Coal seam natural gas decarburization hydrogen production production process and automatic control system

Abstract

The invention discloses a coal seam natural gas decarburization hydrogen production process and an automatic control system, and relates to the technical field of hydrogen preparation, a decarburization hydrogen production unit comprises: a reactor comprising a reaction zone, the reaction zone being internally provided with a reaction tank; a set amount of catalyst is added into the reaction tank through the feeding part, so that the hydrogen production efficiency of natural gas is improved; a plurality of natural gas inlets communicated with the reaction tank are formed in the reaction tank, so that the rate that natural gas enters the reaction tank and starts to contact and react with a catalyst is increased; a plurality of natural gas inlets are uniformly distributed on the reaction tank, so that the natural gas hydrogen production reaction can be fully catalyzed; the first valves are independently arranged, and the controller can change the adjusting parameters of the first valves, so that the catalyst in the reaction tank can efficiently and fully react with a proper amount of natural gas in unit time, and the hydrogen production efficiency of the natural gas is further improved.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen preparation, and in particular to a coal-bed natural gas decarbonization hydrogen production process and an automated control system. Background Art

[0002] Hydrogen can be produced by electrolysis of water, water gas method, synthesis gas and natural gas from petroleum thermal cracking, coal-bed natural gas, coke oven gas freezing, byproduct hydrogen from electrolysis of salt water, brewing industry byproduct, and iron and water vapor reaction. However, the efficiency of coal-bed natural gas hydrogen production in the prior art is relatively low.

[0003] Therefore, how to improve the hydrogen production efficiency of coal-bed natural gas hydrogen production reaction has become a technical problem that technical personnel in this field need to solve urgently. Summary of the invention

[0004] The purpose of the present invention is to provide a coal-bed natural gas decarbonization hydrogen production process and an automated control system to improve the hydrogen production efficiency of the coal-bed natural gas hydrogen production reaction.

[0005] To achieve the above object, the present invention provides the following solutions:

[0006] The present invention provides an automatic control system for decarbonization and hydrogen production of coal-bed natural gas, the automatic control system for decarbonization and hydrogen production of coal-bed natural gas comprises a plurality of groups of decarbonization and hydrogen production mechanisms, the decarbonization and hydrogen production mechanisms comprise the decarbonization and hydrogen production units;

[0007] The decarbonization hydrogen production unit comprises:

[0008] A reactor, wherein a reaction tank is provided in the reactor, a hydrogen outlet connected to the reaction tank is provided on the reactor, and a plurality of natural gas inlets are evenly distributed on the reaction tank, connected to the reaction tank, and arranged toward the catalyst in the reaction tank, wherein the natural gas inlet is connected to an external coal seam natural gas source, and a first valve for controlling the on-off of the natural gas inlet is provided at the natural gas inlet, and the first valves are arranged independently of each other;

[0009] A feed assembly, the feed assembly comprising a feed piece and a distribution piece, the feed piece is used to add a set amount of catalyst into the reaction tank, and the distribution piece is used to evenly distribute the catalyst in the reaction tank;

[0010] A regulating component, the regulating component is used to adjust the reaction conditions in the reaction tank;

[0011] A controller, the controller being respectively connected to the first valve and the regulating component by signals;

[0012] Wherein, before the decarbonization and hydrogen production unit is in working state, the controller controls the regulating component to adjust the reaction conditions of the reactor to set conditions, and the reaction conditions include temperature and oxygen concentration; when the decarbonization and hydrogen production unit is in the working state, the controller controls the regulating parameters of the first valve, and the regulating parameters include the opening timing, opening duration and opening size of the first valve.

[0013] In addition, the present invention also provides a coal-bed natural gas decarbonization hydrogen production process, comprising:

[0014] Step S1, exhausting the air in the reactor, injecting a set amount of inert gas, and adjusting the temperature in the reaction tank to a set value;

[0015] Step S2, adding a set amount of catalyst into the reaction tank in the reactor, and uniformly dispersing the set amount of catalyst into the reaction tank; introducing natural gas into the reaction tank in the direction of 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;

[0016] Step S3, regularly adding catalyst to the reaction tank and outputting the product in the reaction tank according to the state changes of the catalyst and the product in the reaction tank;

[0017] Among them, in step S2, before the natural gas enters the reaction tank, the natural gas first undergoes a heat exchange with the hydrogen discharged from the reaction tank, and then the natural gas enters the low temperature zone of the reactor for a secondary heat exchange, and then enters the reaction tank.

[0018] Compared with the prior art, the present invention has achieved the following technical effects:

[0019] The coal-bed natural gas decarbonization hydrogen production automation control system of the present invention comprises several groups of decarbonization hydrogen production units; the decarbonization hydrogen production units comprise: a reactor comprises a reaction zone, a reaction tank is arranged in the reaction zone, a hydrogen outlet connected to the reaction tank is arranged on the reaction zone, and several natural gas inlets are evenly distributed on the reaction tank, connected to the reaction tank and arranged toward the catalyst in the reaction tank, the natural gas outlet is connected to an external coal-bed natural gas source, a first valve is arranged at the natural gas inlet, and each first valve is independently arranged; a controller is respectively connected to the first valve and the regulating component by signal, the controller is used to control the regulating parameters of the first valve, the regulating parameters include the opening time, opening time and opening size of the first valve, and before the decarbonization hydrogen production unit works, the controller controls the regulating component to adjust the reaction conditions of the reactor to the set conditions, and the reaction conditions include temperature and oxygen concentration;

[0020] Based on the above structure, it should be noted that ① a reaction tank is provided in the reactor. 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 the catalyst, realizes the gathering of natural gas, and enables the natural gas to directly contact with 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 that natural gas is injected from the top of the reaction zone, and the natural gas can only move downward to contact the catalyst after filling the upper space of the reaction zone, thereby accelerating the rate at which the natural gas enters the reaction tank and starts to contact the catalyst;

[0021] ② In the present invention, a plurality of natural gas inlets are evenly distributed on the reaction tank, so that the natural gas entering the reaction tank from the natural gas inlet can 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;

[0022] ③ The first valves are independently arranged, and are all connected to the controller signal. The controller can change the adjustment parameters of the first valves, including the opening time, the opening timing and the opening size. This enables the present invention to gradually add the natural gas required for the reaction into the reaction tank, so that the catalyst in the reaction tank can react efficiently and fully with an appropriate amount of natural gas per unit time, thereby reducing the problem that due to the limited number of active sites of the catalyst in the reaction tank, too much natural gas is added to the reaction tank at one time, resulting in over-catalysis of the catalyst, excessive carbon deposits adsorbed on the catalyst, deactivation of the catalyst, and reduction of the hydrogen production efficiency of natural gas, thereby further improving the hydrogen production efficiency of natural gas in the present invention;

[0023] From the above content, it can be seen that the present invention effectively reduces the problem of insufficient contact between the catalyst and coalbed natural gas, and the problem of catalyst deactivation due to adsorption of carbon deposits, through the above structure, thereby significantly improving the hydrogen production efficiency of coalbed natural gas. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0025] Figure 1 This is a schematic diagram of the structure of the automatic control system for coal-bed natural gas decarbonization and hydrogen production;

[0026] Figure 2 It is a front view schematic diagram of the automatic control system for coal-bed natural gas decarbonization and hydrogen production;

[0027] Figure 3 The schematic diagram of the side of the automatic control system for coal-bed natural gas decarbonization and hydrogen production after omitting the side shell;

[0028] Figure 4 It is a schematic diagram of the structure of the transfer mechanism;

[0029] Figure 5 It is a longitudinal section of the transfer mechanism;

[0030] Figure 6 This is a top view of the automatic control system for coal-bed natural gas decarbonization and hydrogen production;

[0031] Figure 7 It is a schematic diagram of the structure of the feeding part and the cloth part;

[0032] Figure 8 It is a side view schematic diagram of a feeding piece and a cloth piece;

[0033] Fig. 9 It is a structural schematic diagram of the reaction tank;

[0034] Fig.10 is a schematic diagram of a longitudinal section of a reaction tank;

[0035] Among them, 1. reactor; 2. reaction tank; 3. hydrogen outlet; 4. observation window; 5. feeding piece; 6. material distribution piece; 7. silo; 8. dosing device; 9. unloading plate; 10. feeding port; 11. discharging port; 12. second track; 13. product collection area; 14. catalyst filling area; 15. first cover plate; 16. second cover plate; 17. first collection bin; 18. preheating area; 19. reaction area; 20. cooling area; 21. temperature regulation 1. Parts; 22. Heat exchanger; 23. External coal seam natural gas source; 24. Hydrogen storage tank; 25. Reaction tank replaces submarine cabin; 26. First valve; 27. Sealing cover; 28. Second drain valve; 29. ​​Gas replacement valve; 30. Second quantitative plate; 31. Air inlet; 32. Glove box; 33. Partition plate; 34. Fourth drive member; 35. Rotary drive equipment; 36. Hydrogen zone; 37. Nitrogen zone; 38. Dividing line; 39. Receiver box. DETAILED DESCRIPTION

[0036] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0037] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments.

[0038] like Figures 1 to 10 As shown, the present invention discloses an automatic control system for decarbonizing and hydrogenating natural gas from coal seam, which includes several groups of decarbonizing and hydrogenating mechanisms, and the decarbonizing and hydrogenating mechanisms include decarbonizing and hydrogenating units; the decarbonizing and hydrogenating units include: a reactor 1, wherein a reaction tank 2 is arranged in the reactor 1, and a hydrogen outlet 3 connected to the reaction tank 2 is arranged on the reactor 1, and several natural gas inlets are evenly distributed on the reaction tank 2, connected to the reaction tank 2, and arranged toward the catalyst in the reaction tank 2, the natural gas inlet is connected to an external coal seam natural gas source 23, and a first valve 26 for controlling the on-off of the natural gas inlet is arranged at the natural gas inlet, and each first valve 26 is independently arranged; a feed assembly, wherein the feed assembly includes a feeder 5 and a distributor 6, the feeder 5 is used to add a set amount of catalyst into the reaction tank 2, and the distributor 6 is used to evenly distribute the catalyst in the reaction tank 2;

[0039] The detection component of the present invention is used to detect the state of the catalyst in the reaction tank. The detection component includes a first detection component arranged at the hydrogen outlet and a second detection component arranged on the reaction tank. The first detection component can be a flow sensor and a concentration sensor. By detecting the hydrogen flow and concentration at the hydrogen outlet, comparing the natural gas intake, temperature, and reaction time, the algorithm is used to determine whether the catalyst is deactivated or there is a problem with the ratio of natural gas to hydrogen in the reactor, and then the natural gas supply or catalyst supply is adjusted accordingly. According to the specific type and function of the second detection component, the second detection component can be arranged in or on the reaction tank. The second detection component can be specifically an image sensor, a weight sensor, or an ultrasonic sensor. The second detection component needs to be made of a high-temperature resistant material, or a high-temperature resistant layer is provided on the surface to ensure that the second detection component can withstand high temperature without being damaged after entering the reactor with the reaction tank. The detection component also includes a third detection component. The third detection component is arranged outside the reactor, and can be specifically an infrared sensor or an acoustic sensor. The third detection component is arranged toward the reaction tank and can rotate with the movement of the reaction tank, thereby realizing remote detection of the catalyst state in the reaction tank. A regulating component, the regulating component is used to adjust the reaction conditions in the reaction tank 2; a controller, the controller is respectively connected to the first valve 26, the detection component, and the regulating component by signal; before the decarbonization and hydrogen production unit is in working condition, the controller controls the regulating component to adjust the reaction conditions of the reactor 1 to the set conditions, and the reaction conditions include temperature and oxygen concentration; when the decarbonization and hydrogen production unit is in working condition, the detection component is used to feed back the state of the catalyst in the reaction tank 2 to the controller, and the controller is used to control the regulating parameters of the first valve 26 according to the feedback of the detection component, and the regulating parameters include the opening time, opening duration and opening size of the first valve 26.

[0040] Based on the above structure, it should be noted that ① the present invention adds a set amount of catalyst into the reaction tank 2 through the feeding member 5, which alleviates the problem that the natural gas hydrogen production reaction cannot be fully catalyzed and the hydrogen production efficiency is too low due to too little catalyst addition, and also reduces the problem that the catalyst is excessively contacted or unevenly contacted with the natural gas due to excessive catalyst addition, making the reaction too violent, a large amount of carbon deposits adsorbed on the catalyst, causing the catalyst to be deactivated, and the natural gas hydrogen production efficiency is reduced; and the present invention distributes the catalyst evenly in the reaction tank 2 through the distribution member 6, which increases the catalytic surface area in the reaction zone 19 and the contact area between the natural gas and the catalyst, and reduces the problem that the carbon deposits produced by the natural gas are concentrated on the catalyst in the local area of ​​the reaction tank 2 due to the concentration of the catalyst, causing the catalyst to be deactivated and the natural gas hydrogen production efficiency to be reduced, thereby improving the natural gas hydrogen production efficiency;

[0041] ② A reaction tank 2 is provided in the reactor 1. Compared with the method in the prior art in which natural gas is directly introduced into the reaction zone 19, the reaction tank 2 reduces the reaction space between natural gas and the catalyst, realizes the gathering of natural gas, and enables the natural gas to directly contact with 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 the natural gas can only move downward to contact the catalyst after filling the upper space of the reaction zone 19, thereby accelerating the rate at which the natural gas enters the reaction tank 2 and starts to contact the catalyst;

[0042] ③ In the present invention, a plurality of natural gas inlets are evenly distributed on the reaction tank 2, so that the natural gas entering the reaction tank 2 from the natural gas inlet can 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;

[0043] ④ The first valves 26 are independently arranged, and a detection component for detecting the state of the catalyst is arranged in the reaction tank 2. The detection component and the first valve 26 are connected to the controller signal. The controller can change the adjustment parameters of the first valve 26 according to the change of the catalyst state fed back by the detection. The adjustment parameters include the opening time, the opening timing and the opening size. This enables the present invention to gradually add the natural gas required for the reaction into the reaction tank 2, so that the catalyst in the reaction tank 2 can react efficiently and fully with an appropriate amount (not too much, not too little) of natural gas per unit time, thereby reducing the problem that due to the limited number of active sites of the catalyst in the reaction tank 2, too much natural gas is added to the reaction tank 2 at one time, resulting in over-catalysis of the catalyst, excessive carbon deposits adsorbed on the catalyst, deactivation of the catalyst, and reduction of the hydrogen production efficiency of natural gas, thereby further improving the hydrogen production efficiency of natural gas in the present invention;

[0044] From the above content, it can be seen that the present invention effectively reduces the problem of insufficient contact between the catalyst and coalbed natural gas, and the problem of catalyst deactivation due to adsorption of carbon deposits, thereby significantly improving the hydrogen production efficiency of coalbed natural gas.

[0045] It should be noted that: except for the type of natural gas specifically specified in this article, the natural gas and coal-bed natural gas mentioned in this article all refer to coal-bed natural gas, but the coal-bed natural gas decarbonization hydrogen production process and automatic control system in the present invention can also be applied to natural gas, or other types of efficient hydrogen production with CH4 as the main component. The coal-bed natural gas decarbonization hydrogen production automatic control system in the present invention can be provided with a corresponding number of decarbonization hydrogen production mechanisms according to the working conditions, and each decarbonization hydrogen production mechanism can also be provided with a corresponding number of decarbonization hydrogen production units according to the working conditions. The automatic control in the coal-bed natural gas decarbonization hydrogen production process and automatic control system in the present invention refers to the ability to achieve at least the control of the reaction conditions of the reactor 1 and the adjustment parameters of the first valve 26 under the action of the controller. The reaction formula for hydrogen production from coal-bed natural gas in the present invention is CH4=C+2H2, and the process of natural gas generating carbon products and hydrogen is decarbonization and hydrogen production, respectively. C in the reaction formula can be a carbon product such as carbon nanotubes and carbon black according to different factors such as reaction temperature and catalyst; the catalyst can be a metal-based catalyst, such as a nickel-based catalyst, an iron-based catalyst or an aluminum-based catalyst.

[0046] The reaction tank 2 can be understood as being arranged in the reactor 1, with a volume smaller than the shell or box of the reactor 1, and the reaction tank 2 needs to have an inlet for feeding the catalyst. It can be a structure including a bottom plate and a side plate, such as a reaction tank 2 with a U-shaped or trapezoidal longitudinal section, which is equivalent to setting a reaction tank 2 including only a bottom plate in the reactor 1, further reducing the space for the natural gas hydrogen production reaction, and reducing the problem that the natural gas needs to wait for a certain time to diffuse after entering the reaction tank 2 before it can contact with the catalyst for reaction, so that the natural gas can directly contact with the catalyst after entering the reaction tank 2, and quickly start the natural gas hydrogen production reaction, thereby improving the natural gas hydrogen production efficiency.

[0047] Alternatively, the natural gas inlet may be arranged at the bottom of the reaction tank 2 and connected to the bottom of the reaction tank 2. Therefore, after the natural gas enters from the bottom of the reaction tank 2, it can contact with the catalyst for reaction, which accelerates the contact rate between the natural gas and the catalyst and the rate of hydrogen production from the natural gas. Moreover, since the density of natural gas is less than that of air, the natural gas inlet is toward the top of the reaction tank 2. This makes the natural gas move upward under the action of the nozzle and other structures and its own force after entering the reaction tank 2. In the prior art, natural gas is injected 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 a tendency to move upward. Moreover, since the natural gas and the catalyst react instantaneously, the hydrogen produced after the natural gas reaction rises, which will drive a part of the natural gas to move upward, resulting in a further reduction in the amount of natural gas actually reacting with the catalyst. That is, the method of injecting natural gas from the top of the reaction tank in the prior art cannot make the natural gas and the catalyst react fully, and the purity of hydrogen and the efficiency of hydrogen production are both low. In comparison, it is obvious that when the natural gas is arranged at the bottom of the reaction tank 2, the natural gas in the present invention has a greater upward force, which makes the natural gas contact with the catalyst faster to start the decarbonization and hydrogen production reaction.

[0048] Furthermore, the present invention is provided with a guide plate at each natural gas inlet at the bottom of the reaction tank 2, and the guide plate is inclined relative to the natural gas inlet, so that the force for sending the natural gas into the reaction tank 2 can be decomposed into a force along the guide plate direction and a force perpendicular to the guide plate direction under the action of the guide plate, thereby reducing the force driving the natural gas to rise, reducing the natural gas rising rate, allowing the natural gas to move horizontally along the reaction tank 2 and contact with more catalysts, increasing the contact area and reaction time between the natural gas and the catalyst, and further improving the natural gas hydrogen production efficiency in the present invention.

[0049] All guide plates in the reaction tank 2 are arranged in an inclined manner in the same direction. For example, all guide plates are arranged on the right side of the natural gas inlet, and the left end of the same guide plate is lower than the right end of the guide plate. This allows the natural gas to flow from left to right, and the natural gas can contact all catalysts on the bottom surface of the reaction tank 2. Alternatively, the guide plates on the left half of the reaction tank 2 can be arranged on the left side of the corresponding natural gas inlet, and the left end of the same guide plate is higher than the right end of the guide plate. The guide plates on the right half of the reaction tank 2 are arranged on the right side of the corresponding natural gas inlet, and the right end of the same guide plate is higher than the left end of the guide plate; this allows the natural gas on the left half of the reaction tank 2 to flow from right to left, and the natural gas on the right half of the reaction tank 2 to flow from left to right, which allows the natural gas to flow to the corners of the reaction tank 2, reducing the problem that the catalyst at the corners of the reaction tank 2 does not react with the natural gas due to the inability of the natural gas to reach the corners of the reaction tank 2, resulting in the problem of wasting the catalyst. In this paragraph, left can be understood as the side away from the feeding direction, and right can be understood as the side facing the feeding direction. The setting of the guide plate is not limited to the above-mentioned form, but the guide plate must meet the function of "reducing the rising rate of natural gas".

[0050] 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, and the first nozzle extends from bottom to top into the reaction tank 2, and a plurality of spray holes are provided along the circumference of the first nozzle. Thus, when natural gas is supplied into the reaction tank 2, the natural gas will be sprayed out from the spray holes, that is, the natural gas is supplied in a manner of diffusion around the first nozzle as the center, which is suitable for the "bean sprout-like growth" of carbon products. This makes the natural gas fill the bottom of the reaction tank first after entering the reaction tank 2 before gradually rising, which further reduces the rising rate of the natural gas, prolongs the contact time between the natural gas and the catalyst, and ensures that the natural gas hydrogen production reaction has a high hydrogen production efficiency. efficiency; and / or, when the natural gas inlet is located at the first side of the reaction tank 3, the natural gas inlet is provided with a second nozzle, the second nozzle is arranged toward the second side of the reaction tank 2, the first side and the second side are arranged opposite to each other, which realizes a step-by-step directional flow of gas from one side to the other side, and the second nozzle is arranged parallel to the bottom of the reaction tank 3, which is suitable for the "mushroom-like growth" of carbon products, which makes the natural gas entering the reaction tank 2 flow from one side of the reaction tank 2 to the other side, so that the natural gas can "cover" the reaction tank and then rise, which 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.

[0051] Alternatively, natural gas inlets may also be provided at the bottom, side, or even top of the reaction tank 2, and the natural gas inlets are all provided toward the catalyst. At this time, when the natural gas inlet is required to release natural gas into the reaction tank 2, the controller controls all the first valves 26 to be opened simultaneously, so that the natural gas released from multiple directions of the reaction tank 2 can all contact with the catalyst, thereby reducing the problem in the prior art that, because the natural gas is introduced from the top of the reaction tank 2, after the natural gas reacts with the catalyst to produce carbon products, carbon deposits will cover the surface of the catalyst, resulting in the active sites of the catalyst being covered, making it difficult for the subsequent natural gas to contact the catalyst, and the hydrogen production reaction of the natural gas is difficult to be fully catalyzed, resulting in low efficiency of hydrogen production from natural gas.

[0052] The external coalbed natural gas source 23 can specifically be a storage tank storing coalbed natural gas, which is connected to the natural gas inlet through a pipeline, or a coal seam storing coalbed natural gas. At this time, the coalbed natural gas mined from the coal seam can be transported to the natural gas inlet through a transmission pipeline; and the pipeline and the transmission pipeline are both provided with a pump that can input the natural gas into the reaction tank 2 through the natural gas inlet, as well as a valve that controls the pipeline or the transmission pipeline to be on and off.

[0053] The first valve 26 can be specifically an explosion-proof solenoid valve, or other valve that can control whether natural gas enters the natural gas inlet. The first valves 26 are independently arranged, which means that the controller can control a first valve 26 independently without affecting other first valves 26, thereby facilitating independent control of each valve in the reaction tank 2, and then the controller can supply different amounts of natural gas to different points and zones in the reaction tank 2 according to the state of the natural gas in the reaction tank 2 fed back by the detection component, thereby maintaining an efficient reaction rate of the natural gas and the catalyst.

[0054] Furthermore, in the case of being able to add a set amount of catalyst to the reaction tank 2, the feeder 5 has a variety of different presentation forms. Similarly, in the case of being able to evenly distribute the catalyst in the reaction tank 2, the distribution member 6 also has a variety of different types of structures. Figure 1 to Figure 3 , Figure 8 , Fig. 9 As shown, the feed assembly includes a silo 7 for storing catalyst, the silo 7 has a first outlet, and the feeding piece 5 has a second outlet; wherein the feeding piece 5 includes a dosator 8 connected to the silo 7, the dosator includes a first dosing plate and a second dosing plate 30 arranged up and down, the dosator 8 can rotate relative to the silo 7, during the rotation of the dosator 8 or the silo 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, so that by rotating the silo 7 or the dosator 8 a corresponding number of times, the feeding piece 5 can output a set amount of catalyst, that is, the amount required for the current reaction. For example, if the first outlet and the second outlet can only accommodate 10g of catalyst, the dosator 8 rotates one circle relative to the silo 7, and the silo 7 can release 10g of catalyst. The dosing device 8 rotates relative to the silo 7, which can be driven by a rotating drive structure such as a rotating motor to drive the dosing device 8 or the silo 7 to rotate. The dosing device 8 can be understood as a plate with a quantitative grid, i.e., a second outlet; and, the dosing device 8 rotates relative to the silo 7, i.e., the unloading function of the feeding piece 5 can be driven by an operator to manually operate the drive structure to drive the dosing device 8 or the silo 7 to rotate a corresponding number of circles, or the drive structure can be connected to the controller signal, and a displacement sensor such as an angle sensor can be set on the dosing device 8 or the silo 7 that is transmission-connected to the drive structure, and the displacement sensor can be connected to the controller signal. At this time, the controller can start the drive structure regularly according to the feeding instruction pre-entered by the operator, and drive the dosing device 8 to rotate a corresponding number of circles relative to the silo 7 through the drive structure to add a set amount of catalyst to the reaction tank 2.

[0055] The feeding member 5 may not adopt the structure of the doser 8. In this case, the feeding member 5 includes a weight sensor arranged on the silo 7, a baffle plate arranged at the first outlet, and a first driving member connected to the baffle plate and used to drive the baffle plate to block and open the first outlet; the weight sensor is connected to the display screen signal; at this time, the operator can control the opening time of the first outlet through the first driving member according to the change of the weight data of the catalyst in the silo 7 displayed on the display screen, and then add a set amount of catalyst to the reaction tank 2, or the weight sensor and the first driving member can be connected to the controller signal, and the operator inputs instructions into the controller, so that the controller adds the catalyst to the reaction tank 2 regularly and quantitatively according to the instructions. The baffle plate needs to be large enough to completely block the first outlet. According to the different movement modes 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. At the same time, another weight sensor can be set in the reaction tank 2. By comprehensively comparing the two readings of the weight sensor on the reaction tank 2 and the weight sensor on the silo 7, it is accurately known whether a set amount of catalyst is released and added in the reaction tank 2, thereby controlling whether the feeding piece 5 continues to add material to the reaction tank 2.

[0056] Furthermore, the above two forms of the feeding member 5 can also be combined with structures such as the doser 8, the weight sensor, and the baffle plate to realize the quantitative feeding function of the feeding member 5. In this way, even if there is an unexpected failure in the doser 8, the quantitative feeding function can be smoothly realized by delaying or closing the first outlet in advance; and it is necessary to pay attention to the avoidance setting of the doser 8 and the baffle plate so that their respective functions can be smoothly realized.

[0057] like Figure 8 and Fig. 9As shown, the material distribution member 6 includes a discharge plate 9 arranged on one side of the feeding member 5 close to the reaction tank 2. The discharge plate 9 is inclined relative to the dosing device 8 and is arranged toward the reaction tank 2. The second outlet is connected to the discharge plate 9, and the discharge plate 9 is connected to the driving device. The driving device is used to drive the discharge 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 discharge plate 9 to rotate, the discharge plate 9 needs to be located in a relatively central area on the reaction tank 2; when the driving device drives the discharge plate 9 to move along a certain direction of the reaction tank 2 (such as the length direction or the width direction), not only does the discharge plate 9 need to be located in the upper area of ​​the reaction tank 2, but the discharge plate 9 also needs to be able to move from one side of the reaction tank 2 to the opposite side; and no matter Whether the driving device drives the unloading plate 9 to rotate or drives the unloading plate 9 to move along the reaction tank 2, the unloading plate 9 must be able to receive the catalyst released by the feeding member 5 so that the catalyst can be evenly dispersed in the reaction tank 2; according to the movement type of the unloading plate 9, a rotary driving device 35 such as a rotary motor or a linear driving device such as an electric push rod can be selected; or, the driving device can be omitted, and the unloading plate 9 is connected to the quantitative device 8, and the quantitative device 8 is driven to rotate by the driving structure, and the unloading plate 9 is driven to rotate synchronously; and / or, the distribution member 6 includes a first vibrator provided on the feeding member 5 and / or the reaction tank 2, and the catalyst will not be blocked at the second outlet through the first vibrator provided on the reaction tank 2 and / or the feeding member 5, and can be more dispersed and evenly dropped in the reaction tank 2. The operating frequency, operating time and timing of the above-mentioned driving device and the first vibrator can be manually controlled by the operator, or the driving device, the first vibrator and the controller signal can be connected, and instructions are input to the controller, so that the controller automatically drives the driving device and / or the first vibrator to operate under the action of the instructions.

[0058] It should be noted that the second outlet of the feeder 5 does not mean that the feeder 5 is also provided with a first outlet. The second outlet is only for the convenience of distinguishing from the first outlet of the silo 7. The third outlet to the eighth outlet in the following text also have this meaning. The set amount of catalyst refers to the amount of catalyst that can meet the reaction requirements.

[0059] The reaction tank 2 in the present invention also has a variety of settings. The decarbonization hydrogen production unit includes a conveying assembly, which includes a first track arranged along the feed direction, the first track extends from the feed port 10 of the reactor 1 to the discharge port 11 of the reactor 1, and a plurality of reaction tanks 2 are arranged on the first track, and the reaction tank 2 is transmission-connected to the second driving member, and the driving member is used to drive the reaction tank 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, that is, the direction of movement of the reaction tank 2 in the reactor 1. The driving member can drive the reaction tank 2 to move along the feed direction on the first track until the catalyst in the reaction tank 2 completes the catalytic reaction of the corresponding amount of natural gas. According to the different settings and movement types of the reaction tank 2, the drive member can select a corresponding structure. For example, if the reaction tank 2 is slidably matched with the first track, the drive member can be a linear drive device such as a cylinder. At this time, the output shaft of the linear drive device needs to be long enough to push the reaction tank 2 from the feed port 10 to the discharge port 11. Alternatively, the first track can be filled with reaction tanks 2. At this time, when a reaction tank 2 in the reactor 1 completes 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. At this time, the linear drive device does not need to be additionally lengthened. The linear drive device is set toward 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 a pulley is provided at the bottom of the reaction tank 2, and the pulley is rollingly matched with the first track, the drive member can be a rotary motor such as a servo motor or other rotary drive device 35. At this time, the drive member can be provided on the reaction tank 2 so that the reaction tank 2 can run along the feeding direction of the first track.

[0060] like Figure 1 , Figure 2 , Figure 6 , Figure 7As shown, the decarbonization hydrogen production structure includes two decarbonization hydrogen production units arranged side by side and with opposite feeding directions; a transfer mechanism, the transfer mechanism is arranged near the feed port 10 of one of the reactors 1 and the discharge port 11 of the other reactor 1, the transfer mechanism includes a second track 12, the second track 12 is arranged from the feed port 10 of one of the reactors 1 to the discharge port 11 of the other reactor 1, and a product collection area 13 is provided on the path of the second track 12, and a third driving member is used to drive the reaction tank 2 to move along the second track 12; a detector group, the detector group includes a first detector arranged in the reaction tank 2, a second detector is arranged in the reaction tank 2, and / or the second detector is arranged on the second track 12, a second detector on the feed port 10 and the discharge port 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 moving position of the reaction tank 2; a discharge assembly, the discharge assembly is used to completely transfer the product in the reaction tank 2 to the product collection area 13; a transfer assembly, when the transfer mechanism is in working state, the transfer assembly transfers the reaction tank 2 located at the discharge port 11 of one of the reactors 1 to the second track 12, and the third driving member drives the reaction tank 2 on the second track 12 to move toward the feed port 10, and the transfer assembly transfers the reaction tank 2 that has been discharged in the product collection area 13 to the first track located at the feed port 10 of another reactor 1.

[0061] The distance between the feed port and the discharge port of the reactor is greater than the length of the first track in the direction from the discharge port of one reactor to the feed port of another reactor, which shortens the path of the reaction tank re-entering the reactor after outputting from the discharge port of the reactor, and shortens the interval time between the two reactions before and after the reactor.

[0062] When the conveying component of one of the decarbonization hydrogen production units pushes the product such as the carbon product received by the reaction tank 2 out of the reactor 1, the transfer component transfers the reaction tank 2 from the first track of the decarbonization hydrogen production unit to the second track 12, and the third driving component drives the reaction tank 2 to move on the second track 12 toward the feed port 10 of another decarbonization hydrogen production unit, and during the movement, the reaction tank 2 will pass through the product collection area 13, and the discharge component will completely transfer the product in the reaction tank 2 to the product collection area 13 to prevent the carbon deposits in the reaction tank 2 from being adsorbed on the surface of the subsequently filled catalyst, resulting in the deactivation of the catalyst and the reduction of the natural gas hydrogen production rate; after the discharge component completely transfers the product in the reaction tank 2 to the product collection area 13, the third driving component drives the reaction tank 2 to continue to move toward the feed port 10 of another decarbonization hydrogen production unit until it reaches the feed port 10 of another decarbonization hydrogen production unit, and then, the transfer component transfers the reaction tank 2 from the second track 12 to the first track of another decarbonization hydrogen production unit, and the second driving component of the other decarbonization hydrogen production unit drives the reaction tank 2 to move toward the reactor 1.

[0063] Obviously, the transfer mechanism realizes the cycle of feeding and discharging of two decarbonization hydrogen production units, that is, when a reactor 1 in a decarbonization hydrogen production unit outputs a reaction tank 2, after the reaction tank 2 is unloaded, it can move in the feeding direction of another decarbonization hydrogen production unit, and after filling the set amount of catalyst, continue to move in the feeding direction, so as to realize the feeding of another decarbonization unit. This alleviates the problem that only one decarbonization hydrogen production unit is set, and after the reaction tank 2 is discharged, the reaction tank 2 needs to be transferred from the discharge port 11 of the decarbonization hydrogen production unit to the feed port 10 of the decarbonization hydrogen production unit, resulting in intervals in the feeding of the decarbonization hydrogen production unit, discontinuous hydrogen production, and low hydrogen production efficiency, which accelerates the hydrogen production efficiency of the coalbed natural gas decarbonization hydrogen production automation control system in the present invention.

[0064] Among them, according to the feedback from the first detector, it is judged whether the carbon product in the reaction tank 2 is completely discharged, and according to the feedback from the second detector, it is judged 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 feed port 10 of one of the reactors 1, and whether it is located at the discharge port 11 of the other reactor 1. The first detector may be a weight sensor, an image sensor, an infrared sensor or the like which can detect the structure of the product residue in the reaction tank 2; there may be different settings according to the setting position of the second detector, for example, the second detector may be only set on the reaction tank 2, and a spatial coordinate system is prepared according to the automatic control system for decarbonization and hydrogen production of coal-bed natural gas in the present invention, and the position of the reaction tank 2 is judged according to the real-time position coordinates of the reaction tank 2 fed back by the second detector. At this time, the second detector may be a position sensor or an image sensor or the like which can reflect the position of the reaction tank 2; or, the second detector may be respectively set at the feed port 10 of one of the reactors 1, the discharge port 11 of another reactor 1, and the area corresponding to the product collection area 13 on the second track 12. At this time, the second detector may be a position sensor, an image sensor or a Hall sensor. When the second detector is a Hall sensor, the position of the reaction tank 2 is judged by the feedback of the Hall sensors at the three positions, namely, the feed port 10 of one of the reactors 1, the discharge port 11 of another reactor 1, and the area corresponding to the product collection area 13 on the second track 12.

[0065] The transfer component and the discharge component have various settings. For example, the transfer component includes: a receiving box 39, the receiving box 39 is movably arranged on the second track 12, and an inlet and outlet for the reaction tank 2 to enter and leave is provided on the side of the receiving box 39 facing the discharge port 11 of one of the reactors 1, the receiving box 39 has a cavity for accommodating the receiving box 39, and a limiter is provided in the cavity for limiting the reaction tank 2 from leaving the receiving box 39, and a push window with a longitudinal section smaller than the inlet and outlet is provided on the side of the receiving box 39 away from the discharge port 11, and a discharge port connected to the reaction tank 2 is provided on the top of the receiving box 39; the third driving member is connected to the receiving box 39 in a transmission manner, and is used to drive the receiving box 39 to move along the second track 12, when the receiving box 39 moves to the discharge port 11, the inlet and outlet are aligned with the reaction tank 2, and when the receiving box 39 moves to the feed port 10, The third driving member is aligned with the push window; the fourth driving member 34 is arranged close to and toward the feed port 10 of another reactor 1, and the fourth driving member 34 is located on the extension line of the first track; the reaction tank 2 is continuously distributed from one end of the first track close to the feed port 10 to one end of the first track close to the discharge port 11, and the distance between the discharge port 11 and the second track 12, and the distance between the feed port 10 and the second track 12 are both smaller than the length of the reaction tank 2 in the feeding direction; the discharge assembly includes a second track 12 in an annular shape and arranged perpendicular to the plane where the reactor 1 is located, and the discharge assembly includes a second vibrator arranged on the reaction tank 2 and / or the receiving box 39; the product collection area 13 includes a first collection bin 17 arranged below the second track 12 and having a first inlet at the top. The first vibrator and the second vibrator are structures in the prior art that can cause the structure equipped with the vibrator to vibrate up and down, or vibrate left and right, or swing around itself, and the specific structure of the vibrator will not be repeated here.

[0066] like Figure 4 As shown, the second track 12 is composed of two rows of parallel chains, which are supported by a plurality of supporting wheels to drive the rotation, and the supporting wheels are arranged on a rotating shaft, and the other end of the rotating shaft is connected to a rotating motor or other rotating driving device 35. The second track 12 is not limited to the above form, and can also be a structure such as a slide rail, a guide rail, etc. that can meet the above second track function.

[0067] When the second driving member pushes the reaction tank 2 that has completed the reaction out of the discharge port 11 of the reactor 1, the third driving member drives the receiving box 39 to move to the discharge port 11 of the reactor 1 (the position of the reaction tank 2 is 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, aligned with the reaction tank 2 located at the discharge port 11 of the reactor 1 at this time, and then the second driving member continues to move the reaction tank 2 toward the second track 12, so that the reaction tank 2 leaves the first track and enters the receiving box 39. The reaction tank 2 enters the receiving box 39 After that, the limiting member acts on the reaction tank 2, so that the reaction tank 2 will not separate from the receiving box 39 and will not fall out of the receiving box 39 when moving along the second track 12; then, the third driving member drives the reaction tank 2 to move on the second track 12 toward the feeding port 10 close to another reactor 1. Because the plane where the second track 12 is located is perpendicular to the plane where the reactor is located, the product collection area 13 is located below the second track 12, and the receiving box 39 is provided with a discharge port connected to the reaction tank 2. Therefore, when the reaction tank 2 moves to the product collection area 13, the discharge port will be set downward, that is, toward the first collection bin 17. The first inlet of the collecting bin 17 needs to be large enough so that the product in the reaction tank 2 will not leak to the outside when unloading, and the second vibrator is started synchronously so that the product in the reaction tank 2 can be completely discharged into the first collecting bin 17, and the first detector is used to judge whether the unloading of the reaction tank 2 is completed. If the first detector feedback shows that there is still material remaining in the reaction tank 2, the reaction tank 2 continues to unload in the product collecting area 13 until the product in the reaction tank 2 is completely discharged. After the unloading of the reaction tank 2 is completed, the third driving member drives the receiving box 39 on the second track 12 toward the feed port close to another reactor 1 The reaction tank 2 is pushed in the direction of 10 until it is judged that the reaction tank 2 reaches the position on the second track 12 corresponding to the feed port 10 of another reactor 1 according to the feedback from the second detector, the fourth driving member 34 is started, and the output shaft of the fourth driving member 34 extends in the feed direction, extends into the pushing window, contacts with the reaction tank 2 (at this time, the reaction tank 2 needs to have a side shell that can be pushed by the third driving member), and continues to push the reaction tank 2 in the feed direction until the reaction tank 2 is pushed onto the first track of another reactor 1, and then the reaction tank 2 is driven by the second driving member of the other reactor 1 to move along the feed direction.

[0068] In the present invention, the feeder is located near the feed inlet of the reactor. When the fourth driving member 34 pushes the reaction tank toward the feed inlet of the reactor, the feeder adds reactants such as catalysts to the reaction tank.

[0069] The discharge port may be specifically arranged at the top and / or the side of the receiving box 39 .

[0070] The stopper may be a magnet disposed in the cavity. In this case, the reaction tank 2 needs to be made of a magnetic material that can be adsorbed by a magnet; or, the stopper may be a stopper block disposed in the cavity, disposed on both sides of the feeding direction, with a spring or other reset member disposed between the stopper block and the cavity. A guide surface is disposed on the side of the stopper block close to the reactor 1, the guide surface is disposed obliquely relative to the cavity, a gap is disposed between the two guide surfaces, the gap on the side of the guide surface close to the reactor 1 is greater than the gap on the side of the guide surface away from the reactor 1, and the cross section of the gap between the two guide surfaces is Y-shaped. A pulley matching the second track 12 is disposed at the bottom of the reaction tank 2. In this case, the third driving member may be a rotary driving device 35 disposed on the reaction tank 2, connected to the pulley in transmission, and capable of driving the pulley to move on the second track 12, such as a servo motor; the fourth driving member 34 may be a linear driving device such as a cylinder or a hydraulic cylinder, and the fourth driving member 34 needs to be disposed away from the first track and the second track 12.

[0071] Alternatively, the transfer component may not adopt the structure described in the above paragraph. The transfer component includes a mechanical arm and a driving part. The driving part is connected to the mechanical arm in a transmission manner. The driving part is used to drive the mechanical arm to move from the feed port 10 to the direction close to the second track 12, and is used to drive the mechanical arm to move from the second track 12 to the direction close to the feed port 10. The mechanical arm includes a transmission part connected to the driving part. The transmission part can specifically be a joint or connecting rod structure connecting the driving part to the clamp, and a clamp provided at one end of the transmission part away from the driving part, and the clamp is used to clamp and release the reaction tank 2; the discharge component includes a first bin door, and a third vibrator on the reaction tank 2. The first bin door is provided at the discharge port at the bottom of the reaction tank 2, and a discharge port corresponding to the discharge port is provided on the second track 12. The first bin door is connected to the fifth driving member in a transmission manner. When the third driving member drives the reaction tank 2 to move to the product collection area 13, the fifth driving member drives the first bin door to release the blockage of the discharge port; the product collection area 13 includes a second collection bin located below the second track 12 and having a second entrance at the top. At this time, the second track 12 is a track arranged parallel to the plane where the reactor 1 is located.

[0072] According to the required degrees of freedom of the robot arm, the driving part includes driving structures arranged in multiple directions. The driving part needs to include a first driving structure that can drive the clamping and releasing of the clamping claw, a second driving structure that can drive the robot arm to move from the discharge port 11 of one of the reactors 1 along the second track 12, a third driving structure that drives the robot arm to move from the discharge port 11 of one of the reactors 1 toward the feed port 10 of another reactor 1, and a fourth driving structure that drives the robot arm to move from the second track 12 toward the feed port 10 of another reactor 1, and a fifth driving structure that can drive the robot arm to move in a vertical plane toward and away from the second track 12; the first to fifth driving structures can select linear driving devices such as cylinders, or rotary driving devices such as rotary motors 35 according to the movement type of the robot arm.

[0073] After the reaction tank 2 is output from the discharge port 11 of one of the reactors 1, the driving unit can drive the mechanical 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 bin door is driven to move by the fifth driving member, and then the blockage of the discharge port is released. The product in the reaction tank 2 enters the second collection bin through the discharge port, the discharge port, and the second entrance; after the discharge of the reaction tank 2 is completed, the driving unit drives the mechanical arm to move and transfer the reaction tank 2 to the first track of another reactor 1.

[0074] Alternatively, the discharge assembly may be omitted, and a driving structure capable of driving the reaction tank 2 to flip toward the product collection area 13 may be added to the driving part, so that the driving part can drive the reaction tank 2 to flip through a mechanical arm to achieve unloading.

[0075] According to different working conditions, the transfer mechanism can be manually operated by the operator; or, the detector group, transfer assembly, discharge assembly, third drive member, fourth drive member 34, fifth drive member and other structures in the transfer mechanism can be connected to the controller signal, and the operator manually inputs the operation instruction, so that the controller automatically controls the operation of the transfer mechanism according to the operation instruction. The feeder 5 can be arranged between the second track 12 and the feed port 10 of the reactor 1, so that the catalyst is filled before the reaction tank 2 enters the reactor 1.

[0076] It should also be noted that the structures of the detector group and the detection assembly of the present invention that enter the reactor 1 along with the reaction tank 2 are made of high-temperature resistant materials, or a high-temperature resistant layer is provided on the surface of the corresponding structures of the detector group and the detection assembly, so that the structures of the detector and the detection assembly that enter the reactor 1 along with the reaction tank 2 can withstand the high temperature of the natural gas reaction without being damaged or malfunctioning.

[0077] like Figure 1 , Figure 2 , Figure 6 , Figure 7As shown, a group of decarbonization hydrogen production machines includes two decarbonization hydrogen production units, and the feed port 10 of the reactor 1 constitutes a catalyst filling area 14, and the discharge port 11 constitutes a product collection area 13, and the catalyst filling area 14 near one of the reactors 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 arranged between the adjacent product collection area 13 and the catalyst filling area 14, the partition plate 33 and the second track 12 are arranged to avoid each other, the upper area of ​​the partition plate 33 is a hydrogen area 36, ​​and the lower area is a nitrogen area 37 or other inert gas area, there is a dividing line 38 between the hydrogen area 36 and the nitrogen area 37, and the two areas are divided by the density of the gas itself; the transfer mechanism also includes a shell arranged outside the second track 12 and the fourth driving member 34, and the shell is provided with a reaction tank replacement submarine cabin 25, a glove box 32, an observation window 4 and other structures. Before the decarbonization and hydrogen production is in working condition, the shell also needs to replace the internal air with inert gas to create an oxygen-free environment. Specifically, a vacuum valve can be set on the shell, and the shell is connected to the inert gas source through a pipeline. When emptying, the inert gas source and the pump and valve on the shell pipeline are opened to discharge the air through the inert gas. The gas sensor and other detection mechanisms set on the shell can be used to determine whether the air is exhausted.

[0078] The decarbonization hydrogen production unit also includes: a first cover plate 15 provided at the feed port 10 and a second cover plate 16 at the discharge port 11. When the reactor 1 and the transfer mechanism are independently arranged, the first cover plate 15 blocks the feed port 10 under a first force, and the second cover plate 16 blocks the discharge port 11 under a second force; the feed port 10 and the discharge port 11 are blocked by the first cover plate 15 and the second cover plate 16 respectively to maintain the gas phase environment in the reactor 1. When the reactor 1 is in a feeding state, the first cover plate 15 releases the blockage of the feed port 10 under a third force, and the second cover plate 16 releases the blockage of the discharge port 11 under a fourth force; the first cover plate 15 and the second cover plate 16 have various forms. For example, the first cover plate 15 is rotatably connected to the mounting plate provided at the discharge port 11, and the size of the first cover plate 15 is larger than the size of the feed port 10 so as to block the feed port 10; or, the size of the first cover plate 15 can be slightly smaller than the size of the feed port 10, and the first cover plate 15 is A corresponding sealing member is arranged between the plate 15 and the feed port 10 to keep the first cover plate 15 blocking the feed port 10. At this time, the first force may be the weight of the first cover plate 15 itself, or a torsion spring is arranged at the connection between the first cover plate 15 and the mounting plate, so that the first cover plate 15 blocks the feed port 10 under the combined action of its own weight and the torsion spring. At this time, the first cover plate 15 is transmission-connected to a rotating drive device 35 such as a rotating motor, and the first cover plate 15 is driven to rotate by the rotating drive device 35, thereby releasing the blocking of the feed port 10 by the first cover plate 15. The third force is the force of the rotating drive device 35 driving the first cover plate 15 to move away from the feed port 10. The second cover plate 16 is arranged in the same manner as the first cover plate 15. The second force may 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 rotating drive device 35 driving the second cover plate 16 to move away from the discharge port 11. The first cover plate 15 and the second cover plate 16 can be arranged outside the reactor 1 or inside the reactor 1, depending on the working conditions.

[0079] The regulating component includes: a deoxidation component, the deoxidation component includes a first drain valve connected to the reactor 1, an external inert gas source connected to the air inlet 31 of the reactor 1, the external inert gas source and the reactor 1 are connected by a pipeline, and a pump for conveying the inert gas and a second valve arranged at the air inlet 31 are arranged on the pipeline; before the reactor 1 starts to react, the second valve, the pump and the first drain valve are opened, and the air in the reactor 1 is exhausted by injecting inert gas into the reactor 1. The inert gas can be nitrogen or other gas that can suppress or reduce the risk of hydrogen explosion. The inert gas source refers to a storage tank storing inert gas, which can be arranged in the reactor 1 according to the inert gas storage tank. The oxygen sensor or gas analyzer on the reactor 1 determines whether the air is exhausted and whether an oxygen-free environment is formed; the temperature regulating member 21 is connected to the reactor 1, and the temperature regulating member 21 can be specifically an electric heating plate arranged on the reactor 1; the detection component includes a temperature sensor connected to the reactor 1, such as a thermocouple, etc., as well as a pressure sensor, a gas analyzer, an optical sensor, a camera, an ultrasonic sensor, an infrared sensor, etc., which can detect the state of the catalyst in the reaction tank 2. According to the working conditions and the functions of the structures in the detection component, the infrared sensor, the ultrasonic sensor and other detection structures can be selectively arranged in the reaction tank or outside the reactor.

[0080] According to the amount of catalyst added to the reaction tank 2 by the feeder 5, the change in the state of the catalyst in the reaction tank 2 fed back by the ultrasonic sensor, infrared sensor, camera and other structures in the detection assembly, and the concentration and volume of the natural gas in the reaction tank 2, the controller controls the opening time, opening size and other adjustment parameters 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 to the outside of the reaction tank 2), and then realizes the control of the amount of natural gas released into the reaction tank 2 to avoid the problem of excessive natural gas and excessive carbon deposition caused by the reaction of natural gas and catalyst. At the same time, by controlling the adjustment parameters of the first valve 26 by the controller, it is also possible to avoid the release of natural gas in a certain reaction. There is too much natural gas in the reaction tank 2, which causes the remaining natural gas to escape to the outside of the reaction tank 2 and into the space inside the reactor 1 after the natural gas reacts, and enters the subsequent reaction tank 2 from top to bottom, so that the natural gas is blocked by the carbon deposits before it fully contacts the catalyst, thereby reducing the efficiency of hydrogen production from natural gas; and, when natural gas is introduced into the reaction tank 2, the first vibrator on the reaction tank 2 is started, and / or the first vibrator on the reaction tank 2 is started based on the feedback of the carbon deposits in the reaction tank 2 by structures such as cameras, ultrasonic sensors, and infrared sensors, so as to reduce the coverage of the catalyst by carbon deposits, but it should be noted that the vibration amplitude of the first vibrator must not be too large to prevent accidents such as hydrogen explosions caused by excessive vibration amplitude.

[0081] like Figure 8 and Fig. 9As shown, a sealing cover 27, a second drain valve 28 and a gas replacement valve 29 are provided on the top of the silo 7. The gas replacement valve 29 is connected to the inert gas source. Before the reactor 1 reacts, the second drain valve 28 and the gas replacement valve 29 are opened (the second drain valve 28 and the gas replacement valve 29 are only valves that can control the on-off), and the inert gas enters the reactor 1 from the gas replacement valve to discharge the air.

[0082] like Figure 1 , Figure 2 , Figure 6 , Figure 7 As shown, the reactor 1 also includes a preheating zone 18, a reaction zone 19 and a cooling zone 20 which are arranged and connected in sequence along the feeding direction. The temperature of the reaction zone 19 is higher than the temperature of the preheating zone 18 and the temperature of the cooling zone 20. The feeding piece 5 is connected to the preheating zone 18, the hydrogen outlet 3 is connected to the preheating zone 18, the air inlet 31 is connected to the cooling zone 20, and the natural gas inlet is connected to the external natural gas source through the air inlet 31; the preheating zone 18 allows the catalyst to be gradually raised to a temperature suitable for the reaction; the cooling zone 20 is not actually cooled, but the temperature is lower than that of the reaction zone 19. The preheating zone 18, the reaction zone 19 and the cooling zone 20 are respectively connected with independent temperature adjustment parts 21 for heating, such as electric heating plates. The decarbonization hydrogen production unit also includes: a heat exchanger 22, the heat exchanger 22 has a first inlet connected to the hydrogen outlet 3, a second inlet connected to the external coal-bed natural gas source 23, a third outlet connected to the air inlet 31, and a fourth outlet connected to the gas separation and purification equipment; the gas separation and purification equipment has a fifth outlet connected to the hydrogen storage tank 24, and a sixth outlet connected to the external coal-bed natural gas source 23. Before the reaction, the natural gas is preheated for the first time in the heat exchanger 22 by reacting with hydrogen with a certain amount of waste heat, and preheated for the second time in the cooling zone 20, thereby realizing the cascade utilization of the energy of the reactor 1 and reducing the operating energy consumption. After the natural gas is stored in the hydrogen storage tank 24, it can be transported to the hydrogenation station for use.

[0083] When the reactor 1 includes the preheating zone 18, the reaction zone 19 and the cooling zone 20, an intermediate cavity which is not directly connected to the reaction tank 2 is further provided in the reactor 1, and the air inlet 31 is connected to the intermediate cavity. The intermediate cavity is distributed at least in the cooling zone 20, or can also be distributed in the entire reactor 1. The intermediate cavity is used to temporarily store natural gas and ensure that the natural gas can enter the reaction tank 2 from the natural gas inlet, and that the natural gas can exchange heat with the low-temperature zone in the reactor 1 before being released into the reaction tank 2, thereby realizing multi-stage utilization of energy in the reactor 1. A nozzle is provided on the middle cavity. When the controller detects, based on the feedback from the position sensor on the reaction tank 2, that the reaction tank 2 has reached the reaction zone 19 or other set reaction start position, 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, when the reaction tank 2 reaches the reaction start position, the nozzle is abutted against the natural gas inlet. A detection structure that can determine whether the nozzle is aligned with the natural gas inlet can be provided on the reaction tank, such as a camera or a Hall sensor, facing the natural gas inlet position. When the controller determines, based on the feedback from the detection structure and the position sensor, that the reaction tank 2 has reached the reaction start position, and that the nozzle is abutted against and aligned with the natural gas inlet of the reaction tank 2 that has reached the reaction position, the controller controls the first valve 26 and the nozzle to open. After the set amount of natural gas is released, the first valve 26 and the nozzle are closed to prevent the natural gas from escaping out of the reaction tank 2. When releasing natural gas into the reaction tank 2, if the opening and closing speeds of the first valve 26 and the nozzle and the natural gas release rate are fast, there is no need to stop the movement of the reaction tank 2 along the feeding direction; conversely, if the opening and closing speeds of the first valve 26 and the nozzle and the natural gas release rate are slow, the movement of the reaction tank 2 along the feeding direction can be appropriately slowed down or even stopped.

[0084] In addition, the present invention also provides a coal-bed natural gas decarbonization hydrogen production process, including step S1, exhausting the air in the reactor 1, injecting a set amount of inert gas, and adjusting the temperature in the reactor 1 to a set value; step S2, adding a set amount of catalyst to the reaction tank in the reactor 1, and evenly dispersing the set amount of catalyst in the reaction tank; introducing natural gas into the reaction tank 2 in the direction of 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, regularly adding catalyst to the reaction tank 2 according to the state change of the catalyst and the product in the reaction tank 2, and outputting the product in the reaction tank 2; wherein, in step S2, before the natural gas enters the reaction tank 2, the natural gas first exchanges heat with the hydrogen discharged from the reaction tank 2, and then the natural gas enters the low-temperature zone of the reactor 1, i.e., the cooling zone 20, for secondary heat exchange, and then enters the reaction tank.

[0085] In summary, the coal-bed natural gas decarbonization hydrogen production process and automatic control system in the present invention have the following significant advantages: ① Compared with the reactor in the prior art, the coal-bed natural gas decarbonization hydrogen production automatic control system in the present invention is a circulating dual-channel kiln reactor, which increases the single-time catalyst delivery ratio, broadens the natural gas cracking reaction area, and realizes the increase in hydrogen production capacity. The hierarchical arrangement of temperature adjustment parts can make a quick response according to the stage temperature difference in the reactor to prevent product defects. ② Coal-bed natural gas multi-channel gas supply device. The diversified graded and proportioned supply is adopted to adapt to the morphological changes of the catalyst during the reaction process, increase the surface area contact between natural gas and catalyst, avoid reaction attenuation, and increase the natural gas cracking reaction rate. ③ The reaction tank is optimized and the graded gas supply mode is adopted. Improve the catalyst utilization efficiency, prevent supersaturated adsorption, reduce the reaction time, and improve the product quality stability. Suitable for "bean sprout growth" catalysts. ④ Automated catalyst filling equipment, adopting a rotary quantitative supply mode. It comes with a cloth piece, cooperates with the reaction tank, and feeds synchronously. Improve the quantitative controllability of the catalyst and reduce the difficulty of production process operation. ⑤Transfer mechanism can realize high-efficiency reaction tank filling and by-product recovery, reduce the difficulty of production process operation, and save manpower and material resources.

[0086] The "and / or" mentioned in this article means that in the same sentence, the text content before and / or and the text content after and / or can exist at the same time or separately. For example, A and / or B includes three situations: only A or B exists, and A and B exist at the same time. And / or has the same meaning as and / or, which will not be repeated here.

[0087] The present invention discloses multiple technical solutions, but does not provide any contrary technical inspiration.

[0088] The present invention uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only used to help understand the method and core ideas of the present invention. At the same time, for those skilled in the art, according to the ideas of the present invention, there will be changes in the specific implementation methods and application scope. In summary, the content of this specification should not be understood as limiting the present invention.

Claims

1. An automatic control system for coal-bed natural gas decarbonization and hydrogen production, characterized in that: The coal-bed natural gas decarbonization hydrogen production automation control system includes a plurality of groups of decarbonization hydrogen production mechanisms, and the decarbonization hydrogen production mechanisms include decarbonization hydrogen production units; The decarbonization hydrogen production unit comprises: A reactor, wherein a reaction tank is provided in the reactor, a hydrogen outlet connected to the reaction tank is provided on the reactor, and a plurality of natural gas inlets are evenly distributed on the reaction tank, connected to the reaction tank, and arranged toward the catalyst in the reaction tank, wherein the natural gas inlet is connected to an external coal seam natural gas source, and a first valve for controlling the on-off of the natural gas inlet is provided at the natural gas inlet, and the first valves are arranged independently of each other; A regulating component, the regulating component is used to adjust the reaction conditions in the reaction tank; A controller, the controller being respectively connected to the first valve and the regulating component by signals; Wherein, before the decarbonization and hydrogen production unit is in working state, the controller controls the regulating component to adjust the reaction conditions of the reactor to set conditions, and the reaction conditions include temperature and oxygen concentration; when the decarbonization and hydrogen production unit is in the working state, the controller controls the regulating parameters of the first valve, and the regulating parameters include the opening timing, opening duration and opening size of the first valve.

2. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 1 is characterized in that: The natural gas inlet is arranged 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 coal-bed natural gas decarbonization hydrogen production automation control system according to claim 1 is characterized in that: The coal-bed natural gas decarbonization hydrogen production automatic control system also includes a detection component, which is used to detect the state of the catalyst in the reaction tank. The detection component includes a first detection component arranged at the hydrogen outlet and a second detection component arranged on the reaction tank.

4. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 1 is characterized in that: The natural gas inlet is also provided with a guide plate, and the guide plate and the reaction tank are arranged obliquely; And / or, the natural gas inlet is located at the bottom of the reaction tank, 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 opened along the circumference of the first nozzle; And / or, the natural gas inlet is located at the first side of the reaction tank, a second nozzle is provided at the natural gas inlet, the second nozzle is arranged toward the second side of the reaction tank, and the first side of the reaction tank and the second side of the reaction tank are arranged opposite to each other.

5. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 1 is characterized in that: The coal-bed natural gas decarbonization and hydrogen production automation control system also includes a feed assembly, which includes a silo for storing catalysts, a feeding piece for adding a set amount of catalyst into the reaction tank, and a distribution piece for evenly distributing the catalyst in the reaction tank, the silo has a first outlet, and the feeding piece has a second outlet.

6. The automatic control system for decarbonization of coal-bed natural gas to produce hydrogen according to claim 5, characterized in that: The feeding member includes a dosing device connected to the silo, the dosing device can rotate relative to the silo, during the rotation of the dosing device or the silo, 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 material distribution piece includes a discharge plate arranged on the side of the feeding piece close to the reaction tank, the discharge plate is inclined relative to the feeding piece and is arranged toward the reaction tank, the second outlet is connected to the discharge plate, the discharge plate is connected to the driving device, and the driving device is used to drive the discharge plate to rotate or move along the reaction tank.

7. The automatic control system for decarbonizing and hydrogen production from coal-bed natural gas according to claim 5 is characterized in that: The feeding member includes a weight sensor arranged on the silo, a baffle plate arranged at the first outlet, and a first driving member that is transmission-connected to the baffle plate and is used to drive the baffle plate to block and open the first outlet; and / or, the material distribution member includes a first vibrator arranged on the feeding member and / or the reaction tank.

8. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 1 is characterized in that: The decarbonization hydrogen production unit includes a conveying component, which includes a first track arranged along the feed direction, the first track extends from the feed port of the reactor to the discharge port of the reactor, and a plurality of reaction grooves are arranged on the first track, and the reaction grooves are transmission-connected to the second driving member, and the second driving member is used to drive the reaction grooves to move in the feed direction and enter and leave the reactor; the feed direction is the movement direction of the reaction grooves in the reactor.

9. The automatic control system for decarbonizing and hydrogen production from coal-bed natural gas according to claim 8, characterized in that: The decarbonization hydrogen production mechanism comprises: Two decarbonization hydrogen production units are arranged side by side and have opposite feeding directions; A transfer mechanism, wherein the transfer mechanism is disposed near the feed port of one of the reactors and the discharge port of another reactor; The transfer agencies include: a second track, the second track is arranged from the feed port of one of the reactors toward the discharge port of another reactor, and a product collection area is arranged on the path of the second track, a third driving member, the third driving member being used to drive the reaction tank to move along the second track; A discharge assembly, the discharge assembly is used to completely transfer the product in the reaction tank to the product collection area; The transfer component, when the transfer mechanism is in working state, the transfer component transfers the reaction tank at the discharge port of one of the reactors to the second track, the third driving member drives the reaction tank on the second track to move toward the feed port of another reactor, and the transfer component transfers the reaction tank that has completed discharge in the product collection area to the first track at the feed port of another reactor.

10. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 9, characterized in that: The transfer component comprises: A receiving box, the receiving box is movably arranged on the second track, an inlet and outlet for the reaction tank to enter and leave is provided on the side of the receiving box facing the discharge port of one of the reactors, a cavity for accommodating the reaction tank is provided in the receiving box, a push window with a longitudinal section smaller than the inlet and outlet is provided on the side of the receiving box away from the discharge port, and a discharge port connected to the reaction tank is provided on the receiving box; The third driving member is in transmission connection with the receiving box, and 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 member is aligned with the push window. a fourth driving member, the fourth driving member being arranged close to and facing the feed port of another reactor, and the fourth driving member being located on an extension line of the first track; The reaction grooves are continuously distributed from one end of the first track close to the feed port to one end of the first track close to the discharge port, and the distance between the discharge port and the second track, and the distance between the feed port and the second track are both smaller than the length of the reaction grooves in the feed direction; The discharge assembly includes a second track which is arranged perpendicularly to the plane where the reactor is located and is in a ring shape. The discharge assembly includes a second vibrator arranged on the reaction tank and / or the receiving box. The product collection area includes a first collection bin which is arranged below the second track and has a first inlet on the top.

11. The automatic control system for decarbonizing and hydrogen production from coal-bed natural gas according to claim 9, characterized in that: The transfer assembly includes a mechanical arm and a driving part, the driving part is connected to the mechanical arm in a transmission manner, the driving part is used to drive the mechanical arm to move from the feed port to the direction close to the second track, and is used to drive the mechanical arm to move from the second track to the direction close to the feed port, the mechanical arm includes a transmission part connected to the driving part, and a clamping claw provided at one end of the transmission part away from the driving part, the clamping claw is used to clamp and release the reaction tank; The discharge assembly includes a third vibrator disposed on the reaction tank, and a first bin door disposed at a discharge port at the bottom of the reaction tank, a discharge port corresponding to the discharge port is disposed on the second track, the first bin door is transmission-connected with a fifth driving member, and when the third driving member drives the reaction tank to move to the product collection area, the fifth driving member drives the first bin door to release the blockage of the discharge port; The product collection area includes a second collection bin located below the second track and having a second inlet at the top.

12. The automatic control system for decarbonizing and hydrogen production from coal-bed natural gas according to any one of claims 9 to 11, characterized in that: The decarbonization hydrogen production unit includes: a first cover plate arranged at the feed port and a second cover plate at the discharge port. When the reactor and the transfer mechanism are independently arranged, the first cover plate blocks the feed port under a first force, and the second cover plate blocks the discharge port under a second force; when the reactor is in a feeding state, the first cover plate releases the blockage of the feed port under a third force, and the second cover plate releases the blockage of the discharge port under a fourth force.

13. The automatic control system for decarbonizing and hydrogen production from coal-bed natural gas according to any one of claims 9 to 11, characterized in that: The reactor also includes a preheating zone, a reaction zone and a cooling zone which are sequentially arranged and connected along the feeding 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 gas inlet of the cooling zone.

14. The coal-bed natural gas decarbonization hydrogen production automation control system according to claim 13, characterized in that: The adjustment component comprises: A deoxidation component, the deoxidation component comprising a first drain valve connected to the reactor, an external inert gas source connected to the gas inlet of the reactor, and a second valve disposed at the gas inlet; A temperature regulating member connected to the reactor; And / or, the decarbonization hydrogen production unit further comprises: A heat exchanger having 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 air inlet, and a fourth outlet connected to a gas separation and purification device; the gas separation and purification device having a fifth outlet connected to a hydrogen storage tank, and a sixth outlet connected to the external coalbed natural gas source.

15. A coal-bed natural gas decarbonization hydrogen production process, characterized in that: include: Step S1, exhausting the air in the reactor, injecting a set amount of inert gas, and adjusting the temperature in the reaction tank to a set value; Step S2, adding a set amount of catalyst into the reaction tank in the reactor, and evenly dispersing the set amount of catalyst into the reaction tank; introducing natural gas into the reaction tank in the direction of the catalyst, and adjusting the introduction area and release amount of the natural gas; Step S3, regularly adding a catalyst into the reaction tank and outputting the product in the reaction tank; Among them, in step S2, before the natural gas enters the reaction tank, the natural gas first undergoes a heat exchange with the hydrogen discharged from the reaction tank, and then the natural gas enters the low temperature zone of the reactor for a secondary heat exchange, and then enters the reaction tank.

Images