acute angle, which is also the angle θ between the upper surface of the guide vane 301 and the horizontal plane. Figure 1 and Figure 2 As shown. The range of the included angle θ can be selected and set as needed, for example, from 15° to 45°.

[0041] Therefore, the gas distributor for the green ammonia synthesis tower provided in this embodiment of the invention initially slows down and uniformly diffuses the raw material gas through the orifice plate assembly 2, and guides the raw material gas radially along the tower body 1 using the flow guiding assembly 3. With the help of the flow rate detector and controller, it can automatically adjust the tilt angle of the guide vanes 301 according to the magnitude of the inlet flow rate. When the inlet flow rate is low, it can improve the radial diffusion capacity of the guide vanes 301. When the inlet flow rate is high, it can increase the resistance of the guide vanes 301 to the raw material gas and guide the airflow to diffuse rapidly, thereby reducing the force of the airflow impacting the catalyst bed 4. It effectively controls the force of the raw material gas impacting the catalyst bed 4, significantly reduces the risk of catalyst particles breaking and pulverizing due to violent collisions, reduces catalyst wear, alleviates the problem of bed pore blockage, thereby reducing maintenance costs and catalyst consumption, and significantly improving the production efficiency of green ammonia synthesis.

[0042] It should be noted that the controller can be any existing controller as needed. For example, the controller can be a microcontroller unit (MCU), a central processing unit (CPU), an electronic control unit (ECU), or other existing controllers. Of course, other conventional controllers can also be selected as needed. This embodiment of the invention does not impose any limitations on this.

[0043] In addition, the flow velocity detector can select any existing detector that can detect gas flow velocity as needed. For example, the flow velocity detector can select existing flow velocity detectors such as thermal flow velocity sensor (measures flow velocity based on the principle of heat transfer), ultrasonic flow velocity sensor (measures flow velocity by utilizing the time difference of sound wave propagation in fluid), electromagnetic flow velocity sensor (measures the flow velocity of conductive fluid based on the principle of Faraday's electromagnetic induction), and mechanical impeller flow velocity sensor (measures flow velocity by the fluid driving the impeller to rotate).

[0044] Specifically, the controller is configured to control the radial angle between the guide vane 301 and the tower body 1 to be negatively correlated with the inlet air velocity. The higher the inlet air velocity, the smaller the radial angle between the guide vane 301 and the tower body 1. The lower the inlet air velocity, the larger the radial angle between the guide vane 301 and the tower body 1.

[0045] Reference Figure 2When the inlet air velocity is large, corresponding to the high output load condition, the included angle between the guide vane 301 and the radial direction of the tower body 1 is reduced, the contact area between the guide vane 301 and the airflow is increased, the resistance is increased, thereby reducing the impact force of the airflow on the catalyst bed 4.

[0046] Reference Figure 1 When the inlet air velocity is low, corresponding to low output load conditions, the radial angle between the guide vane 301 and the tower body 1 is increased. This increases the radial diffusion capacity of the airflow and reduces the resistance of the guide vane 301 to the airflow, preventing airflow deviation under low output load conditions, which could lead to local impact on the catalyst, aggravate local wear, and reduce reaction efficiency.

[0047] It should be noted that the embodiments of the present invention do not limit the specific structure of the perforated plate 201, and any existing structure can be selected as needed.

[0048] Furthermore, there are no restrictions on the shape of the through holes 202 on the perforated plate 201. Any existing shape can be selected as needed. For example, the through hole 202 can be a round hole, a triangular hole, a rectangular hole, an elliptical hole, etc.

[0049] For example, refer to Figure 6 The perforated plate 201 can be a grid, and the through holes 202 are triangular holes arranged in even rows.

[0050] In one embodiment, the orifice ratio on the orifice plate 201 gradually decreases along the flow direction of the raw gas, and the orifice plate assembly 2 is used to progressively reduce the flow velocity of the raw gas. The orifice ratio refers to the proportion of the total open area of ​​each through hole 202 on the orifice plate 201 to the total area of ​​the entire orifice plate 201. The smaller the orifice ratio, the smaller the area through which the airflow passes, the greater the obstruction to the airflow, and the faster the airflow velocity decreases.

[0051] The opening ratio of the orifice plate 201 decreases along the airflow direction, thereby gradually slowing down the feed gas. This reduces the flow rate of the feed gas at the top of the tower, weakens the impact energy of the airflow on the catalyst bed 4, and initially evenly distributes the airflow, avoiding the formation of local high-speed zones and significantly reducing the wear risk of the catalyst bed 4.

[0052] Furthermore, in one embodiment, referring to Figures and Figure 2 The orifice plate assembly 2 includes a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013 in sequence along the flow direction of the raw gas. The orifice ratio of the first sub-plate 2011 is Φ1, the orifice ratio of the second sub-plate 2012 is Φ2, and the orifice ratio of the third sub-plate 2013 is Φ3, satisfying 30%≤Φ1≤40%, 20%≤Φ2≤30%, 10%≤Φ3≤20%, and Φ1>Φ2>Φ3.

[0053] By setting up a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013 with sequentially decreasing opening ratios, the high-speed airflow from the feed inlet 101 can be smoothly and gradually reduced in speed, avoiding airflow rebound, turbulence, or local energy concentration caused by a sudden increase in resistance. The first sub-plate 2011 initially distributes and decelerates the high-speed airflow, the second sub-plate 2012 further decelerates the airflow and eliminates local high-speed zones, and the third sub-plate 2013 achieves precise speed control.

[0054] For example, in this embodiment of the invention, Φ1 can be any value among 30%, 35%, and 40%, or a value between any two values. Φ2 can be any value among 20%, 25%, and 30%, or a value between any two values. Φ3 can be any value among 10%, 15%, and 20%, or a value between any two values.

[0055] For example, the opening ratio Φ1 of the first sub-plate 2011 is 35%, the opening ratio Φ2 of the second sub-plate 2012 is 25%, and the opening ratio Φ3 of the third sub-plate 2013 is 15%. Each perforated plate 201 is made of stainless steel with a thickness of 2 mm to 4 mm, preferably 3 mm, and the spacing between adjacent perforated plates 201 is 30 mm to 50 mm, preferably 40 mm. The through holes 202 are round holes with a diameter of 4 mm to 8 mm, preferably 6 mm. The perforated plates 201 are fixed to the inner wall of the tower body 1 by support rods.

[0056] Furthermore, in one embodiment, reference is made to... Figure 1 and Figure 2 The orifice plate assembly 2 includes at least three orifice plates 201, each with a through hole 202 of the same size. Along the flow direction of the raw gas, at least one orifice plate 201 in the middle is connected to a rotating shaft 203. The rotating shaft 203 is connected to a second driving member (not shown in the figure). The second driving member drives the rotating shaft 203 to rotate the corresponding orifice plate 201 around its vertical axis. The second driving member can be a drive motor.

[0057] The system defines at least three perforated plates 201, with at least one of the middle perforated plates 201 being adjustable. This allows for dynamic adjustment of the overlap of the through holes 202 between the perforated plates 201, adapting to deceleration requirements under different airflow velocities and improving usability.

[0058] Furthermore, in one embodiment, the second drive member is electrically connected to the controller, which is configured to control the orifice plate 201 connected to the rotation shaft 203 to rotate to a first position when the inlet air velocity detected by the flow velocity detector is smaller, and to control the orifice plate 201 connected to the rotation shaft 203 to rotate to a second position when the inlet air velocity detected by the flow velocity detector is larger.

[0059] Reference Figure 2 In the first position, along the flow direction of the raw gas, the projection of the through hole 202 on the orifice plate 201 connected to the rotating shaft 203 at least partially overlaps with the projection of the through hole 202 on the adjacent orifice plate 201. At this time, part of the airflow can directly pass through the through hole 202 of each orifice plate 201, and the resistance of the orifice plate 201 to the airflow is small. The first position corresponds to the highest output load condition.

[0060] Reference Figure 1 In the second position, along the flow direction of the raw gas, the projections of the through holes 202 on the orifice plate 201 connected to the rotating shaft 203 are misaligned with the projections of the through holes 202 on the adjacent orifice plates 201. The orifice plate 201 provides greater resistance to the airflow, thus extending the airflow path. The second position corresponds to the lowest output load condition.

[0061] When the flow rate is low, corresponding to low output load conditions, the orifice plate 201 is rotated to the first position, that is, the through holes 202 of adjacent orifice plates 201 at least partially overlap, and part of the airflow can directly pass through the overlapping part and flow directly to the guide vane 301, reducing the resistance of the orifice plate 201 to the airflow. When the flow rate is high, corresponding to high output load conditions, it is rotated to the second position, so that the through holes 202 of adjacent orifice plates 201 are misaligned, increasing the resistance of the orifice plate 201 to the airflow, extending the flow path of the airflow, enhancing the deceleration effect, further optimizing the uniform distribution of flow velocity on the surface of the catalyst bed 4 under different inlet flow rates, and reducing the wear rate.

[0062] Furthermore, in one embodiment, reference is made to... Figure 2 Along the flow direction of the raw gas, a base 204 is provided at one end of the rotating shaft 203 near the downstream orifice plate 201. The base 204 is connected to the downstream orifice plate 201, and the downstream orifice plate 201 is fixedly connected to the inner wall of the tower body 1.

[0063] The rotating shaft 203 is connected to the downstream perforated plate 201 via the base 204. The downstream perforated plate 201 can support the rotating shaft 203, ensuring that the rotatable perforated plate 201 is installed firmly and rotates reliably, thus maintaining the stability of the perforated plate assembly 2 in terms of gradual deceleration and uniform airflow distribution.

[0064] For example, refer to Figure 2 The perforated plate 201 includes a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013. The first sub-plate 2011 and the third sub-plate 2013 are fixedly connected to the inner wall of the tower body 1 by support rods. The outer peripheral wall of the second sub-plate 2012 has a gap with the inner wall of the tower body 1. The center of the second sub-plate 2012 is connected to the rotating shaft 203. The base 204 below the rotating shaft 203 is fixedly connected to the third sub-plate 2013.

[0065] Furthermore, referring to Figures 3 to 5The opening ratio of the first sub-board 2011 is greater than that of the second sub-board 2012, and the opening ratio of the second sub-board 2012 is greater than that of the third sub-board 2013.

[0066] In one embodiment, refer to Figure 1 and Figure 2 The lowermost orifice plate 201, the upper surface of the guide vane 301, and the inner wall of the tower body 1 form an annular buffer cavity 5. The buffer cavity 5 is an empty cavity with no obstructions inside. By forming the buffer cavity 5 between the lowermost orifice plate 201, the guide vane 301, and the inner wall of the tower body 1, the airflow decelerated by the orifice plate assembly 2 can be fully mixed in the buffer cavity 5, eliminating local high-speed zones, further reducing the airflow velocity, reducing the direct impact of the airflow on the guide vane 301, and ensuring a uniform airflow velocity distribution upon reaching the guide assembly 3.

[0067] Furthermore, in one embodiment, reference is made to... Figure 2 Along the flow direction of the raw gas, the height of the buffer chamber 5 is H, which satisfies 50 mm ≤ H ≤ 100 mm. The height of the buffer chamber 5 refers to the fixed distance between the lower surface of the downstream orifice plate 201 and the horizontal plane where the top of the guide vane 301 is located.

[0068] By controlling H within a suitable range, the airflow can be sufficiently decelerated and mixed within the buffer chamber 5, avoiding insufficient airflow mixing due to an excessively small height of the buffer chamber 5, and avoiding wasted space due to an excessively large height of the buffer chamber 5.

[0069] It should be noted that the embodiments of the present invention do not limit the specific structure of the guide vane 301, and any existing structure can be selected as needed. For example, the surface of the guide vane 301 is flat, the whole is in the shape of a long strip, it is made of stainless steel, and the thickness of each guide vane 301 is 2 mm.

[0070] In one embodiment, refer to Figure 7 The flow guiding assembly 3 also includes a mounting frame 303, which is fixed to the inner wall of the tower body 1. One end of each flow guiding blade 301 is hinged to the mounting frame 303 via a rotating shaft. The first driving member drives each flow guiding blade 301 to swing synchronously relative to the mounting frame 303 via a transmission part 302. The transmission part 302 includes a linkage rod, and each flow guiding blade 301 is hinged to the linkage rod. The first driving member is an electric angular stroke actuator or a manual adjusting screw, and its output end is connected to the linkage rod for transmission.

[0071] The mounting frame 303 supports each guide vane 301. One end of each guide vane 301 is hinged to the mounting frame 303 and can swing relative to the mounting frame 303, thereby adjusting the angle between the guide vane 301 and the radial direction of the tower body 1. The first drive unit drives each guide vane 301 to swing synchronously relative to the mounting frame 303 through the transmission unit 302, ensuring that the angle between each guide vane 301 and the radial direction of the tower body 1 is adjusted synchronously, so that the airflow is evenly diffused to the catalyst bed 4, further reducing local wear of the catalyst and improving the reaction efficiency.

[0072] Of course, in other embodiments, the driving method of the guide vanes 301 can also be any other existing structure as needed. For example, one end of each guide vane 301 is hinged to the mounting frame 303 via a rotating shaft, and the transmission part 302 includes a telescopic rod. Each guide vane 301 is also connected to the first driving member via the telescopic rod. The guide vanes 301, the telescopic members, and the first driving members correspond one-to-one, and the telescopic members are controlled to extend and retract by each first driving member, so as to drive the guide vanes 301 to swing relative to the mounting frame 303.

[0073] According to an embodiment of the present invention, another aspect provides a green ammonia synthesis tower, comprising: a tower body 1, a new energy power generation device, and the aforementioned green ammonia synthesis tower gas distributor.

[0074] The top of the tower body 1 is provided with a feed inlet 101 for the raw material gas to enter. Along the flow direction of the raw material gas, the synthesis tower is provided with an orifice plate assembly 2, a flow guiding assembly 3, and a catalyst bed 4 in sequence. The tower body 1 is also provided with a power system, which provides power to the tower body 1 and affects the inlet gas flow rate of the feed inlet 101.

[0075] The catalyst bed 4 is filled below the flow guiding assembly 3, and the distance between its top and the lower edge of the flow guiding blade 301 is 30 mm to 60 mm, preferably 50 mm, to ensure that the airflow after being guided can be evenly diffused to the entire surface of the catalyst bed 4.

[0076] New energy power generation equipment is used to generate electricity. This equipment can be wind power, photovoltaic power, etc. The new energy power generation equipment is electrically connected to the power system to provide power; the inlet gas flow rate is positively correlated with the output load of the new energy power generation equipment.

[0077] Therefore, the green ammonia synthesis system provided by the embodiments of the present invention is powered by the new energy power generation equipment for the power system of the green ammonia synthesis tower. Affected by the output load fluctuation of the new energy power generation equipment, the inlet flow rate of the raw material gas fluctuates accordingly. The flow guiding component 3 in the tower body 1 can adaptively adjust the airflow distribution according to the load change. The feed gas is initially slowed down and uniformly diffused by the orifice plate assembly 2. The feed gas is then guided radially along the tower body 1 by the flow guide assembly 3. With the help of the flow velocity detector and controller, the tilt angle of the flow guide vanes 301 can be automatically adjusted according to the magnitude of the inlet flow velocity, i.e., the output load of the new energy power generation equipment. This enhances the radial diffusion capacity of the flow guide vanes 301 when the inlet flow velocity is low, i.e., under low output load conditions. When the inlet flow velocity is high, i.e., under high output load conditions, the flow guide vanes 301 increase the resistance of the feed gas to the flow guide vanes 301 and guide the airflow to diffuse rapidly. This reduces the force of the airflow impacting the catalyst bed 4, effectively controls the force of the feed gas impacting the catalyst bed 4, significantly reduces the risk of catalyst particle breakage and pulverization caused by violent collisions, alleviates the problem of bed pore blockage, thereby reducing maintenance costs and catalyst consumption, and significantly improving the production efficiency of green ammonia synthesis.

[0078] The following detailed description of the green ammonia synthesis system of the present invention, in conjunction with specific embodiments, is intended to limit the scope of protection claimed by the present invention.

[0079] In the following examples and comparative examples, the same new energy power generation equipment was used, specifically wind power equipment. The inner diameter of tower 1 was 800 mm, and its internal height was 6000 mm. The catalyst bed 4 was located at the bottom of tower 1, with a height of 4000 mm, and was filled with an iron-based catalyst (Fe3O4-Al2O3-K2O) at a loading of 2.5 m³. The operating pressure was 7.5 MPa, the inlet temperature of feed inlet 101 was 380°C, the inlet hydrogen-nitrogen molar ratio was 3:1, and the space velocity was 8000 h⁻¹. -1 .

[0080] Example 1: The output load of the new energy power generation equipment is 100%.

[0081] The green ammonia synthesis tower includes: a tower body 1, an orifice plate assembly 2, a buffer chamber 5, a flow guiding assembly 3, a catalyst bed 4, a flow rate detector, and a controller. The orifice plate assembly 2 has three orifice plates 201 spaced apart along the flow direction of the feed gas, including a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013. The opening ratio of the first sub-plate 2011 is 35%, the second sub-plate 2012 is 25%, and the third sub-plate 2013 is 15%. Each sub-plate has a thickness of 3 mm. The through-holes 202 are equilateral triangular.

[0082] The guide vanes 301 are 2 mm thick and there are 12 of them. The controller controls the radial angle θ between the guide vanes 301 and the tower body 1 to be 30°. The height H of the buffer cavity 5 is 80 mm.

[0083] The feed gas inlet 101 has an inlet gas velocity of 18.5 m / s and an inlet gas flow rate of 5500 Nm³. 3 / h.

[0084] After passing through three sub-plates, the flow velocity of the feed gas gradually decreases from 18.5 m / s, dropping to 6.2 m / s below the third sub-plate 2013. Upon entering the buffer chamber 5, the velocity further decreases to 4.5 m / s. Guided by the guide vanes 301, the average velocity reaching the surface of the catalyst bed 4 is 2.8 m / s, with a maximum local velocity of 3.6 m / s. The uniformity of the velocity distribution on the surface of the catalyst bed 4 (the ratio of the standard deviation of the velocity to the average velocity) is 0.21. The maximum impact force on the surface of the catalyst bed 4 is 18.5 Pa. The annual catalyst wear rate is approximately 1.3%, and the annual increase in bed pressure differential is approximately 2.8%.

[0085] Example 2: The output load of the new energy power generation equipment is 40%.

[0086] The green ammonia synthesis tower includes: a tower body 1, an orifice plate assembly 2, a buffer chamber 5, a flow guiding assembly 3, a catalyst bed 4, a flow rate detector, and a controller. The orifice plate assembly 2 has three orifice plates 201 spaced apart along the flow direction of the feed gas, including a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013. The opening ratio of the first sub-plate 2011 is 35%, the second sub-plate 2012 is 25%, and the third sub-plate 2013 is 15%. Each sub-plate has a thickness of 3 mm. The through-holes 202 are equilateral triangular.

[0087] The guide vanes 301 are 2 mm thick and there are 12 of them. The controller controls the radial angle θ between the guide vanes 301 and the tower body 1 to be 45°.

[0088] The height H of the buffer chamber 5 is 80 mm. The inlet gas velocity at the feed inlet 101 is 7.4 m / s, and the feed gas flow rate is 2200 Nm³. 3 / h.

[0089] After passing through three sub-plates, the feed gas velocity gradually decreases from 7.4 m / s, with an average velocity of 1.9 m / s before reaching the guide vane 301. Guided by the guide vane 301, the gas flow increases radially at a diffusion angle of approximately 70°, reaching an average velocity of 1.2 m / s on the surface of catalyst bed 4, with a maximum local velocity of 1.5 m / s. The velocity distribution uniformity index on the surface of catalyst bed 4 is 0.18. The maximum impact force on the surface of catalyst bed 4 is 7.2 Pa. The annual catalyst wear rate is approximately 0.9%, and the annual pressure difference growth rate of the bed is approximately 1.9%.

[0090] Example 3: The output load of the new energy power generation equipment is 110%.

[0091] The green ammonia synthesis tower includes: a tower body 1, an orifice plate assembly 2, a buffer chamber 5, a flow guiding assembly 3, a catalyst bed 4, a flow rate detector, and a controller. The orifice plate assembly 2 has three orifice plates 201 spaced apart along the flow direction of the feed gas, including a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013. The opening ratio of the first sub-plate 2011 is 35%, the second sub-plate 2012 is 25%, and the third sub-plate 2013 is 15%. Each sub-plate has a thickness of 3 mm. The through-holes 202 are equilateral triangular.

[0092] The guide vanes 301 are 2 mm thick and there are 12 of them. The controller controls the radial angle θ between the guide vanes 301 and the tower body 1 to be 15°.

[0093] The height H of the buffer chamber 5 is 80 mm. The inlet gas velocity at the feed inlet 101 is 20.4 m / s, and the feed gas flow rate is 6050 Nm³. 3 / h.

[0094] After passing through three sub-plates, the feed gas velocity gradually decreases from 20.4 m / s, with an average velocity of 6.8 m / s before reaching the guide vane 301. Guided by the guide vane 301, the gas flow increases radially at a diffusion angle of approximately 40°, reaching an average velocity of 3.5 m / s on the surface of catalyst bed 4, with a maximum local velocity of 4.2 m / s. The velocity distribution uniformity index on the surface of catalyst bed 4 is 0.23. The maximum impact force on the surface of catalyst bed 4 is 22.4 Pa. The annual catalyst wear rate is approximately 1.6%, and the annual increase in bed pressure differential is approximately 3.2%.

[0095] Example 4: The difference between this embodiment and Embodiment 3 is that the controller controls the radial angle between the guide vane 301 and the tower body 1 to be 30°, resulting in an average flow velocity of 3.2 m / s and a maximum local flow velocity of 5.1 m / s reaching the surface of the catalyst bed 4. The uniformity index of the flow velocity distribution on the surface of the catalyst bed 4 is 0.26. The maximum impact force on the surface of the catalyst bed 4 is 24 Pa. The annual catalyst wear rate is approximately 2.1%, and the annual growth rate of the bed pressure difference is approximately 4%.

[0096] Comparative Example 1: The output load of the new energy power generation equipment is 100%.

[0097] The green ammonia synthesis tower includes: a tower body 1, within which a perforated plate assembly 2 and a catalyst bed 4 are installed. The perforated plate assembly 2 uses a single-layer grid with an opening ratio of 30%. All layers are 3 mm thick. The through holes 202 are equilateral triangular.

[0098] The feed gas inlet 101 has an inlet gas velocity of 18.5 m / s and an inlet gas flow rate of 5500 Nm³. 3 / h.

[0099] After passing through a single-layer grid, the feed gas velocity decreases from 18.5 m / s to 12.8 m / s, reaching an average velocity of 6.8 m / s at the surface of catalyst bed 4, with a maximum local velocity of 10.5 m / s. The velocity distribution uniformity index on the surface of catalyst bed 4 is 0.58. The maximum impact force on the surface of catalyst bed 4 is 65 Pa. The annual catalyst attenuation rate is approximately 8.2%, and the annual increase in bed pressure differential is approximately 15.6%.

[0100] Comparative Example 2: The output load of the new energy power generation equipment is 100%.

[0101] The green ammonia synthesis tower includes: a tower body 1, within which are sequentially arranged an orifice plate assembly 2, a buffer chamber 5, a flow guiding assembly 3, and a catalyst bed 4. The orifice plate assembly 2 consists of a single-layer grid with an opening ratio of 30%. All layers are 3 mm thick. The through holes 202 are equilateral triangular.

[0102] The guide vanes 301 are 2 mm thick and there are 12 of them. The controller controls the radial angle θ between the guide vanes 301 and the tower body 1 to be 30°. The height H of the buffer cavity 5 is 30 mm.

[0103] The feed gas inlet 101 has an inlet gas velocity of 18.5 m / s and an inlet gas flow rate of 5500 Nm3 / h.

[0104] After passing through a single-layer grid, the feed gas velocity decreases from 18.5 m / s to 12.8 m / s. Guided by the guide vanes 301, the average velocity reaching the surface of catalyst bed 4 is 4.5 m / s, with a maximum local velocity of 7.2 m / s. The velocity distribution uniformity index on the surface of catalyst bed 4 is 0.42. The maximum impact force on the surface of catalyst bed 4 is 38 Pa. The annual catalyst wear rate is approximately 5.5%, and the annual increase in bed pressure differential is approximately 9.8%.

[0105] Comparative Example 3: The output load of the new energy power generation equipment is 100%.

[0106] The green ammonia synthesis tower includes: a tower body 1, within which a perforated plate assembly 2, a buffer chamber 5, and a catalyst bed 4 are sequentially arranged. The perforated plate assembly 2 has three perforated plates 201 spaced apart along the flow direction of the feed gas, including a first sub-plate 2011, a second sub-plate 2012, and a third sub-plate 2013. The perforation ratios of the first sub-plate 2011 are 35%, 25%, and 15%, respectively. Each sub-plate has a thickness of 3 mm. The through-holes 202 are equilateral triangular. The height H of the buffer chamber 5 is 80 mm.

[0107] The feed gas inlet 101 has an inlet gas velocity of 18.5 m / s and an inlet gas flow rate of 5500 Nm3 / h.

[0108] After passing through three sub-plates and buffer chamber 5, the average velocity of the feed gas reaching the surface of catalyst bed 4 is 3.9 m / s, with a maximum local velocity of 5.8 m / s. The velocity distribution uniformity index on the surface of catalyst bed 4 is 0.39. The maximum impact force on the surface of catalyst bed 4 is 29 Pa. The annual catalyst wear rate is approximately 3.2%, and the annual increase rate of bed pressure difference is approximately 5.6%.

[0109] The airflow direction is mainly vertically downward, with insufficient radial diffusion, resulting in a higher flow velocity in the central region (5.8 m / s) and a lower flow velocity in the edge region (2.2 m / s) of catalyst bed 4.

[0110] The parameters and performance indicators of the above embodiments and comparative examples are summarized in Table 1.

[0111] Table 1: Parameters and Performance Indicators

[0112] As shown in Table 1, under 100% output load conditions, Example 1 reduced the annual catalyst wear rate from 8.2% in the traditional single-layer grid (Comparative Example 1) to 1.3%, a reduction of 84%. The annual growth rate of bed pressure difference decreased from 15.6% to 2.8%, a reduction of 82%, and the operating cycle was extended by more than 1.5 times. The maximum local flow velocity on the surface of catalyst bed 4 decreased from 10.5 m / s to 3.6 m / s, a reduction of 66%. The flow velocity uniformity index improved from 0.58 to 0.21, an improvement of 64%.

[0113] For Examples 2 and 3, under low-load conditions of 40% output load and high-load conditions of 110% output load, by adjusting the angle θ (45° and 15°), the annual wear rate was controlled at 0.9% and 1.6% respectively, which were significantly better than Comparative Examples 1, 2 and 3.

[0114] The flow rate uniformity index of Examples 1, 2, 3, and 4 is all below 0.23, while that of Comparative Example 1 is 0.58, Comparative Example 2 is 0.42, and Comparative Example 3 is 0.39. Therefore, the combined design of the orifice plate assembly 2, buffer chamber 5, and flow guiding assembly 3 of the present invention achieves step-by-step deceleration, uniform distribution, and controllable direction of airflow, effectively solving the technical problems of severe catalyst wear, rapid rise in bed pressure difference, and short operating cycle in traditional synthesis towers.

[0115] In Examples 1 and 2, it can be seen that when the output load is low, the wear can be further reduced by increasing the included angle θ.

[0116] In Examples 3 and 4, it can be seen that when the output load is high, wear can be effectively controlled by reducing the included angle θ.

[0117] Based on 8,000 hours of operation per year, the embodiments of the present invention can extend the time for the differential pressure of catalyst bed 4 to reach the alarm threshold from less than 6 months in the traditional structure (Comparative Example 1) to more than 15 months. A single thousand-ton skid-mounted green ammonia synthesis tower can save about RMB 120,000 per year in costs for shutdown cleaning and catalyst replenishment due to excessive differential pressure, while reducing production losses by about RMB 300,000, which has significant economic benefits and industrial application value.

[0118] It should be noted that in the testing process of the above embodiments and comparative examples, three-dimensional numerical simulation verification was performed using computational fluid dynamics software. The feed gas was considered an ideal gas, the standard k-ε model was used as the turbulence model, the inlet boundary was set as a velocity inlet (calculated based on the load), the outlet boundary was set as a pressure outlet, no-slip boundary conditions were used on the walls, and a hexahedral core mesh was used. The mesh size was determined to be 3.8 million after independence verification. Based on the steady-state solution, the convergence criterion was that the residual decreased to 10. -6 the following.

[0119] Although embodiments of the invention have been described in conjunction with the accompanying drawings, those skilled in the art can make various modifications and variations without departing from the spirit and scope of the invention, and such modifications and variations all fall within the scope defined by the appended claims.

Claims

1. A gas distributor for a green ammonia synthesis tower, characterized in that, The gas distributor of the green ammonia synthesis tower is suitable for being installed inside the green ammonia synthesis tower along the flow direction of the raw material gas. The gas distributor of the green ammonia synthesis tower includes an orifice plate assembly (2) and a flow guiding assembly (3) in sequence. The orifice plate assembly (2) is provided with a plurality of orifice plates (201) spaced apart along the flow direction of the raw gas, and each orifice plate (201) is provided with a plurality of through holes (202). The orifice plate assembly (2) is used to reduce the flow rate of the raw gas. The flow guiding component (3) includes multiple flow guiding blades (301), which are distributed circumferentially along the tower body (1) of the green ammonia synthesis tower to guide the raw material gas to diffuse radially along the tower body (1) and flow to the catalyst bed (4) inside the green ammonia synthesis tower. One end of each flow guiding blade (301) is connected to the first driving member through the transmission part (302), and each flow guiding blade (301) is inclined toward the catalyst bed (4). The gas distributor of the green ammonia synthesis tower also includes a flow rate detector and a controller. The flow rate detector is adapted to be installed at the feed inlet (101) of the green ammonia synthesis tower to detect the inlet flow rate of the raw material gas. The controller is electrically connected to the first drive unit and the flow rate detector respectively. The controller is configured to control the first drive unit to drive the transmission unit (302) based on the magnitude of the inlet flow rate to adjust the included angle between the guide vane (301) and the radial direction of the tower body (1).

2. The gas distributor for the green ammonia synthesis tower according to claim 1, characterized in that, The controller is configured to control the angle between the guide vane (301) and the radial direction of the tower body (1) to be negatively correlated with the inlet air velocity.

3. The gas distributor for the green ammonia synthesis tower according to claim 1, characterized in that, Along the flow direction of the raw gas, the opening ratio on the orifice plate (201) gradually decreases, and the orifice plate assembly (2) is used to gradually reduce the flow rate of the raw gas.

4. The gas distributor for the green ammonia synthesis tower according to claim 3, characterized in that, The orifice plate assembly (2) includes a first sub-plate (2011), a second sub-plate (2012), and a third sub-plate (2013) in sequence along the flow direction of the raw gas. The orifice ratio of the first sub-plate (2011) is Φ1, the orifice ratio of the second sub-plate (2012) is Φ2, and the orifice ratio of the third sub-plate (2013) is Φ3, satisfying 30%≤Φ1≤40%, 20%≤Φ2≤30%, and 10%≤Φ3≤20%.

5. The gas distributor for the green ammonia synthesis tower according to claim 3, characterized in that, The orifice plate assembly (2) includes at least three orifice plates (201), and the opening size of the through holes (202) on each orifice plate (201) is the same. Along the flow direction of the raw gas, at least one orifice plate (201) in the middle is connected to a rotating shaft (203). The rotating shaft (203) is connected to a second driving member, which is used to drive the rotating shaft (203) to drive the corresponding orifice plate (201) to rotate.

6. The gas distributor for the green ammonia synthesis tower according to claim 5, characterized in that, The second drive unit is electrically connected to the controller, which is configured to control the orifice plate (201) connected to the rotating shaft (203) to rotate to a first position when the inlet air velocity detected by the flow velocity detector is smaller, and to control the orifice plate (201) connected to the rotating shaft (203) to rotate to a second position when the inlet air velocity detected by the flow velocity detector is larger. At the first position, along the flow direction of the raw gas, the projection of the through hole (202) on the orifice plate (201) connected to the rotating shaft (203) at least partially coincides with the projection of the through hole (202) on the adjacent orifice plate (201); In the second position, along the flow direction of the raw gas, the projection of the through hole (202) on the orifice plate (201) connected to the rotating shaft (203) is misaligned with the projection of the through hole (202) on the adjacent orifice plate (201).

7. The gas distributor for the green ammonia synthesis tower according to claim 5, characterized in that, Along the flow direction of the raw gas, the rotating shaft (203) is provided with a base (204) at one end near the downstream orifice plate (201). The base (204) is connected to the downstream orifice plate (201), and the downstream orifice plate (201) is fixedly connected to the inner wall of the tower body (1).

8. The gas distributor for the green ammonia synthesis tower according to any one of claims 1 to 7, characterized in that, The orifice plate (201) located at the lowest end forms a buffer cavity (5) with the guide vane (301) and the inner wall of the tower body (1).

9. The gas distributor for the green ammonia synthesis tower according to claim 8, characterized in that, Along the flow direction of the raw gas, the height of the buffer chamber (5) is H, which satisfies 50 mm ≤ H ≤ 100 mm.

10. A green ammonia synthesis tower, characterized in that, include: The tower body (1) is equipped with a feed inlet (101) for the raw material gas to enter and a power system; A new energy power generation device is used to generate electrical energy. The new energy power generation device is electrically connected to the power system to provide power to the power system. The inlet flow rate of the raw material gas is positively correlated with the output load of the new energy power generation device. The gas distributor of the green ammonia synthesis tower according to any one of claims 1 to 9 is provided in the tower body (1) along the flow direction of the raw material gas, and the tower body (1) is also provided with a catalyst bed (4) located downstream of the flow guiding component (3).

Images