Coalbed methane decarbonization and hydrogen production process and automatic control system

Abstract

The present invention relates to a coalbed methane decarbonization and hydrogen production process and an automatic control system. A decarbonization and hydrogen production unit comprises: a reactor (1) comprising a reaction zone (9), wherein a reaction tank (2) is provided in the reaction zone (9), the reaction tank (2) is provided with a plurality of natural gas inlets evenly distributed on the reaction tank (2), the natural gas inlets are in communication with an external coalbed methane source (23), a first valve (26) for controlling the opening and closing of each natural gas inlet is provided at the natural gas inlet, and the first valves (26) are arranged independently of one another; a regulating assembly configured to regulate reaction conditions inside the reaction tank (2); and a controller in signal connection with the first valves (26) and the regulating assembly.

Description

Coal-sea natural gas decarbonization hydrogen production process and automated control system

[0001] This application claims priority to Chinese Patent Application No. CN202411993340.9, filed with the China National Intellectual Property Administration on December 31, 2024, entitled "Coal Seam Natural Gas Decarbonization Hydrogen Production Process and Automated Control System", the entire contents of which are incorporated herein by reference. Technical Field

[0002] This invention relates to the field of hydrogen production technology, and in particular to a process and automated control system for hydrogen production from coalbed methane decarbonization. Background Technology

[0003] Hydrogen can be produced through various methods, including water electrolysis, water-gas production, production from syngas and natural gas obtained from petroleum thermal cracking, coalbed methane production, coke oven gas refrigeration, as a byproduct of brine electrolysis, as a byproduct of the brewing industry, and the reaction of iron with steam. However, the efficiency of coalbed methane production is relatively low among existing technologies.

[0004] Therefore, how to improve the hydrogen production efficiency of coalbed methane hydrogen production reaction has become a technical problem that urgently needs to be solved by those skilled in the art. Summary of the Invention

[0005] The purpose of this invention is to provide a process and automated control system for decarbonizing coalbed methane to produce hydrogen, so as to improve the hydrogen production efficiency of the coalbed methane hydrogen production reaction.

[0006] To achieve the above objectives, the present invention provides the following solution:

[0007] This invention provides an automated control system for decarbonization and hydrogen production from coalbed methane. The automated control system for decarbonization and hydrogen production from coalbed methane includes several sets of decarbonization and hydrogen production mechanisms, and each decarbonization and hydrogen production mechanism includes a decarbonization and hydrogen production unit.

[0008] The decarbonization hydrogen production unit includes:

[0009] The reactor includes a reaction tank and a hydrogen outlet connected to the reaction tank. Several natural gas inlets are uniformly distributed on the reaction tank, connected to the reaction tank, and facing the catalyst within the reaction tank. Each natural gas inlet is connected to an external coalbed methane source. A first valve is provided at each natural gas inlet to control the flow of the natural gas, and these first valves are independently configured.

[0010] The feeding assembly includes a feeding component and a distributing component. The feeding component is used to add a set amount of catalyst into the reaction tank, and the distributing component is used to evenly distribute the catalyst in the reaction tank.

[0011] An adjustment component, the adjustment component being used to adjust the reaction conditions within the reaction tank;

[0012] The controller is signal-connected to the first valve and the regulating component respectively;

[0013] Before the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment component to adjust the reaction conditions of the reactor to set conditions, including temperature and oxygen concentration. When the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment parameters of the first valve, including the opening timing, opening duration, and opening degree of the first valve.

[0014] Furthermore, the present invention also provides a process for producing hydrogen from coalbed methane through decarbonization, comprising:

[0015] Step S1: Expel the air from the reactor, inject a set amount of inert gas, and adjust the temperature in the reaction tank to a set value;

[0016] Step S2: Add a set amount of catalyst to the reaction tank inside the reactor and evenly disperse the set amount of catalyst in the reaction tank; introduce natural gas into the reaction tank in the direction of the catalyst, and adjust the introduction area and release amount of natural gas according to the state change of the catalyst during the reaction process;

[0017] Step S3: Based on the state changes of the catalyst and product in the reaction tank, add catalyst to the reaction tank periodically and output the product from the reaction tank.

[0018] In step S2, before the natural gas enters the reaction tank, the natural gas first exchanges heat with the hydrogen discharged from the reaction tank. Then, the natural gas enters the low-temperature zone of the reactor for a second heat exchange before entering the reaction tank.

[0019] The present invention achieves the following technical effects compared to the prior art:

[0020] The automated control system for decarbonization and hydrogen production from coalbed methane in this invention includes several decarbonization and hydrogen production units. Each decarbonization and hydrogen production unit includes: a reactor comprising a reaction zone, a reaction tank within the reaction zone, a hydrogen outlet connected to the reaction tank on the reaction zone, and several natural gas inlets uniformly distributed on the reaction tank, connected to the reaction tank, and facing the catalyst within the reaction tank. The natural gas outlet is connected to an external coalbed methane source. Each natural gas inlet is equipped with a first valve, and each first valve is independently configured. A controller is connected to the first valve and an adjustment component. The controller controls the adjustment parameters of the first valve, including the opening timing, opening duration, and opening degree of the first valve. Before the decarbonization and hydrogen production unit operates, the controller controls the adjustment component to adjust the reaction conditions of the reactor to set conditions, including temperature and oxygen concentration.

[0021] Based on the above structure, it should be noted that: ① The reactor is equipped with a reaction tank. Compared with the method of directly introducing natural gas into the reaction zone in the prior art, the reaction tank reduces the reaction space between natural gas and catalyst, and realizes the aggregation of natural gas. This allows natural gas to directly contact the catalyst after entering the reaction tank from the natural gas inlet and react with the catalyst accordingly. This reduces the problem in the prior art where natural gas is injected from the top of the reaction zone and can only move downward to contact the catalyst after filling the upper space of the reaction zone. This accelerates the rate at which natural gas enters the reaction tank and begins to contact the catalyst for reaction.

[0022] ②In this invention, several natural gas inlets are evenly distributed on the reaction tank, which allows the natural gas entering the reaction tank from the natural gas inlet to react with a sufficient amount of catalyst in the area where the natural gas inlet is located. This ensures that the natural gas hydrogen production reaction can be fully catalyzed, reducing the problem of low hydrogen production efficiency caused by too much or too little natural gas or catalyst participating in the reaction.

[0023] ③ The first valves are set independently of each other, and each first valve is connected to the controller signal. The controller can change the adjustment parameters of the first valves, including opening time, opening timing and opening degree. This allows the natural gas required for the reaction to be added to the reaction tank step by step, so that the catalyst in the reaction tank can react efficiently and fully with an appropriate amount of natural gas per unit time. This reduces the problem of over-catalysis of the catalyst and excessive carbon adsorption on the catalyst due to the limited number of active sites of the catalyst in the reaction tank, which deactivates the catalyst and reduces the efficiency of hydrogen production from natural gas. This further improves the efficiency of hydrogen production from natural gas in the present invention.

[0024] As can be seen from the above, the present invention effectively reduces the problems of insufficient contact between the catalyst and coalbed natural gas and catalyst deactivation due to carbon deposition through the above structure, thereby significantly improving the hydrogen production efficiency of coalbed natural gas. Attached Figure Description

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

[0026] Figure 1 is a schematic diagram of the automated control system for decarbonization and hydrogen production from coal seam natural gas.

[0027] Figure 2 is a front view schematic diagram of the automated control system for coalbed methane decarbonization and hydrogen production.

[0028] Figure 3 is a side view of the automated control system for decarbonization and hydrogen production from coal seam natural gas after the side shell is removed.

[0029] Figure 4 is a schematic diagram of the transfer mechanism;

[0030] Figure 5 is a longitudinal section of the transfer mechanism;

[0031] Figure 6 is a top view of the automated control system for coalbed methane decarbonization and hydrogen production;

[0032] Figure 7 is a structural schematic diagram of the feeding component and the cloth feeding component;

[0033] Figure 8 is a side view of the feeding component and the cloth component;

[0034] Figure 9 is a schematic diagram of the reaction tank;

[0035] Figure 10 is a schematic diagram of the longitudinal section of the reaction tank;

[0036] The components include: 1. Reactor; 2. Reaction tank; 3. Hydrogen outlet; 4. Observation window; 5. Feeding component; 6. Feeding component; 7. Hopper; 8. Meter; 9. Feeding plate; 10. Inlet; 11. Outlet; 12. Second track; 13. Product collection area; 14. Catalyst loading area; 15. First cover plate; 16. Second cover plate; 17. First collection bin; 18. Preheating zone; 19. Reaction zone; 20. Cooling zone; 21. Temperature control. Components; 22. Heat exchanger; 23. External coal seam natural gas source; 24. Hydrogen storage tank; 25. Reactor tank replacing submarine compartment; 26. First valve; 27. Sealing cover; 28. Second vent valve; 29. ​​Gas replacement valve; 30. Second metering plate; 31. Air inlet; 32. Glove box; 33. Partition plate; 34. Fourth drive component; 35. Rotary drive equipment; 36. Hydrogen zone; 37. Nitrogen zone; 38. Boundary line; 39. Receiving box. Detailed Implementation

[0037] 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, and 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.

[0038] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0039] As shown in Figures 1 to 10, this invention discloses an automated control system for decarbonization and hydrogen production from coalbed methane. The automated control system includes several sets of decarbonization and hydrogen production mechanisms, each including a decarbonization and hydrogen production unit. Each decarbonization and hydrogen production unit includes: a reactor 1, with a reaction tank 2 inside; a hydrogen outlet 3 connected to the reaction tank 2 on the reactor 1; and several natural gas inlets evenly distributed on the reaction tank 2, connected to the reaction tank 2, and facing the catalyst inside the reaction tank 2. The natural gas inlets are connected to an external coalbed methane source 23. A first valve 26 for controlling the opening and closing of the natural gas inlets is provided at each natural gas inlet, and each first valve 26 is independently configured. A feeding assembly includes a feeding component 5 and a distributing component 6. The feeding component 5 is used to add a set amount of catalyst to the reaction tank 2, and the distributing component 6 is used to evenly distribute the catalyst within the reaction tank 2.

[0040] The detection component of this invention is used to detect the state of the catalyst in the reaction tank. The detection component includes a first detection element located at the hydrogen outlet and a second detection element located on the reaction tank. The first detection element can be a flow sensor and a concentration sensor. By detecting the hydrogen flow rate and concentration at the hydrogen outlet, and comparing it with the natural gas intake, temperature, and reaction time, an algorithm is used to determine whether the catalyst is deactivated or if there is a problem with the natural gas-to-hydrogen ratio in the reactor, and then adjustments are made accordingly to the natural gas supply or catalyst supply. Depending on the specific type and function of the second detection element, it can be located inside or on the reaction tank. Specifically, the second detection element can be an image sensor, a weight sensor, or an ultrasonic sensor. The second detection element must be made of high-temperature resistant material or have a high-temperature resistant layer on its surface to ensure that it can withstand high temperatures without damage after entering the reactor with the reaction tank. The detection component also includes a third detection element located outside the reactor. Specifically, it can be an infrared sensor or an acoustic sensor. The third detection element faces the reaction tank and can rotate with the movement of the reaction tank, thereby achieving remote detection of the catalyst state within the reaction tank. The regulating component is used to regulate the reaction conditions within the reaction tank 2. The controller is connected to the first valve 26, the detection component, and the regulating component via signals. Before the decarbonization and hydrogen production unit is in operation, the controller controls the regulating component to adjust the reaction conditions of the reactor 1 to the set conditions, including temperature and oxygen concentration. When the decarbonization and hydrogen production unit is in operation, the detection component is used to feed back the status of the catalyst in the reaction tank 2 to the controller. The controller is used to control the regulating parameters of the first valve 26 based on the feedback from the detection component. The regulating parameters include the opening timing, opening duration, and opening degree of the first valve 26.

[0041] Based on the above structure, it should be noted that: ① The present invention adds a set amount of catalyst to the reaction tank 2 through the feeding component 5. This alleviates the problem that the hydrogen production reaction of natural gas cannot be fully catalyzed due to insufficient catalyst addition, resulting in low hydrogen production efficiency. It also reduces the problem that excessive catalyst addition leads to excessive or uneven contact between the catalyst and natural gas, causing the reaction to be too violent, resulting in a large amount of carbon deposits adsorbed on the catalyst, leading to catalyst deactivation and reduced hydrogen production efficiency of natural gas. Furthermore, the present invention distributes the catalyst evenly in the reaction tank 2 through the distribution component 6. This increases the catalytic surface area in the reaction zone 19 and the contact area between natural gas and catalyst. It reduces the problem that the carbon deposits generated by natural gas are concentrated in a local area in the reaction tank 2 due to the catalyst being concentrated in a local area, leading to catalyst deactivation and reduced hydrogen production efficiency of natural gas. This improves the hydrogen production efficiency of natural gas.

[0042] ② The reactor 1 is equipped with a reaction tank 2. Compared with the method of directly introducing natural gas into the reaction zone 19 in the prior art, the reaction tank 2 reduces the reaction space between natural gas and catalyst, realizes the aggregation of natural gas, and allows natural gas to directly contact the catalyst after entering the reaction tank 2 from the natural gas inlet and react with the catalyst accordingly. This reduces the problem in the prior art that natural gas is injected from the top of the reaction zone 19 and can only move downward to contact the catalyst after filling the upper space of the reaction zone 19. This speeds up the rate at which natural gas enters the reaction tank 2 and begins to contact the catalyst for reaction.

[0043] ③ In this invention, the reaction tank 2 is uniformly distributed with several natural gas inlets, which allows the natural gas entering the reaction tank 2 from the natural gas inlet to react with a sufficient amount of catalyst in the area where the natural gas inlet is located, so that the natural gas hydrogen production reaction can be fully catalyzed, reducing the problem of low hydrogen production efficiency caused by too much or too little natural gas or catalyst participating in the reaction.

[0044] ④ The first valves 26 are set independently. The reaction tank 2 is equipped with a detection component for detecting the catalyst state. The detection component and the first valves 26 are all connected to the controller signal. The controller can change the adjustment parameters of the first valves 26 according to the changes in the catalyst state detected by the detection feedback. The adjustment parameters include opening time, opening timing and opening degree. This allows the natural gas required for the reaction to be added to the reaction tank 2 step by step, so that the catalyst in the reaction tank 2 can react efficiently and fully with an appropriate amount (not too much and not too little) of natural gas per unit time. This reduces the problem that due to the limited number of active sites of the catalyst in the reaction tank 2, adding too much natural gas to the reaction tank 2 at one time will cause the catalyst to over-catalyze, produce excessive carbon deposits adsorbed on the catalyst, and deactivate the catalyst, thereby reducing the hydrogen production efficiency of natural gas. This further improves the hydrogen production efficiency of natural gas in the present invention.

[0045] As can be seen from the above, the present invention effectively reduces the problems of insufficient contact between the catalyst and coalbed natural gas, as well as the deactivation of the catalyst by carbon deposition, thereby significantly improving the hydrogen production efficiency of coalbed natural gas.

[0046] It should be noted that, unless otherwise specified, the natural gas and coalbed methane mentioned in this article refer to coalbed methane. However, the coalbed methane decarbonization hydrogen production process and automated control system of this invention can also be applied to the efficient hydrogen production of natural gas or other types of gas whose main component is CH4. The coalbed methane decarbonization hydrogen production automated control system of this invention can be configured with a corresponding number of decarbonization hydrogen production units according to the operating conditions, and each decarbonization hydrogen production unit can also be configured with a corresponding number of decarbonization hydrogen production units according to the operating conditions. In the coalbed methane decarbonization hydrogen production process and automated control system of this invention, automation control refers to the ability, under the action of the controller, to at least control the reaction conditions of reactor 1 and the adjustment parameters of the first valve 26. The reaction formula for coalbed methane hydrogen production in this invention is CH4=C+2H2, and the processes of natural gas generating carbon products and hydrogen are decarbonization and hydrogen production, respectively. The C in the reaction formula can be carbon products such as carbon nanotubes and carbon black, depending on factors such as reaction temperature and catalyst; the catalyst can specifically be a metal-based catalyst, such as a nickel-based catalyst, an iron-based catalyst, or an aluminum-based catalyst.

[0047] The reaction tank 2 can be understood as being located inside the reactor 1, with a volume smaller than the shell or box of the reactor 1, and the reaction tank 2 must have an inlet for adding catalyst. It can be a structure including a bottom plate and side plates, such as a reaction tank 2 with a U-shaped or trapezoidal longitudinal section. This is equivalent to further reducing the space for the natural gas to hydrogen production reaction by setting up a reaction tank 2 inside the reactor 1 that only includes a bottom plate. This reduces the problem of natural gas needing a certain amount of time to diffuse after entering the reaction tank 2 before it can come into contact with the catalyst to react, allowing the natural gas to directly contact the catalyst upon entering the reaction tank 2 and quickly begin the natural gas to hydrogen production reaction, thereby improving the efficiency of natural gas hydrogen production.

[0048] Alternatively, the natural gas inlet can be located at the bottom of the reaction tank 2 and connected to the bottom of the reaction tank 2. Therefore, after entering from the bottom of the reaction tank 2, the natural gas can immediately contact the catalyst and react, accelerating the contact rate between the natural gas and the catalyst, as well as the rate of hydrogen production from natural gas. Furthermore, because the density of natural gas is less than that of air, and the natural gas inlet faces the top of the reaction tank 2, the natural gas, after entering the reaction tank 2, will move upwards under the action of the nozzle and other structures, as well as its own force. In contrast, existing technology injects natural gas from the top of the reaction tank 2. Since the density of natural gas is less than that of air, this means that the natural gas has an upward tendency. Moreover, because the reaction between natural gas and the catalyst is instantaneous, the rising hydrogen produced by the reaction will further drive some natural gas upwards, resulting in a further reduction in the actual amount of natural gas reacting with the catalyst. In other words, the existing method of injecting natural gas from the top of the reaction tank cannot ensure sufficient reaction between the natural gas and the catalyst, resulting in lower hydrogen purity and hydrogen production efficiency. In comparison, it is clear that when the natural gas is located at the bottom of the reaction tank 2, the natural gas in this invention has a greater upward force, allowing it to contact the catalyst more quickly and begin the decarbonization and hydrogen production reaction.

[0049] Furthermore, this invention provides a guide plate at each natural gas inlet at the bottom of the reaction tank 2. The guide plate is inclined relative to the natural gas inlet, which allows the force that sends the natural gas into the reaction tank 2 to be decomposed into a force along the direction of the guide plate and a force perpendicular to the direction of the guide plate. This reduces the force that drives the natural gas upward and lowers the natural gas rising rate, allowing the natural gas to move horizontally along the reaction tank 2 and come into contact with more catalysts. This increases the contact area and reaction time between the natural gas and the catalyst, further improving the hydrogen production efficiency of natural gas in this invention.

[0050] All guide vanes within reaction tank 2 are inclined in the same direction. For example, all guide vanes are positioned to the right of the natural gas inlet, with the left end of the same guide vane lower than its right end. This allows the natural gas to flow from left to right, ensuring contact between the natural gas and all catalysts on the bottom surface of reaction tank 2. Alternatively, the guide vanes on the left half of reaction tank 2 can be positioned to the left of the corresponding natural gas inlet, with the left end of the same guide vane higher than its right end. Similarly, the guide vanes on the right half of reaction tank 2 can be positioned to the right of the corresponding natural gas inlet, with the right end of the same guide vane higher than its left end. This allows the natural gas on the left half of reaction tank 2 to flow from right to left, and on the right half to flow from left to right. This ensures the natural gas reaches the corners of reaction tank 2, reducing the problem of catalyst waste at the corners due to insufficient natural gas flow. In this section, "left" can be understood as the side away from the feed direction, and "right" as the side facing the feed direction. The placement of the baffle is not limited to the above forms, but the baffle must meet the function of "reducing the rate of natural gas rise".

[0051] Furthermore, when the natural gas inlet is located at the bottom of the reaction tank 2, a first nozzle is provided at the natural gas inlet. The first nozzle extends upwards into the reaction tank 2, and several spray holes are arranged around the circumference of the first nozzle. Thus, when natural gas is supplied to the reaction tank 2, the natural gas will be ejected from the spray holes, that is, supplied in a manner that diffuses outwards from the first nozzle as the center. This is suitable for the "sprout-like growth" of carbon products. This causes the natural gas to fill the bottom of the reaction tank 2 first before gradually rising, which further reduces the rate of natural gas rise, prolongs the contact time between natural gas and catalyst, and ensures that the natural gas-to-hydrogen reaction has a high hydrogen production rate. Efficiency; and / or, when the natural gas inlet is located on the first side of the reaction tank 3, the natural gas inlet is equipped with a second nozzle, which is set towards the second side of the reaction tank 2. The first side and the second side are set opposite to each other, which realizes a stepped directional flow of gas from one side to the other. The second nozzle is set parallel to the bottom of the reaction tank 3, which is suitable for the "mushroom growth" of carbon products. This allows the natural gas entering the reaction tank 2 to flow from one side of the reaction tank 2 to the other side, so that the natural gas can "fill" the reaction tank and then rise. This obviously prolongs the contact time between the natural gas and the catalyst, ensuring that the natural gas hydrogen production reaction has a high hydrogen production efficiency.

[0052] Alternatively, natural gas inlets can be installed at the bottom, side, and even top of the reaction tank 2, all facing the catalyst. In this case, when natural gas needs to be released into the reaction tank 2, the controller controls all the first valves 26 to open simultaneously. This allows natural gas released from multiple directions of the reaction tank 2 to come into contact with the catalyst, reducing the problem in the prior art where, after natural gas is introduced from above the reaction tank 2 and reacts with the catalyst to produce carbon products, carbon deposits cover the catalyst surface, causing the active sites of the catalyst to be covered, making it difficult for subsequent natural gas to come into contact with the catalyst, and the hydrogen production reaction of natural gas cannot be fully catalyzed, resulting in low efficiency of natural gas hydrogen production.

[0053] The external coalbed methane source 23 can be a storage tank containing coalbed methane, which is connected to the natural gas inlet via a pipeline, or a coal seam containing coalbed methane. In this case, the coalbed methane extracted from the coal seam can be transported to the natural gas inlet via a pipeline. Both the pipeline and the pipeline are equipped with pumps that can input natural gas into the reaction tank 2 through the natural gas inlet, as well as valves that control the opening and closing of the pipeline or the pipeline.

[0054] The first valve 26 can specifically be an explosion-proof solenoid valve, or a valve that controls whether natural gas enters the inlet. The independent configuration of the first valves 26 means that the controller can control one first valve 26 independently without affecting the others. This facilitates independent control of each valve within the reaction tank 2, allowing the controller to supply different amounts of natural gas to different points and zones within the reaction tank 2 based on the status of the natural gas in the reaction tank 2 as reported by the detection components, thereby maintaining a high-efficiency reaction rate between the natural gas and the catalyst.

[0055] Furthermore, while ensuring the addition of a set amount of catalyst to the reaction tank 2, the feeding component 5 has various different forms. Similarly, while ensuring the uniform distribution of catalyst in the reaction tank 2, the distributing component 6 also has various different structures. As shown in Figures 1-3, 8, and 9, the feeding assembly includes a hopper 7 for storing catalyst, with a first outlet and the feeding component 5 having a second outlet. The feeding component 5 includes a metering device 8 connected to the hopper 7. The metering device includes a first metering plate and a second metering plate 30 arranged vertically. The metering device 8 can rotate relative to the hopper 7. During the rotation of the metering device 8 or the hopper 7, the first outlet and the second outlet are intermittently connected. The first outlet and the second outlet can accommodate the same set amount of catalyst. Thus, by rotating the hopper 7 or the metering device 8 a corresponding number of times, the feeding component 5 can output a set amount of catalyst, i.e., the amount required for the current reaction. For example, if the first outlet and the second outlet can only accommodate 10g of catalyst, then the metering device 8 can rotate one revolution relative to the hopper 7, and the hopper 7 can release 10g of catalyst. The metering device 8 rotates relative to the hopper 7. This rotation can be achieved by a rotary drive structure such as a rotary motor. The metering device 8 can be understood as a plate with metering holes, i.e., a second outlet. The function of the metering device 8 rotating relative to the hopper 7, i.e., the feeding of the feeding component 5, can be achieved either by the operator manually manipulating the drive structure to rotate the metering device 8 or the hopper 7 a certain number of times, or by connecting the drive structure to the controller signal and installing a displacement sensor, such as an angle sensor, on the metering device 8 or the hopper 7 which is connected to the drive structure. The displacement sensor is then connected to the controller signal. In this case, the controller can periodically start the drive structure according to the feeding command pre-input by the operator, and drive the metering device 8 to rotate relative to the hopper 7 a certain number of times to add the set amount of catalyst into the reaction tank 2.

[0056] The feeding component 5 may not use the metering device 8. In this case, the feeding component 5 includes a weight sensor on the hopper 7, a baffle plate at the first outlet, and a first drive component connected to the baffle plate for blocking and opening the first outlet. The weight sensor is connected to the display screen. The operator can then control the opening time of the first outlet via the first drive component based on the weight data of the catalyst in the hopper 7 displayed on the screen, thereby adding a set amount of catalyst to the reaction tank 2. Alternatively, the weight sensor and the first drive component can be connected to the controller, allowing the operator to input commands to the controller, which will then periodically and quantitatively add catalyst to the reaction tank 2 according to the commands. The baffle plate needs to be large enough to completely block the first outlet. Depending on the movement of the baffle plate, a linear drive device such as a cylinder or a rotary drive device 35 such as a rotary motor can be selected. Meanwhile, another weight sensor can be installed in the reaction tank 2. By comparing the readings of the weight sensor on the reaction tank 2 and the weight sensor on the hopper 7, the amount of catalyst released in the reaction tank 2 can be accurately determined, thereby controlling whether the feeding component 5 continues to feed into the reaction tank 2.

[0057] Furthermore, the above two forms of the feeding component 5 can be combined with the metering device 8, weight sensor, baffle plate and other structures to realize the quantitative feeding function of the feeding component 5. In this way, even if the metering device 8 has an unexpected failure, the quantitative feeding function can be successfully realized by delaying or closing the first outlet in advance. It is also necessary to ensure that the metering device 8 and the baffle plate are set to avoid each other so that their respective functions can be realized smoothly.

[0058] As shown in Figures 8 and 9, the feeding component 6 includes a feeding plate 9 located on the side of the feeding component 5 near the reaction tank 2. The feeding plate 9 is inclined relative to the metering device 8 and faces the reaction tank 2. The second outlet is connected to the feeding plate 9. The feeding plate 9 is connected to the driving device, which drives the feeding plate 9 to rotate or move along the reaction tank 2, so that the catalyst is evenly dispersed in the reaction tank 2. To achieve this function, when the driving device drives the feeding plate 9 to rotate, the feeding plate 9 needs to be located in a relatively central area of ​​the reaction tank 2; when the driving device drives the feeding plate 9 to move along a certain direction of the reaction tank 2 (such as the length or width direction), the feeding plate 9 not only needs to be located in the area above the reaction tank 2, but the feeding plate 9 also needs to be able to move from one side of the reaction tank 2 to the opposite side; and Regardless of whether the drive device rotates the feeding plate 9 or moves it along the reaction tank 2, the feeding plate 9 must be able to receive the catalyst released by the feeding component 5 so that the catalyst can be evenly dispersed in the reaction tank 2. Depending on the movement type of the feeding plate 9, a rotary drive device 35 such as a rotary motor or a linear drive device such as an electric push rod can be selected; alternatively, the drive device can be omitted, and the feeding plate 9 can be connected to the metering device 8, so that the metering device 8 rotates while the feeding plate 9 rotates synchronously through the drive structure; and / or, the feeding component 6 includes a first vibrator provided on the feeding component 5 and / or the reaction tank 2. The first vibrator provided on the reaction tank 2 and / or the feeding component 5 ensures that the catalyst will not be blocked at the second outlet and can fall into the reaction tank 2 in a relatively dispersed and even manner. The operating frequency, operating time, and timing of the above-mentioned drive device and the first vibrator can be manually controlled by the operator, or the drive device and the first vibrator can be connected to the controller signal, and instructions can be input to the controller so that the controller automatically drives the drive device and / or the first vibrator to operate under the action of the instructions.

[0059] It should be noted that the second outlet of the feeder 5 does not mean that the feeder 5 also has a first outlet. The second outlet is only for easy distinction from the first outlet of the hopper 7. The third to eighth outlets mentioned later also have this meaning. The set amount of catalyst refers to the amount of catalyst that can meet the reaction requirements.

[0060] In this invention, the reaction tank 2 can also be configured in various ways. The decarbonization and hydrogen production unit includes a conveying assembly, which includes a first track arranged along the feed direction. The first track extends from the feed inlet 10 of the reactor 1 to the discharge outlet 11 of the reactor 1. Several reaction tanks 2 are arranged on the first track. The reaction tanks 2 are connected to a second driving component for transmission. The driving component is used to drive the reaction tanks 2 to move in the feed direction and enter and leave the reactor 1. The feed direction refers to the direction in which the catalyst moves with the reaction tank 2 after a set amount of catalyst is added to the reaction tank 2, i.e., the direction of movement of the reaction tank 2 within the reactor 1. The driving component can drive the reaction tanks 2 to move along the first track in the feed direction until the catalyst in the reaction tank 2 completes the catalytic reaction of the corresponding amount of natural gas. Depending on the arrangement and movement of the reaction tank 2, the drive unit can be selected with a corresponding structure. For example, if the reaction tank 2 is slidably coupled with the first track, the drive unit can be a linear drive device such as a cylinder. In this case, the output shaft of the linear drive device needs to be long enough to push the reaction tank 2 out of the feed port 10 and out of the discharge port 11. Alternatively, the first track can be filled with reaction tanks 2. In this case, when a reaction tank 2 in the reactor 1 has completed the reaction and needs to be output from the reactor 1, in order to ensure the continuity of hydrogen production, a reaction tank 2 filled with catalyst needs to be input into the reactor 1. In this case, the linear drive device does not need to be lengthened. The linear drive device is set towards the feed port 10. After the linear drive device pushes the reaction tank 2 filled with catalyst into the reactor 1, the reaction tank 2 that has completed the reaction is automatically output from the reactor 1 under the push of the subsequent reaction tank 2. If the bottom of the reaction tank 2 is equipped with a pulley, and the pulley is slidably coupled with the first track, the drive unit can be a rotary motor such as a servo motor or other rotary drive device 35. In this case, the drive unit can be set on the reaction tank 2 so that the reaction tank 2 can run along the feed direction on the first track.

[0061] As shown in Figures 1, 2, 6, and 7, the decarbonization hydrogen production structure includes two decarbonization hydrogen production units arranged side by side with opposite feeding directions; a transfer mechanism located near the inlet 10 of one reactor 1 and the outlet 11 of the other reactor 1; the transfer mechanism includes a second track 12 extending from the inlet 10 of one reactor 1 towards the outlet 11 of the other reactor 1; a product collection area 13 along the path of the second track 12; a third drive unit for moving the reaction tank 2 along the second track 12; and a detector group including a first detector located inside the reaction tank 2, a second detector located in the reaction tank 2, and / or... The second detector is located on the second track 12, the inlet 10 and the outlet 11. The first detector is used to detect the product retention status in the reaction tank 2, and the second detector is used to detect the movement position of the reaction tank 2. The discharge assembly is used to completely transfer the product in the reaction tank 2 to the product collection area 13. The transfer assembly is used when the transfer mechanism is in operation. The transfer assembly transfers the reaction tank 2 located at the outlet 11 of one of the reactors 1 to the second track 12. The third drive unit drives the reaction tank 2 on the second track 12 to move towards the inlet 10. The transfer assembly transfers the reaction tank 2 that has been discharged from the product collection area 13 to the first track located at the inlet 10 of the other reactor 1.

[0062] The distance between the inlet and outlet of the reactor is greater than the length of the first track in the direction from the outlet of one reactor to the inlet of the other reactor. This shortens the path of the reactor tank after it exits the reactor outlet and re-enters the reactor, thus shortening the interval between two reactions in the reactor.

[0063] When the conveying assembly of one of the decarbonization hydrogen production units pushes the product, such as carbon, from the reactor 1 out of the reactor 2, the transfer assembly transfers the reactor 2 from the first track of the decarbonization hydrogen production unit to the second track 12. A third drive unit then moves the reactor 2 along the second track 12 towards the inlet 10 of another decarbonization hydrogen production unit. During this movement, the reactor 2 passes through the product collection area 13. The discharge assembly completely transfers the product from the reactor 2 into the product collection area 13 to prevent carbon buildup in the reactor 2 from adsorbing onto the surface of the subsequently loaded catalyst, which could lead to catalyst deactivation and a decrease in the natural gas hydrogen production rate. After the discharge assembly has completely transferred the product from the reactor 2 to the product collection area 13, the third drive unit continues to move the reactor 2 towards the inlet 10 of another decarbonization hydrogen production unit until it reaches the inlet 10. Then, the transfer assembly transfers the reactor 2 from the second track 12 to the first track of the other decarbonization hydrogen production unit, where a second drive unit moves the reactor 2 into the reactor 1.

[0064] Clearly, the transfer mechanism enables the feeding and discharging cycle of the two decarbonization hydrogen production units. Specifically, when a reaction tank 2 outputs from reactor 1 of one decarbonization hydrogen production unit, after unloading, it can move towards the feeding direction of another decarbonization hydrogen production unit. After being filled with a set amount of catalyst, it continues to move towards the feeding direction, thus enabling the feeding of the other decarbonization unit. This alleviates the problem of discontinuous hydrogen production and low hydrogen production efficiency caused by having only one decarbonization hydrogen production unit, where after discharging from reaction tank 2, it is necessary to transfer reaction tank 2 from the discharge port 11 to the feed port 10 of the decarbonization hydrogen production unit, resulting in an interval in the feeding of the decarbonization hydrogen production unit. This significantly improves the hydrogen production efficiency of the automated control system for decarbonization hydrogen production from coalbed methane in this invention.

[0065] Based on the feedback from the first detector, it is determined whether the carbon product in the reaction tank 2 has been completely discharged. Based on the feedback from the second detector, it is determined whether the reaction tank 2 is located on the second track 12, whether the reaction tank 2 has reached the second track 12, whether it has reached the product collection area 13, whether it is located at the inlet 10 of one of the reactors 1, and whether it is located at the outlet 11 of the other reactor 1. The first detector can be a weight sensor, an image sensor, or an infrared sensor, etc., capable of detecting product residues in the reaction tank 2. The second detector can be configured in different ways depending on its location. For example, the second detector can be placed solely on the reaction tank 2. A spatial coordinate system is established based on the coalbed methane decarbonization and hydrogen production automation control system of this invention, and the location of the reaction tank 2 is determined based on the real-time position coordinates of the reaction tank 2 fed back by the second detector. In this case, the second detector can be a position sensor or an image sensor, etc., capable of reflecting the location of the reaction tank 2. Alternatively, the second detector can be placed at the inlet 10 of one reactor 1, the outlet 11 of the other reactor 1, and the area on the second track 12 corresponding to the product collection area 13. In this case, the second detector can be a position sensor, an image sensor, or a Hall sensor. When the second detector is a Hall sensor, the location of the reaction tank 2 is determined by the feedback from the Hall sensors at the inlet 10 of one reactor 1, the outlet 11 of the other reactor 1, and the area on the second track 12 corresponding to the product collection area 13.

[0066] The transfer assembly and discharge assembly can be configured in various ways. For example, the transfer assembly includes: a receiving box 39, which is movably mounted on the second track 12. The receiving box 39 has an inlet / outlet on the side facing the discharge port 11 of one of the reactors 1 for the reaction tank 2 to enter and exit. The receiving box 39 has a cavity for accommodating the receiving box 39, and a limiting member within the cavity to prevent the reaction tank 2 from detaching from the receiving box 39. A pushing window with a cross-section smaller than the inlet / outlet is located on the side of the receiving box 39 away from the discharge port 11. The top of the receiving box 39 has a discharge port connected to the reaction tank 2. A third driving component is connected to the receiving box 39 for driving the receiving box 39 to move along the second track 12. When the receiving box 39 moves to the discharge port 11, the inlet / outlet aligns with the reaction tank 2. When the receiving box 39 moves to the inlet 10, ... The third drive component is aligned with the push window; the fourth drive component 34 is positioned close to and towards the feed inlet 10 of another reactor 1, and is located on the extension line of the first track; reaction tanks 2 are continuously distributed from one end of the first track near the feed inlet 10 to the other end near the discharge outlet 11, and the distance between the discharge outlet 11 and the second track 12, as well as the distance between the feed inlet 10 and the second track 12, are both less than the length of the reaction tank 2 in the feeding direction; the discharge assembly includes a second track 12 arranged in a ring shape perpendicular to the plane of the reactor 1, and the discharge assembly includes a second vibrator mounted on the reaction tank 2 and / or the receiving box 39; the product collection area 13 includes a first collection chamber 17 located below the second track 12 and having a first inlet at the top. The first and second vibrators are existing structures that can cause the structure on which the vibrator is mounted to vibrate up and down, or vibrate left and right, or swing around itself, and the specific structure of the vibrator will not be described in detail here.

[0067] As shown in Figure 4, the second track 12 consists of two rows of parallel chains, which are supported by multiple support wheels and driven to rotate. The support wheels are mounted on a rotating shaft, and the other end of the shaft is connected to a rotary drive device 35, such as a rotary motor. The second track 12 is not limited to the above form and can also be a slide rail, guide rail, or other structure that can meet the functions of the second track.

[0068] When the second driving component pushes the reaction tank 2, which has completed the reaction, out of the discharge port 11 of the reactor 1, the third driving component moves the receiving box 39 to the position of the discharge port 11 of the reactor 1 (based on the position of the reaction tank 2 determined by the second detector), so that the inlet and outlet of the reaction tank 2 are aligned with the discharge port 11 of the reactor 1, specifically with the reaction tank 2 located at the discharge port 11 of the reactor 1 at this time. Subsequently, the second driving component continues to move the reaction tank 2 towards the direction closer to the second track 12, so that the reaction tank 2 leaves the first track and enters the receiving box 39. Then, the limiting component acts on the reaction tank 2, ensuring that the reaction tank 2 will not detach from the receiving box 39 or fall out of the receiving box 39 when moving along the second track 12. Subsequently, the third driving component drives the reaction tank 2 to move along the second track 12 towards the feed inlet 10 of the other reactor 1. Since the plane of the second track 12 is perpendicular to the plane of the reactor, and the product collection area 13 is located below the second track 12, and the receiving box 39 is provided with a discharge port communicating with the reaction tank 2, when the reaction tank 2 moves to the product collection area 13, the discharge port will face downwards, i.e., towards the first collection bin 17. The first inlet of the collection chamber 17 must be large enough to prevent leakage of the product from the reaction tank 2 to the outside during unloading. Simultaneously, the second vibrator is activated to ensure that the product in the reaction tank 2 is completely discharged into the first collection chamber 17. Feedback from the first detector determines whether unloading of the reaction tank 2 is complete. If the first detector indicates that there is still material residue in the reaction tank 2, unloading continues in the product collection area 13 until all product is discharged. After unloading of the reaction tank 2, the third drive unit moves the receiving box 39 along the second track 12 towards the feed inlet near the other reactor 1. The reactor continues to push in the direction of 10. When the feedback from the second detector determines that the reaction tank 2 has reached the position on the second track 12 corresponding to the feed inlet 10 of the other reactor 1, the fourth drive unit 34 is activated. The output shaft of the fourth drive unit 34 extends in the feeding direction and into the push window to contact the reaction tank 2 (at this time, the reaction tank 2 needs to have a side shell that can be pushed by the third drive unit). The reactor continues to push the reaction tank 2 in the feeding direction until it is pushed onto the first track of the other reactor 1. Then, the second drive unit of the other reactor 1 drives the reaction tank 2 to move along the feeding direction.

[0069] In this invention, the feeding component is located near the feed inlet of the reactor. During the process of the fourth driving component 34 pushing the reaction tank toward the feed inlet of the reactor, the feeding component adds reactants such as catalysts to the reaction tank.

[0070] The discharge port can be specifically located at the top and / or side of the receiving box 39.

[0071] The limiting component can be a magnet installed inside the cavity. In this case, the reaction tank 2 needs to be made of a magnetic material that can be attracted by the magnet. Alternatively, the limiting component can be a limiting block installed inside the cavity on both sides of the feeding direction. A spring or other reset component is provided between the limiting block and the cavity. A guide surface is provided on the side of the limiting block near the reactor 1. The guide surface is inclined relative to the cavity. There is a gap between the two guide surfaces. The gap on the side of the guide surface near the reactor 1 is larger than the gap on the side of the guide surface away from the reactor 1. The cross-section of the gap between the two guide surfaces is Y-shaped. The bottom of the reaction tank 2 is provided with a pulley that cooperates with the second track 12. In this case, the third driving component can be a rotary driving device 35 installed on the reaction tank 2 and connected to the pulley for transmission, which can drive the pulley to move on the second track 12. For example, a servo motor. The fourth driving component 34 can be a linear driving device such as a cylinder or hydraulic cylinder. The fourth driving component 34 needs to be set to avoid the first track and the second track 12.

[0072] Alternatively, the transfer assembly may not adopt the structure described above. The transfer assembly includes a robotic arm and a drive unit. The drive unit is connected to the robotic arm via a transmission. The drive unit is used to drive the robotic arm to move from the feed port 10 toward the direction close to the second track 12, and to drive the robotic arm to move from the second track 12 toward the direction close to the feed port 10. The robotic arm includes a transmission unit connected to the drive unit. The transmission unit may specifically be a joint or linkage structure connecting the drive unit and the gripper, and a gripper located at the end of the transmission unit away from the drive unit. The gripper is used to grip and release the reaction tank 2. The discharge assembly includes a first chamber door and a third vibrator on the reaction tank 2. The first chamber door is located at the discharge port at the bottom of the reaction tank 2. The second track 12 has a discharge port corresponding to the discharge port. The first chamber door is connected to a fifth drive unit via a transmission. When the third drive unit drives the reaction tank 2 to move to the product collection area 13, the fifth drive unit drives the first chamber door to release the blockage of the discharge port. The product collection area 13 includes a second collection chamber located below the second track 12 and having a second inlet at the top. At this time, the second track 12 is a track set parallel to the plane where the reactor 1 is located.

[0073] Depending on the required degrees of freedom of the robotic arm, the drive unit includes drive structures arranged in multiple directions. The drive unit needs to include a first drive structure that can drive the gripper to clamp and release, a second drive structure that can drive the robotic arm to move from the discharge port 11 of one of the reactors 1 along the second track 12, a third drive structure that can drive the robotic arm to move from the discharge port 11 of one of the reactors 1 towards the inlet 10 of another reactor 1, a fourth drive structure that can drive the robotic arm to move from the second track 12 towards the inlet 10 of another reactor 1, and a fifth drive structure that can drive the robotic arm to move in a vertical plane towards and away from the second track 12; the first to fifth drive structures can be selected from linear drive devices such as cylinders or rotary drive devices such as rotary motors 35, depending on the type of movement of the robotic arm.

[0074] After the reaction tank 2 is discharged from the outlet 11 of one of the reactors 1, the drive unit can drive the robotic arm to move the reaction tank 2 to the second track 12. When the reaction tank 2 moves to the product collection area 13, the first chamber door is driven by the fifth drive unit to move, thereby releasing the blockage of the discharge port. The product in the reaction tank 2 enters the second collection chamber through the discharge port, the discharge port, and the second inlet. After the reaction tank 2 has finished discharging, the drive unit drives the robotic arm to move and transfer the reaction tank 2 to the first track of the other reactor 1.

[0075] Alternatively, the discharge assembly can be omitted. By adding a drive structure inside the drive unit that can rotate the product collection area 13, the drive unit can rotate the reaction tank 2 via a robotic arm to achieve unloading.

[0076] Depending on the operating conditions, the transfer mechanism can be manually operated by the operator; alternatively, the detector group, transfer component, discharge component, third drive component, fourth drive component 34, and fifth drive component in the transfer mechanism can be connected to the controller signal, allowing the operator to manually input operating commands, which will then enable the controller to automatically control the operation of the transfer mechanism. The feeding component 5 can be located between the second track 12 and the feed inlet 10 of the reactor 1, ensuring that the catalyst is loaded before the reaction tank 2 enters the reactor 1.

[0077] It should also be noted that the structures of the detector group and detection components that enter the reactor 1 with the reaction tank 2 are all made of high-temperature resistant materials, or have a high-temperature resistant layer on the corresponding structural surface of the detector group and detection components, so that the structures of the detector and detection components that enter the reactor 1 with the reaction tank 2 can withstand the high temperature of the natural gas reaction without being damaged or malfunctioning.

[0078] As shown in Figures 1, 2, 6, and 7, a set of decarbonization hydrogen production machines includes two decarbonization hydrogen production units. The inlet 10 of reactor 1 constitutes a catalyst filling area 14, and the outlet 11 constitutes a product collection area 13. The catalyst filling area 14 of one reactor 1 and the product collection area 13 of the other reactor 1 are arranged adjacent to each other. The transfer mechanism also includes a partition plate 33 located between the adjacent product collection area 13 and catalyst filling area 14. The partition plate 33 is arranged to avoid the second track 12. The area above the partition plate 33 is the hydrogen area 36, ​​and the area below it is the nitrogen area 37 or other inert gas area. There is a boundary line 38 between the hydrogen area 36 and the nitrogen area 37, and the two areas are divided by the density of the gases themselves. The transfer mechanism also includes a shell fitted outside the second track 12 and the fourth drive component 34. The shell is equipped with structures such as a reaction tank replacement submarine compartment 25, a glove box 32, and an observation window 4. Before the decarbonization and hydrogen production process is operational, the shell must be purged of its internal air by inert gas to create an oxygen-free environment. Specifically, a vacuum valve can be installed on the shell, and the shell can be connected to an inert gas source via a pipeline. When purging, the pump and valve on the inert gas source and the shell pipeline are opened to purge the air through the inert gas. The presence of air can be determined by a gas sensor or other detection mechanism installed on the shell.

[0079] The decarbonization and hydrogen production unit also includes: a first cover plate 15 located at the inlet 10 and a second cover plate 16 located at the outlet 11. When the reactor 1 is independently set up with the transfer mechanism, the first cover plate 15 blocks the inlet 10 under a first force, and the second cover plate 16 blocks the outlet 11 under a second force. By blocking the inlet 10 and the outlet 11 with the first cover plate 15 and the second cover plate 16 respectively, the gas phase environment inside the reactor 1 is maintained. When the reactor 1 is in the feeding state, the first cover plate 15 releases the blockage of the inlet 10 under a third force, and the second cover plate 16 releases the blockage of the outlet 11 under a fourth force. The first cover plate 15 and the second cover plate 16 can have various forms. For example, the first cover plate 15 is rotatably connected to the mounting plate located at the outlet 11, and the size of the first cover plate 15 is larger than the size of the inlet 10 so as to block the inlet 10; or, the size of the first cover plate 15 can be slightly smaller than the size of the inlet 10, and the first cover plate 16 can be used to block the inlet 10. A corresponding sealing element is provided between the first cover plate 15 and the feed inlet 10 to maintain the sealing of the feed inlet 10 by the first cover plate 15. At this time, the first force can be the weight of the first cover plate 15 itself, or a torsion spring is provided at the connection between the first cover plate 15 and the mounting plate, so that the first cover plate 15 seals the feed inlet 10 under the combined action of its own weight and the torsion spring. At this time, the first cover plate 15 is connected to a rotary drive device 35 such as a rotary motor. The rotary drive device 35 drives the first cover plate 15 to rotate, thereby releasing the sealing of the feed inlet 10 by the first cover plate 15. The third force is the force of the rotary drive device 35 driving the first cover plate 15 to move away from the feed inlet 10. The second cover plate 16 is set in the same way as the first cover plate 15. The second force can be the weight of the second cover plate 16 itself, or the combined force of the weight of the second cover plate 16 itself and the torsion spring. The fourth force is the force of the rotary drive device 35 driving the second cover plate 16 to move away from the discharge outlet 11. The first cover plate 15 and the second cover plate 16 can be located outside or inside the reactor 1, depending on the operating conditions.

[0080] The regulating components include: a deoxidizing unit, which includes a first vent valve connected to reactor 1, an external inert gas source connected to the inlet 31 of reactor 1, and the external inert gas source and reactor 1 connected by a pipeline equipped with a pump for supplying inert gas and a second valve located at the inlet 31; before reactor 1 starts reacting, the second valve, the pump, and the first vent valve are opened to inject inert gas into reactor 1 to purge the air inside reactor 1. The inert gas can be nitrogen or other gases that suppress or reduce the risk of hydrogen explosion. The inert gas source refers to a storage tank containing inert gas, which can be configured according to the location of the inert gas in reactor 1. An oxygen sensor or gas analyzer determines whether the air has been completely exhausted and whether an oxygen-free environment has been formed; a temperature regulating component 21 is connected to the reactor 1, and the temperature regulating component 21 can specifically be an electric heating plate installed on the reactor 1; the detection components include a temperature sensor, such as a thermocouple, connected to the reactor 1, as well as a pressure sensor, a gas analyzer, an optical sensor, a camera, an ultrasonic sensor, an infrared sensor, and other detectors that can detect the state of the catalyst in the reaction tank 2. Depending on the operating conditions and the function of the structures in the detection components, the infrared sensor, ultrasonic sensor, and other detection structures can be selectively installed inside the reaction tank or outside the reactor.

[0081] Based on the amount of catalyst added to the reaction tank 2 by the feeder 5, and based on the state changes of the catalyst in the reaction tank 2 fed back by the ultrasonic sensor, infrared sensor, camera, and other structures in the detection component, as well as the concentration and volume of natural gas in the reaction tank 2, the controller adjusts the opening time and opening degree of the first valve 26 (for example, each first valve 26 is opened for 13 seconds, and the natural gas released in 13 seconds can fully react with the catalyst and will not escape outside the reaction tank 2). This controls the amount of natural gas released into the reaction tank 2 to avoid excessive natural gas and the problem of excessive carbon buildup caused by the reaction of natural gas and catalyst. At the same time, by controlling the adjustment parameters of the first valve 26, the controller can also prevent the release of natural gas into a certain part of the reaction tank 2. Excessive natural gas in reactor 2 can cause the remaining natural gas to escape outside reactor 2 and into the space inside reactor 1 after the reaction, flowing from top to bottom into subsequent reactor 2. This results in the natural gas being blocked by carbon deposits before it can fully contact the catalyst, reducing the efficiency of hydrogen production from natural gas. Furthermore, when natural gas is introduced into reactor 2, the first vibrator on reactor 2 can be activated, and / or the first vibrator on reactor 2 can be activated based on feedback from cameras, ultrasonic sensors, infrared sensors, etc., regarding the carbon buildup in reactor 2, to reduce the coverage of the catalyst by carbon deposits. However, it is important to note that the vibration amplitude of the first vibrator should not be too large to prevent accidents such as hydrogen explosions caused by excessive vibration amplitude.

[0082] As shown in Figures 8 and 9, the top of the silo 7 is equipped with a sealing cover 27, a second vent valve 28, and a gas replacement valve 29. The gas replacement valve 29 is connected to an inert gas source. Before the reactor 1 reacts, the second vent valve 28 and the gas replacement valve 29 are opened (the second vent valve 28 and the gas replacement valve 29 are only valves that can control the on and off states). The inert gas enters the reactor 1 through the gas replacement valve, and the air is discharged.

[0083] As shown in Figures 1, 2, 6, and 7, reactor 1 also includes a preheating zone 18, a reaction zone 19, and a cooling zone 20 arranged sequentially and connected along the feed direction. The temperature of the reaction zone 19 is higher than the temperature of the preheating zone 18 and the cooling zone 20. The feed component 5 is connected to the preheating zone 18, the hydrogen outlet 3 is connected to the preheating zone 18, the gas inlet 31 is connected to the cooling zone 20, and the natural gas inlet is connected to an external natural gas source through the gas inlet 31. The preheating zone 18 allows the catalyst to be gradually heated to a suitable reaction temperature. The cooling zone 20 does not actually cool the reactor; it is simply at a lower temperature than the reaction zone 19. The preheating zone 18, the reaction zone 19, and the cooling zone 20 are each connected to an independent temperature regulating component 21, such as an electric heating plate, for heating. The decarbonization hydrogen production unit also includes: a heat exchanger 22, which has a first inlet connected to the hydrogen outlet 3, a second inlet connected to the external coalbed natural gas source 23, a third outlet connected to the gas inlet 31, and a fourth outlet connected to a gas separation and purification device; the gas separation and purification device has a fifth outlet connected to the hydrogen storage tank 24 and a sixth outlet connected to the external coalbed natural gas source 23. Before the reaction, the natural gas undergoes a first preheating process in the heat exchanger 22 with hydrogen that has some residual heat, and a second preheating process in the cooling zone 20, thereby achieving cascaded utilization of the energy in reactor 1 and reducing operating energy consumption. After the natural gas is stored in the hydrogen storage tank 24, it can be transported to a hydrogen refueling station for use.

[0084] When reactor 1 includes a preheating zone 18, a reaction zone 19, and a cooling zone 20, reactor 1 is also provided with an intermediate cavity that is not directly connected to the reaction tank 2. The air inlet 31 is connected to the intermediate cavity. The intermediate cavity is distributed at least in the cooling zone 20, or it can be distributed throughout the entire reactor 1. The intermediate cavity is used to temporarily store natural gas and ensure that natural gas can enter the reaction tank 2 from the natural gas inlet. It also allows the natural gas to exchange heat with the low-temperature zone in reactor 1 before being released into the reaction tank 2, thereby realizing multi-stage utilization of energy in reactor 1. The intermediate cavity is equipped with a nozzle. When the controller detects that the reaction tank 2 has reached the reaction zone 19 or other set start-up position based on the feedback from the position sensor on the reaction tank 2, the nozzle is aligned with the natural gas inlet on the reaction tank 2. To prevent the natural gas ejected from the nozzle from leaking out, the nozzle is aligned with the natural gas inlet when the reaction tank 2 reaches the start-up position. This can be achieved by setting a detection structure on the reaction tank, such as a camera or Hall sensor facing the natural gas inlet, to determine whether the nozzle is aligned with the natural gas inlet. Once the controller determines that the reaction tank 2 has reached the start-up position and the nozzle is aligned with the natural gas inlet of the reaction tank 2 at the reaction position based on the feedback from the detection structure and the position sensor, the controller controls the first valve 26 and the nozzle to open. After the set amount of natural gas has been released, the first valve 26 and the nozzle are closed to prevent natural gas from escaping outside the reaction tank 2. When releasing natural gas into the reaction tank 2, if the opening and closing speed of the first valve 26 and the nozzle and the rate of natural gas release are relatively fast, it is not necessary to stop the movement of the reaction tank 2 along the feeding direction; conversely, if the opening and closing speed of the first valve 26 and the nozzle and the rate of natural gas release are relatively slow, the movement of the reaction tank 2 along the feeding direction can be appropriately slowed down or even stopped.

[0085] Furthermore, the present invention also provides a process for producing hydrogen from coalbed methane through decarbonization, comprising: step S1, discharging air from reactor 1 and injecting a set amount of inert gas, and adjusting the temperature of reactor 1 to a set value; step S2, adding a set amount of catalyst to the reaction tank in reactor 1 and uniformly dispersing the set amount of catalyst in the reaction tank; introducing natural gas into reaction tank 2 towards the catalyst, and adjusting the introduction area and release amount of natural gas according to the state change of the catalyst during the reaction process; step S3, periodically adding catalyst to reaction tank 2 according to the state change of the catalyst and product in reaction tank 2, and outputting the product from reaction tank 2; wherein, in step S2, before the natural gas enters reaction tank 2, the natural gas first exchanges heat with the hydrogen discharged from reaction tank 2, and then the natural gas enters the low-temperature zone, i.e., the cooling zone 20, of reactor 1 for a second heat exchange, and then enters the reaction tank.

[0086] In summary, the coalbed methane decarbonization hydrogen production process and automated control system of this invention have the following significant advantages: ① Compared with reactors in existing technologies, the automated control system for coalbed methane decarbonization hydrogen production in this invention is a circulating dual-channel kiln reactor, which increases the single-time catalyst addition ratio, expands the natural gas cracking reaction area, and realizes increased hydrogen production capacity. The graded arrangement of temperature regulating components can respond quickly according to the stage temperature difference in the reactor, preventing product defects. ② Multi-channel gas supply device for coalbed methane. A diversified, graded, and proportioned supply is adopted to adapt to the morphological changes of the catalyst during the reaction process, increasing the surface area contact between natural gas and catalyst, avoiding reaction attenuation, and improving the natural gas cracking reaction rate. ③ Optimized design of the reaction tank, adopting a graded gas supply mode. This improves catalyst utilization efficiency, prevents supersaturated adsorption, reduces reaction time, and improves product quality stability. It is suitable for "sprout-like growth" catalysts. ④ Automated catalyst filling equipment, adopting a rotary quantitative supply mode. It has its own material distribution component, which works in conjunction with the reaction tank for synchronous feeding. This improves the quantitative controllability of the catalyst and reduces the difficulty of production process operation. ⑤ The transfer mechanism enables efficient filling of reaction tanks and recovery of by-products. This reduces the difficulty of production process operation and saves manpower and resources.

[0087] In this article, "and / or" refers to the fact that within the same sentence, the text preceding "and / or" and the text following "and / or" can exist simultaneously or separately. For example, "A and / or B" includes three cases: either A or B exists alone, or A and B exist simultaneously. "And / or" has the same meaning as "and / or" and will not be elaborated upon here.

[0088] This invention discloses multiple technical solutions, but does not provide any contrary technical teachings.

[0089] Specific examples have been used to illustrate the principles and implementation methods of this invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this invention. Furthermore, those skilled in the art will recognize that, based on the ideas of this invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of this invention.

Claims

1. An automated control system for decarbonization and hydrogen production from coal seam natural gas, characterized in that, The coalbed natural gas decarbonization and hydrogen production automation control system includes several sets of decarbonization and hydrogen production mechanisms, and each decarbonization and hydrogen production mechanism includes a decarbonization and hydrogen production unit. The decarbonization hydrogen production unit includes: The reactor includes a reaction tank and a hydrogen outlet connected to the reaction tank. Several natural gas inlets are uniformly distributed on the reaction tank, connected to the reaction tank, and facing the catalyst within the reaction tank. Each natural gas inlet is connected to an external coalbed methane source. A first valve is provided at each natural gas inlet to control the flow of the natural gas, and these first valves are independently configured. An adjustment component, the adjustment component being used to adjust the reaction conditions within the reaction tank; The controller is signal-connected to the first valve and the regulating component respectively; Before the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment component to adjust the reaction conditions of the reactor to set conditions, including temperature and oxygen concentration. When the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment parameters of the first valve, including the opening timing, opening duration, and opening degree of the first valve.

2. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The natural gas inlet is located at the bottom of the reaction tank and is connected to the bottom of the reaction tank; and / or, the longitudinal section of the reaction tank is U-shaped or trapezoidal; and / or, when natural gas needs to be released into the reaction tank, the controller controls all the first valves to open simultaneously.

3. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The automated control system for decarbonization and hydrogen production from coalbed methane also includes a detection component for detecting the state of the catalyst in the reaction tank. The detection component includes a first detection element located at the hydrogen outlet and a second detection element located on the reaction tank.

4. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The natural gas inlet is also equipped with a guide plate, and the guide plate and the reaction tank are inclined. And / or, the natural gas inlet is located at the bottom of the reaction tank, and a first nozzle is provided at the natural gas inlet. One end of the first nozzle extends into the reaction tank, and a plurality of spray holes are provided along the circumference of the first nozzle. And / or, the natural gas inlet is located on the first side of the reaction tank, and a second nozzle is provided at the natural gas inlet, the second nozzle being arranged facing the second side of the reaction tank, and the first side and the second side of the reaction tank being arranged opposite to each other.

5. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The automated control system for decarbonization and hydrogen production from coalbed methane also includes a feeding assembly, which includes a silo for storing catalyst, a feeder for adding a set amount of catalyst into the reaction tank, and a feeder for evenly distributing the catalyst in the reaction tank. The silo has a first outlet, and the feeder has a second outlet.

6. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 5, characterized in that, The feeding device includes a metering device connected to the hopper, the metering device being rotatable relative to the hopper, and during the rotation of the metering device or the hopper, the first outlet and the second outlet are intermittently connected, and the first outlet and the second outlet can accommodate the same set amount of catalyst; And / or, the fabric component includes a feeding plate disposed on the side of the feeding component near the reaction tank, the feeding plate being inclined relative to the feeding component and facing the reaction tank, the second outlet being connected to the feeding plate, the feeding plate being connected to a driving device for driving the feeding plate to rotate or move along the reaction tank.

7. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 5, characterized in that, The feeding component includes a weight sensor disposed on the hopper, a baffle plate disposed at the first outlet, and a first driving component that is pulsatorically connected to the baffle plate and used to drive the baffle plate to block and open the first outlet; and / or, the feeding component includes a first vibrator disposed on the feeding component and / or on the reaction tank.

8. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The decarbonization hydrogen production unit includes a conveying assembly, which includes a first track arranged along the feeding direction. The first track extends from the feed inlet of the reactor to the discharge outlet of the reactor. A plurality of reaction tanks are arranged on the first track. The reaction tanks are connected to a second driving member for driving the reaction tanks to move in the feeding direction and enter and leave the reactor. The feeding direction is the direction of movement of the reaction tanks in the reactor.

9. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 8, characterized in that, The decarbonization hydrogen production mechanism includes: Two decarbonization hydrogen production units arranged side by side with opposite feeding directions; A transfer mechanism is disposed near the feed inlet of one of the reactors and the discharge outlet of the other reactor; The transit agencies include: A second track is provided, extending from the inlet of one of the reactors toward the outlet of the other reactor, and a product collection area is provided along the path of the second track. A third driving component is used to drive the reaction tank to move along the second track; A discharge assembly for completely transferring the product in the reaction tank to the product collection area; When the transfer mechanism is in operation, the transfer component transfers the reaction tank at the outlet of one of the reactors to the second track. The third drive unit drives the reaction tank on the second track to move towards the inlet of the other reactor. The transfer component then transfers the reaction tank after it has been discharged from the product collection area to the first track at the inlet of the other reactor.

10. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 9, characterized in that, The relay component includes: A receiving box is movably mounted on the second track. The receiving box has an inlet and outlet for entering and leaving the reaction tank on the side facing the discharge port of one of the reactors. The receiving box has a cavity for accommodating the reaction tank. The receiving box has a push window with a longitudinal section smaller than the inlet and outlet on the side away from the discharge port. The receiving box has a discharge port connected to the reaction tank. The third driving component is connected to the receiving box for transmission. The third driving component is used to drive the receiving box to move along the second track. When the receiving box moves to the discharge port, the inlet and outlet are aligned with the reaction tank. When the receiving box moves to the feed port, the third driving component is aligned with the push window. A fourth drive unit is disposed near and toward the feed inlet of another of the reactors, and the fourth drive unit is located on the extension of the first track; The reaction tanks are continuously distributed from one end of the first track near the feed inlet to the other end of the first track near the discharge outlet. The distance between the discharge outlet and the second track, and the distance between the feed inlet and the second track, are both less than the length of the reaction tanks in the feed direction. The discharge assembly includes a second track arranged perpendicularly to the plane of the reactor and in a ring shape; the discharge assembly includes a second vibrator disposed on the reaction tank and / or the receiving box; the product collection area includes a first collection chamber disposed below the second track and having a first inlet at the top.

11. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 9, characterized in that, The transfer assembly includes a robotic arm and a drive unit. The drive unit is connected to the robotic arm via a transmission mechanism. The drive unit is used to drive the robotic arm to move from the feed inlet toward the direction closer to the second track, and to drive the robotic arm to move from the second track toward the direction closer to the feed inlet. The robotic arm includes a transmission unit connected to the drive unit, and a gripper located at the end of the transmission unit away from the drive unit. The gripper is used to grip and release the reaction tank. The discharge assembly includes a third vibrator mounted on the reaction tank and a first gate located at the discharge port at the bottom of the reaction tank. A discharge port corresponding to the discharge port is provided on the second track. The first gate is connected to a fifth drive unit. When the third drive unit moves the reaction tank to the product collection area, the fifth drive unit drives the first gate to release the blockage of the discharge port. The product collection area includes a second collection chamber located below the second track and having a second inlet at the top.

12. The automated control system for coalbed methane decarbonization and hydrogen production according to any one of claims 9-11, characterized in that, The decarbonization hydrogen production unit includes a first cover plate at the inlet and a second cover plate at the outlet. When the reactor and the transfer mechanism are set up independently, the first cover plate blocks the inlet under a first force, and the second cover plate blocks the outlet under a second force. When the reactor is in the feeding state, the first cover plate releases the blockage of the inlet under a third force, and the second cover plate releases the blockage of the outlet under a fourth force.

13. The automated control system for coalbed methane decarbonization and hydrogen production according to any one of claims 9-11, characterized in that, The reactor further includes a preheating zone, a reaction zone, and a cooling zone arranged sequentially and connected along the feed direction. The temperature of the reaction zone is higher than the temperature of the preheating zone and the temperature of the cooling zone. The hydrogen outlet is connected to the preheating zone, and the natural gas inlet is connected to the inlet of the cooling zone.

14. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 13, characterized in that, The adjustment component includes: The deoxidizing component includes a first vent valve connected to the reactor, an external inert gas source connected to the inlet of the reactor, and a second valve located at the inlet. A temperature regulating element, which is connected to the reactor; And / or, the decarbonization hydrogen production unit further includes: The heat exchanger has a first inlet connected to the hydrogen outlet, a second inlet connected to the external coalbed natural gas source, a third outlet connected to the gas inlet, and a fourth outlet connected to a gas separation and purification device; the gas separation and purification device has a fifth outlet connected to the hydrogen storage tank and a sixth outlet connected to the external coalbed natural gas source.

15. A process for producing hydrogen from coalbed methane through decarbonization, characterized in that, include: Step S1: Expel the air from the reactor, inject a set amount of inert gas, and adjust the temperature in the reaction tank to a set value; Step S2: Add a set amount of catalyst to the reaction tank inside the reactor and evenly disperse the set amount of catalyst in the reaction tank; introduce natural gas into the reaction tank in the direction of the catalyst, and adjust the gas introduction area and release rate; Step S3: Periodically add catalyst to the reaction tank and output the product from the reaction tank; In step S2, before the natural gas enters the reaction tank, the natural gas first exchanges heat with the hydrogen discharged from the reaction tank. Then, the natural gas enters the low-temperature zone of the reactor for a second heat exchange before entering the reaction tank.

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