Coke oven gas to lng cogeneration synthetic ammonia device and control method

Abstract

This invention discloses a coke oven gas-to-LNG and co-production ammonia synthesis device and control method, relating to the field of coke oven gas treatment technology. The proposed solution includes a methanation reactor containing a catalyst bed. Above the catalyst bed is an inert alumina sphere layer, and above the inert alumina sphere layer is an active distribution control component. The active distribution control component includes a vertically positioned adjusting shaft, a motor driving the adjusting shaft, multiple circumferentially distributed guide vanes driven by the adjusting shaft through a first transmission mechanism, and a conical mesh bag driven by the adjusting shaft through a second transmission mechanism and partially housed within the inert alumina sphere layer. Through the synergistic cooperation of the active distribution control component and the inert alumina sphere layer, the graded and uniform distribution of the feed gas and the dynamic control of the exothermic zone are achieved, effectively solving the problem of local overheating caused by trace amounts of carbon dioxide in existing technologies and ensuring the stable operation of the catalyst.

Description

Technical Field

[0001] This invention relates to the field of coke oven gas treatment technology, and in particular to a coke oven gas-to-LNG and co-production ammonia production unit and control method. Background Technology

[0002] Coke oven gas to LNG co-production ammonia technology is an important direction for the resource utilization of coke oven gas. One of its core steps is to remove residual carbon monoxide and carbon dioxide from coke oven gas through methanation reaction, so as to avoid poisoning of the subsequent ammonia synthesis catalyst and improve the methane purity of LNG products. Currently, most mainstream methanation reactions adopt vertical fixed-bed reactors, which realize the reaction through nickel-based catalysts filled inside.

[0003] However, existing technologies have the following shortcomings in practical applications: Firstly, trace amounts of carbon dioxide remain in the decarbonized coke oven gas. This carbon dioxide reacts rapidly on the catalyst in the reactor inlet area, releasing a large amount of heat in a short time. If the heat cannot be dissipated in time, it can easily cause the local temperature to exceed the catalyst's tolerance limit, leading to catalyst sintering and deactivation. Secondly, the existing reactors mostly have a fixed airflow distribution structure, which cannot dynamically adjust the airflow direction according to the fluctuation of carbon dioxide concentration in the raw gas and the change of flow load, so as to guide the heat release area to the side wall area with better heat dissipation conditions, thus leading to local overheating. Summary of the Invention

[0004] In view of this, the purpose of the present invention is to solve the above-mentioned problems.

[0005] To achieve the above technical objectives, the present invention provides a coke oven gas to LNG co-production ammonia synthesis unit, including a methanation reaction tank, wherein a catalyst bed is provided in the reaction tank, an inert alumina ball layer is provided above the catalyst bed, and an active distribution control component is provided above the inert alumina ball layer. The active distribution control component includes a vertically arranged adjustment shaft, a motor that drives the adjustment shaft to rotate, a plurality of guide vanes that are driven by the adjustment shaft through a first transmission mechanism and distributed circumferentially, and a conical mesh bag that is driven by the adjustment shaft through a second transmission mechanism and partially housed within the inert alumina spherical layer. When the motor drives the adjusting shaft to rotate, it simultaneously changes the deflection angle of the guide vanes and the vertical height of the conical net.

[0006] Preferably, the first transmission mechanism includes an adjusting bevel gear disk coaxially sleeved on the adjusting shaft and driven bevel teeth disposed at the shaft ends of each guide vane, wherein the adjusting bevel gear disk meshes with each driven bevel tooth; a keyway and a key are provided between the adjusting shaft and the adjusting bevel gear disk to realize circumferential transmission and axial relative sliding.

[0007] Preferably, the second transmission mechanism includes a spiral groove formed at the bottom of the adjusting shaft, a connecting seat sleeved at the bottom of the adjusting shaft, and a conical mesh fixed below the connecting seat; Furthermore, the inner hole of the connecting seat is provided with a protrusion that mates with the spiral groove; the connecting seat is connected to the fixed component through a guide mechanism, which restricts its movement to only the vertical direction.

[0008] Preferably, the guiding mechanism includes at least two guide rods fixed to the bottom of the fixed cylinder, and the connecting seat has guide holes that cooperate with the guide rods.

[0009] Preferably, a spring is sleeved on the adjusting shaft, the spring being used to provide a downward elastic force to the adjusting bevel gear disk; the active distribution control assembly also includes a mechanical limiting mechanism for limiting the maximum rotation angle of the guide vanes.

[0010] Preferably, an annular distributor is installed between the top air inlet of the reaction vessel and the active distribution control component. The annular distributor includes a fixed disk, a gas distribution disk, and a sealing disk arranged coaxially, which together form a gas equalization space. The gas distribution disk has evenly distributed gas distribution grooves on its outer periphery.

[0011] A method for controlling the co-production of ammonia from coke oven gas to LNG, based on the above, includes: S1, The carbon dioxide concentration and volumetric flow rate of the raw gas entering the reaction tank are collected in real time and labeled as C and Q, respectively; S2, compare C and Q with the raw gas carbon dioxide concentration threshold and the raw gas flow rate threshold, respectively. The raw gas carbon dioxide concentration threshold and the raw gas flow rate threshold are labeled as follows: and ; S3, if and Then, control the motor to drive the adjustment shaft to rotate, so that the guide vanes are reset to the initial angle and the conical net is lowered; like or Then, control the motor to drive the adjustment shaft to rotate, so that the guide vanes deflect to the guide angle and the conical net bag rises.

[0012] Preferably, in step S3, the step of controlling the motor to drive the adjustment shaft to rotate includes: when it is determined that the guide vane needs to be reset, controlling the motor to reverse; when it is determined that the guide vane needs to be deflected to the guide angle, controlling the motor to rotate forward.

[0013] Preferably, in step S3, before controlling the motor to move, the current position signal of the motor or adjusting shaft is obtained; if the current position already corresponds to the target state, the current state is maintained.

[0014] Preferably, the initial angle of the guide vanes is configured to allow the airflow to flow uniformly downwards across the cross-section of the reaction vessel, and the guide angle is configured to allow the airflow to diffuse toward the sidewall of the reaction vessel.

[0015] As can be seen from the above technical solutions, this application has the following beneficial effects: 1. By coordinating the active distribution control components with the inert alumina spheres, the graded and uniform distribution of the feed gas and the dynamic control of the exothermic zone are achieved, effectively solving the problem of local overheating caused by trace amounts of carbon dioxide in the existing technology and ensuring the stable operation of the catalyst. 2. In the active distribution control component, the adjusting shaft drives the guide vane angle adjustment through bevel gear transmission, while simultaneously driving the conical net bag to rise and fall through the screw transmission, thereby achieving synchronous control of airflow guidance and spherical layer distribution and improving the adaptability to working conditions; 3. The design of the spring and the adjusting bevel gear disc can compensate for the travel difference between the adjustment of the guide vane and the movement of the connecting seat by the axial sliding of the bevel gear disc when the guide vane reaches the limit angle, thus avoiding component jamming or damage and improving the stability and reliability of the device operation. Attached Figure Description

[0016] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0017] Figure 1 A schematic diagram of the overall structure of a coke oven gas to LNG co-production ammonia synthesis unit provided by the present invention; Figure 2 This is a cross-sectional structural schematic diagram of a coke oven gas to LNG co-production ammonia synthesis unit provided by the present invention; Figure 3 This is a cross-sectional structural schematic diagram of a coke oven gas to LNG co-production ammonia synthesis unit provided by the present invention; Figure 4 This is a cross-sectional view of the annular distributor of a coke oven gas to LNG co-production ammonia synthesis unit provided by the present invention; Figure 5 This invention provides a schematic diagram of the overall structure of an active distributed control component for a coke oven gas to LNG co-production ammonia synthesis unit. Figure 6 This is a partial structural diagram of the active distributed control component of a coke oven gas to LNG co-production ammonia synthesis unit provided by the present invention; Figure 7This invention provides a schematic diagram of the guide vane angle adjustment state structure of a coke oven gas to LNG co-production ammonia synthesis unit.

[0018] In the diagram: 10. Reactor; 11. Catalyst bed; 20. Inert alumina spherical layer; 30. Annular distributor; 31. Fixed plate; 32. Gas distribution plate; 321. Flow divider; 322. Gas distribution slot; 33. Sealing plate; 40. Active distribution control component; 41. Fixed cylinder; 411. Guide rod; 412. Limit block; 42. Guide vane; 421. Driven bevel gear; 422. Limiting plate; 43. Adjusting shaft; 44. Adjusting bevel gear disc; 45. Connecting seat; 46. Conical net bag; 461. Connecting frame; 47. Spring; 50. Electric motor. Detailed Implementation

[0019] The following description is exemplary in nature and is not intended to limit the scope, application, or use of this disclosure. It should be understood that in all these figures, the same or similar reference numerals indicate the same or similar parts and features. The figures are merely schematic representations of the concept and principles of embodiments of this disclosure and do not necessarily show the specific dimensions and scale of the various embodiments of this disclosure. Certain details or structures of embodiments of this disclosure may be exaggerated in particular portions of certain figures.

[0020] Example 1, see Figures 1-7 As shown, a coke oven gas to LNG co-production ammonia production unit includes a raw gas pretreatment unit, a purification and component modulation unit, an LNG preparation unit, and an ammonia preparation unit. Each unit is connected by pipelines and valve groups to form a closed-loop collaborative production chain. Specifically, the purification and component modulation unit includes a reaction tank 10, which is used to deeply remove residual carbon monoxide (CO) and carbon dioxide (CO2) from the coke oven gas obtained from the feed gas pretreatment unit and convert it into methane, providing high-quality feedstock for the LNG preparation unit and the synthetic ammonia preparation unit.

[0021] More specifically, the reaction vessel 10 is a vertical pressure vessel, including an upper head, a middle tank, and a lower head. A catalyst bed 11 is fixed inside the middle tank. The catalyst bed 11 is filled with a nickel-based methanation catalyst to realize the methanation reaction of carbon monoxide (CO), carbon dioxide (CO2), and hydrogen (H2). For example, coke oven gas enters the reaction vessel 10 after pretreatment and decarbonization. After the methanation reaction is completed through the catalyst bed 11, the gas is discharged. The discharged gas enters the LNG preparation unit and is cryogenically separated to obtain LNG products. The tail gas containing H2 and N2 produced by the LNG preparation unit enters the ammonia synthesis preparation unit and is synthesized into liquid ammonia products through component proportioning, compression, and high temperature and high pressure synthesis.

[0022] For further details, please refer to [link / reference]. Figure 2 and Figure 3 As shown, the upper end cap of the reaction vessel 10 is fixed with an air inlet and an air outlet, respectively, for air intake and exhaust. An annular distributor 30 is installed between the upper end cap and the middle tank of the reaction vessel 10 to achieve preliminary uniform distribution of the raw material gas. The annular distributor 30 includes a fixed plate 31, a gas distribution plate 32, and a sealing plate 33, which are coaxially assembled to form a closed gas equalization space. The fixed plate 31 is an annular plate structure and is fixed to the top end face of the middle tank of the reaction vessel 10 by bolts. The gas distribution plate 32 is located in the middle of the fixed plate 31. Multiple flow dividers 321 are uniformly welded and fixed on the upper surface of the gas distribution plate 32. The flow dividers 321 are radially distributed. The top of the flow dividers 321 abuts against the lower surface of the fixed plate 31, which not only achieves relative support between the gas distribution plate 32 and the fixed plate 31, but also allows the raw material gas entering from the middle of the fixed plate 31 to be dispersed into the gas equalization space formed by the fixed plate 31, the gas distribution plate 32 and the sealing plate 33 through the radial flow dividers 321. The sealing plate 33 is an annular plate structure, which is fixed to the bottom of the fixed plate 31 and the gas distribution plate 32 by bolts to achieve bottom sealing of the gas equalization space. Multiple gas distribution grooves 322 are evenly distributed on the outer circumference of the gas distribution plate 32. The gas distribution grooves 322 are evenly distributed along the circumference of the gas distribution plate 32. The gas in the gas equalization space can be evenly discharged into the middle tank of the reaction tank 10 through the gas distribution grooves 322.

[0023] Furthermore, it also includes an active distribution control component 40, which includes a fixed cylinder 41, guide vanes 42, an adjusting shaft 43, an adjusting bevel gear disc 44, a connecting seat 45, a conical net 46, and a spring 47. The fixed cylinder 41 is a hollow cylindrical structure and is fixed to the bottom center of the air distribution disc 32 by bolts. The guide vanes 42 are evenly distributed along the outer circumference of the fixed cylinder 41. One end of the guide vanes 42 is rotatably connected to the side wall of the fixed cylinder 41 through a rotating shaft, and the end of the rotating shaft is coaxially fixed with a driven bevel gear 421. The regulating shaft 43 has a stepped shaft structure, with its top penetrating the middle of the gas distribution plate 32 and achieving a rotating seal connection with the gas distribution plate 32 through a rotating seal. The top of the regulating shaft 43 extends to the outside of the upper end cap of the reaction vessel 10 and is fixedly connected to the output end of the motor 50 through a coupling. The motor 50 is fixed to the top of the reaction vessel 10 by a bracket and is used to provide regulating power to the active distribution control component 40.

[0024] Specifically, the adjusting bevel gear disk 44 is sleeved on the outer surface of the adjusting shaft 43. A keyway is provided on the corresponding section of the adjusting shaft 43. The inner hole of the adjusting bevel gear disk 44 is provided with a key that matches the keyway, so as to realize the transmission connection between the adjusting bevel gear disk 44 and the adjusting shaft 43. The adjusting shaft 43 can drive the adjusting bevel gear disk 44 to rotate synchronously, while allowing the adjusting bevel gear disk 44 to slide along the axial direction of the adjusting shaft 43. The outer peripheral bevel teeth of the adjusting bevel gear disk 44 mesh with the driven bevel teeth 421 of each guide vane 42. The motor 50 drives the adjusting bevel gear disk 44 to rotate through the adjusting shaft 43, and the adjusting bevel gear disk 44 can drive the guide vane 42 to adjust the angle through the driven bevel teeth 421.

[0025] It is worth mentioning that the width of the guide vane 42 gradually narrows from the radial direction of the fixed cylinder 41, ensuring that after the guide vane 42 is adjusted, it can guide the airflow to diffuse towards the inner wall of the reaction tank 10.

[0026] For further details, please refer to [link / reference]. Figure 6 As shown, the bottom of the adjusting shaft 43 is provided with a spiral groove, and the bottom of the adjusting shaft 43 is fitted with a connecting seat 45; the bottom of the fixed cylinder 41 is fixed with a guide rod 411, at least two guide rods 411 are provided, and they are evenly distributed along the circumference of the fixed cylinder 41. The connecting seat 45 is provided with a guide hole at the position corresponding to the guide rod 411, and the guide rod 411 passes through the guide hole to realize the sliding connection between the connecting seat 45 and the fixed cylinder 41, thereby limiting the connecting seat 45 to move only in the axial direction; the inner hole of the connecting seat 45 is fixed with a protrusion, which is embedded in the spiral groove of the adjusting shaft 43. The outer periphery of the connecting seat 45 is connected to a conical net bag 46 through a connecting frame 461. When the adjusting shaft 43 drives the guide vane 42 to adjust the angle, the conical net bag 46 can be driven to rise and fall through the connecting seat 45.

[0027] An inert alumina sphere layer 20 is arranged below the active distribution control component 40 to buffer the initiation rate of the methanation reaction and disperse the exothermic region. The inert alumina sphere layer 20 is located above the catalyst bed 11 and is composed of several inert alumina spheres. Inert alumina spheres refer to alumina particles with stable chemical properties that do not participate in the methanation reaction. They have the characteristics of high temperature resistance, tolerance to methanation reaction conditions of 400-650℃, moderate specific surface area, and high mechanical strength. Some of the inert alumina spheres are arranged inside the conical mesh bag 46. It is worth mentioning that the vertical cross-section of the conical net bag 46 is conical (with a large diameter at the top and a small diameter at the bottom), and its top is welded and fixed to the lower surface of the connecting seat 45 through the connecting frame 461; the inert alumina ball layer 20 is laid on the top of the catalyst bed 11, some of which are arranged inside the conical net bag 46, and the remaining inert alumina balls are distributed around the outside of the conical net bag 46.

[0028] For example, the decarbonized raw material gas enters through the raw material gas inlet of the upper head of the reaction tank 10, and the pressure of the raw material gas is evenly distributed into the intermediate tank by the annular distributor 30. When the carbon dioxide (CO2) content in the raw gas is ≤ the preset carbon dioxide threshold, the preset carbon dioxide threshold is determined by those skilled in the art according to actual needs, and is not specifically limited here, the guide vane 42 is adjusted to the initial angle, the initial angle is determined by those skilled in the art according to actual needs, and is not specifically limited here. The rule for setting the initial angle is to allow the guide vane 42 to guide the airflow to flow uniformly downwards across the entire cross section of the reaction tank 10, prioritizing reaction efficiency. When the carbon dioxide (CO2) content in the raw material gas increases, or when the carbon dioxide (CO2) content in the raw material gas exceeds the preset carbon dioxide threshold, or when the raw material gas flow rate increases, the guide vane 42 is adjusted to a preset angle. The preset angle is determined by those skilled in the art based on actual needs and is not specifically limited here. The rule for setting the preset angle is to guide the airflow towards the inner wall of the reaction tank 10 to diffuse, and to guide the heat release area to the side wall area with better heat dissipation conditions. The side wall of the conventional reaction tank 10 is equipped with a cooling jacket, so the heat dissipation conditions are better. While the guide vane 42 is adjusted to the preset angle, the adjusting shaft 43 drives the connecting seat 45, so that the connecting seat 45 drives the conical net bag 46 to rise synchronously through the connecting frame 461; the inert alumina balls inside the conical net bag 46 rise with the net bag, and the inert alumina balls outside the conical net bag 46 lose their support and gather towards the middle of the conical net bag 46, that is, the middle of the reaction tank 10, forming a hill-like distribution of "high in the middle and low around the edges". This ensures that the airflow near the side wall can quickly contact the catalyst bed 11 for reaction, and also enhances the heat absorption buffer of the middle area through the inert alumina balls gathered in the middle, avoiding overheating in the middle. When the carbon dioxide (CO2) content in the feed gas returns to normal or the feed gas flow rate decreases, the guide vane 42 returns to its initial angle. At the same time, the conical net 46 descends and pushes the inert alumina balls gathered in the middle to the outside, so that the inert alumina ball layer 20 returns to a flat distribution state, ensuring that the airflow contacts the catalyst bed 11 evenly.

[0029] Furthermore, to compensate for the travel difference between the angle adjustment of the guide vane 42 and the axial movement of the connecting seat 45, a spring 47 is sleeved on the outer surface of the adjusting shaft 43. The spring 47 is located above the adjusting bevel gear disk 44. The top end of the spring 47 abuts against the stepped platform of the adjusting shaft 43, and the bottom end abuts against the upper surface of the adjusting bevel gear disk 44, providing a downward elastic force to the adjusting bevel gear disk 44 to ensure stable meshing between the adjusting bevel gear disk 44 and the driven bevel gear 421. A limit block 412 is fixed on the side wall of the fixed cylinder 41, and a limit piece 422 is fixed on the side of the guide vane 42 near the fixed cylinder 41 to limit movement. Block 412 cooperates with limiting piece 422 to limit the flow guide vane 42 in two rotational directions. That is, when the flow guide vane 42 rotates to the point where the limiting block 412 and the limiting piece 422 abut, the flow guide vane 42 reaches its limit rotation angle. At this time, the adjusting shaft 43 continues to rotate. The axial thrust generated at the meshing point of the driven bevel tooth 421 and the adjusting bevel tooth disk 44 is greater than the elastic force of the spring 47. The adjusting bevel tooth disk 44 slides upward axially along the adjusting shaft 43, disengaging from the meshing with the driven bevel tooth 421, thus preventing the flow guide vane 42 from continuing to adjust. The adjusting shaft 43 can continue to drive the connecting seat 45 to compensate for the stroke difference between the two.

[0030] It should be noted that the feed gas, guided downward by the guide vane 42, is further dispersed and slowed down when passing through the inert alumina sphere layer 20. The starting position of the reaction is delayed to the junction of the sphere layer and the catalyst bed 11, and the initial heat release rate is slowed down. Subsequently, the feed gas enters the catalyst bed 11 and undergoes a methanation reaction under the action of the nickel-based catalyst. The heat generated by the reaction is uniformly diffused through the buffer of the inert alumina sphere layer 20 and the heat dissipation of the side wall cooling jacket, avoiding local overheating. The gas after the reaction enters the lower head of the reaction tank 10 and is discharged to the subsequent LNG preparation unit.

[0031] Example 2, based on the above examples, the coke oven gas to LNG co-production ammonia control method further includes a first acquisition module, a second acquisition module and a control module, and each module and motor 20 are connected by wired and / or wireless signals; Specifically, the first acquisition module is an online gas analyzer installed on the gas inlet pipe of the reaction tank 10, which is used to collect the carbon dioxide concentration value in the raw gas in real time and label it as C. The online gas analyzer is such as an infrared analyzer. The second acquisition module is a flow meter, used to collect the volumetric flow rate of the raw gas in real time, denoted as Q.

[0032] The control module is a distributed control system or a programmable logic controller. The control module is used to periodically execute control methods, which specifically include the following steps: S1, acquire operating data, which includes carbon dioxide concentration and raw gas volume flow rate; S2 compares the operating data with preset thresholds and generates an operating condition judgment based on the comparison results; the preset thresholds include the raw gas carbon dioxide concentration threshold and the raw gas flow rate threshold, respectively marked as... and ; S3, if and If the reaction is in a stable condition, a reset command is generated. like or If any of the conditions are met, the reaction is determined to have a risk of exothermic exacerbation, is in a risky operating condition, and an adjustment command is generated.

[0033] It is worth mentioning that the carbon dioxide concentration threshold of the feed gas is determined based on the stability requirements of the feed gas components and is used to assess the potential exothermic risk caused by changes in the feed gas composition; the feed gas flow rate threshold is determined based on the design load and is used to assess the potential exothermic risk caused by changes in the feed load. The specific values ​​of the preset thresholds are set by those skilled in the art based on the catalyst characteristics, design process and safety requirements, and are not specifically limited here.

[0034] Specifically, if a reset command is generated, the controller first checks the current position or feedback signal of the motor 50, for example, by determining the rotation angle of the adjusting shaft 43 through the encoder; if the motor 50 is not currently in the position corresponding to the initial state, that is, the guide vane 42 is not at the initial angle, the controller generates and sends a reset command to the motor 50, that is, drives the motor 50 to reverse until the guide vane 42 returns to the initial angle, and at the same time the conical net bag 46 descends to the bottom, and the inert alumina ball layer 20 returns to a flat distribution; if the motor 50 is already in the position corresponding to the initial state, the controller does not send an action command, the motor 50 maintains its current position, and the system remains in the initial state; If an adjustment command is generated, the controller sends an adjustment command to the motor 50, driving it to rotate forward. This drives the adjustment bevel gear disk 44 to rotate via the adjustment shaft 43, causing all the guide vanes 42 to deflect synchronously to a preset angle, guiding the airflow to diffuse towards the side wall of the reaction tank 10. At the same time, the connecting seat 45 is driven to rise along the guide rod 411 via the spiral groove at the bottom of the adjustment shaft 43, thereby lifting the conical net bag 46 via the connecting frame 461, changing the shape of the inert alumina sphere layer 20 to a hill-like distribution that is "high in the middle and low around the edges".

[0035] The exemplary implementation of the solution proposed in this disclosure has been described in detail above with reference to preferred embodiments. However, those skilled in the art will understand that various modifications and alterations can be made to the above specific embodiments without departing from the spirit of this disclosure, and various combinations can be made to the various technical features and structures proposed in this disclosure without exceeding the protection scope of this disclosure, which is determined by the appended claims.

Claims

1. A coke oven gas to LNG co-production ammonia synthesis unit, comprising a methanation reactor (10), wherein a catalyst bed (11) is provided inside the reactor (10), characterized in that: An inert alumina sphere layer (20) is disposed above the catalyst bed (11), and an active distribution control component (40) is disposed above the inert alumina sphere layer (20). The active distribution control component (40) includes a vertically arranged adjustment shaft (43), a motor (50) that drives the adjustment shaft (43) to rotate, a plurality of guide vanes (42) driven by the adjustment shaft (43) through a first transmission mechanism and distributed circumferentially, and a conical net bag (46) driven by the adjustment shaft (43) through a second transmission mechanism and partially housed in the inert alumina spherical layer (20). When the motor (50) drives the adjusting shaft (43) to rotate, it simultaneously changes the deflection angle of the guide vane (42) and the vertical height of the conical net (46).

2. The coke oven gas to LNG co-production ammonia unit according to claim 1, characterized in that, The first transmission mechanism includes an adjusting bevel gear disk (44) coaxially sleeved on the adjusting shaft (43) and driven bevel gears (421) disposed at the shaft ends of each guide vane (42). The adjusting bevel gear disk (44) meshes with each driven bevel gear (421). A keyway and a key are provided between the adjusting shaft (43) and the adjusting bevel gear disk (44) to realize circumferential transmission and axial relative sliding.

3. A coke oven gas to LNG co-production ammonia unit according to claim 2, characterized in that, The second transmission mechanism includes a spiral groove opened at the bottom of the adjusting shaft (43), a connecting seat (45) sleeved at the bottom of the adjusting shaft (43), and a conical net bag (46) fixed below the connecting seat (45). The inner hole of the connecting seat (45) is provided with a protrusion that mates with the spiral groove; the connecting seat (45) is connected to the fixed component through a guide mechanism, which limits it to moving only in the vertical direction.

4. A coke oven gas to LNG co-production ammonia production unit according to claim 3, characterized in that, The guiding mechanism includes at least two guide rods (411) fixed to the bottom of the fixed cylinder (41), and the connecting seat (45) has a guide hole that cooperates with the guide rods (411).

5. A coke oven gas to LNG co-production ammonia unit according to claim 3, characterized in that, A spring (47) is sleeved on the adjusting shaft (43), and the spring (47) is used to provide a downward elastic force to the adjusting bevel gear disk (44); the active distribution control assembly (40) also includes a mechanical limiting mechanism for limiting the maximum rotation angle of the guide vane (42).

6. A coke oven gas to LNG co-production ammonia unit according to claim 1, characterized in that, An annular distributor (30) is installed between the top air inlet of the reaction vessel (10) and the active distribution control component (40). The annular distributor (30) includes a fixed disk (31), a gas distribution disk (32) and a sealing disk (33) arranged coaxially, which together form a uniform gas space. The gas distribution disk (32) has uniformly distributed gas distribution grooves (322) on its outer periphery.

7. A method for controlling the co-production of LNG and synthetic ammonia from coke oven gas according to any one of claims 1-6, characterized in that the method... include: S1, real-time collection of carbon dioxide concentration and volumetric flow rate of raw gas entering the reaction tank (10), labeled as C and Q respectively; S2, compare C and Q with the raw gas carbon dioxide concentration threshold and the raw gas flow rate threshold, respectively. The raw gas carbon dioxide concentration threshold and the raw gas flow rate threshold are labeled as follows: and ; S3, if and Then, control the motor (50) to drive the adjusting shaft (43) to rotate, so that the guide vane (42) is reset to the initial angle and the conical net bag (46) is lowered; like or Then control the motor (50) to drive the adjustment shaft (43) to rotate, so that the guide vane (42) deflects to the guide angle and the conical net bag (46) rises.

8. The method for controlling the co-production of ammonia from coke oven gas to LNG according to claim 7, characterized in that, In step S3, the step of controlling the motor (50) to drive the adjustment shaft (43) to rotate includes: when it is determined that the guide vane (42) needs to be reset, the motor (50) reverses; when it is determined that the guide vane (42) needs to be deflected to the guide angle, the motor (50) rotates forward.

9. The method for controlling the co-production of ammonia from coke oven gas to LNG according to claim 7, characterized in that, In step S3, before controlling the motor (50) to move, the current position signal of the motor (50) or the adjusting shaft (43) is obtained; if the current position already corresponds to the target state, the current state is maintained.

10. The method for controlling the co-production of ammonia from coke oven gas to LNG according to claim 7, characterized in that, The initial angle of the guide vane (42) is configured to allow the airflow to flow uniformly downwards across the cross-section of the reaction vessel (10), and the guide angle is configured to allow the airflow to diffuse toward the sidewall of the reaction vessel (10).

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