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

Abstract

The present application discloses coal seam natural gas decarburization hydrogen production process and automation control system, relates to hydrogen production technical field, and decarburization hydrogen production unit includes: reactor including reaction zone, reaction zone is equipped with reaction tank; The present application adds the catalyst of setting amount to the reaction tank through the feeding part, improves the natural gas hydrogen production efficiency; A plurality of natural gas inlets which are communicated with the reaction tank are arranged on the reaction tank, and the rate that the natural gas enters the reaction tank and begins to contact and react with the catalyst is accelerated; The reaction tank is uniformly provided with a plurality of natural gas inlets, which makes the natural gas hydrogen production reaction can be fully catalyzed; The first valve is independently arranged between the first valve, and the controller can change the adjustment parameter of the first valve, which makes the catalyst in the reaction tank and the appropriate natural gas in the unit time carry out efficient and sufficient reaction, and the hydrogen production efficiency of natural gas in the present application is improved again.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen production, in particular to a coal seam natural gas decarburization hydrogen production process and an automatic control system. BACKGROUND

[0002] Hydrogen can be produced by electrolysis of water, water gas method, synthetic gas and natural gas from petroleum thermal cracking, coal seam natural gas, coke oven gas freezing, by-product hydrogen from electrolysis of salt water, brewing industry by-product, iron and steam reaction.

[0003] Therefore, how to improve the hydrogen production efficiency of the coal seam natural gas hydrogen production reaction has become a technical problem to be solved by those skilled in the art. SUMMARY

[0004] The present application provides a coal seam natural gas decarburization hydrogen production process and an automatic control system to improve the hydrogen production efficiency of the coal seam natural gas hydrogen production reaction.

[0005] To achieve the above-mentioned purpose, the present application provides the following solutions.

[0006] The present application provides a coal seam natural gas decarburization hydrogen production process and an automatic control system, which comprises a plurality of decarburization hydrogen production mechanisms, and each decarburization hydrogen production mechanism comprises a decarburization hydrogen production unit.

[0007] The decarburization hydrogen production unit comprises:

[0008] A reactor is provided with a reaction tank, a hydrogen outlet connected with the reaction tank, and a plurality of natural gas inlets connected with the reaction tank and arranged towards the catalyst in the reaction tank, wherein the natural gas inlets are connected with an external coal seam natural gas source, the natural gas inlets are provided with first valves for controlling the on-off of the natural gas inlets, and the first valves are independently arranged.

[0009] A feeding assembly is provided, which comprises a feeding member and a distributing member, wherein the feeding member is used for adding a certain amount of catalyst into the reaction tank, and the distributing member is used for distributing the catalyst in the reaction tank.

[0010] An adjusting assembly is provided for adjusting the reaction conditions in the reaction tank.

[0011] A controller is provided, which is signal connected with the first valves and the adjusting assembly.

[0012] Wherein, before the decarburization hydrogen production unit is in a working state, the controller controls the adjusting assembly to adjust the reaction condition of the reactor to a set condition, the reaction condition including temperature and oxygen concentration; when the decarburization hydrogen production unit is in the working state, the controller controls the adjusting parameter of the first valve, the adjusting parameter including the opening time, opening duration and opening degree of the first valve.

[0013] Furthermore, the application also provides a coal seam natural gas decarburization hydrogen production process, comprising:

[0014] Step S1, discharging 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 towards the catalyst, and adjusting the introduction area and release amount of the natural gas according to the state change of the catalyst in the reaction process;

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

[0017] In step S2, before the natural gas enters the reaction tank, the natural gas first exchanges heat with the hydrogen discharged from the reaction tank, then the natural gas enters the low-temperature zone of the reactor for secondary heat exchange, and then enters the reaction tank.

[0018] The application has the following technical effects compared with the prior art:

[0019] The coal seam natural gas decarburization hydrogen production automatic control system in the application comprises a plurality of decarburization hydrogen production units; the decarburization hydrogen production unit comprises: a reactor comprising a reaction zone, a reaction tank arranged in the reaction zone, a hydrogen outlet arranged on the reaction zone and in communication with the reaction tank, and a plurality of natural gas inlets arranged on the reaction tank and in communication with the reaction tank and towards the catalyst in the reaction tank, the hydrogen outlet being in communication with an external coal seam natural gas source, and the natural gas inlets being provided with first valves, the first valves being independently arranged between each other; a controller being in signal connection with the first valves and the adjusting assembly, the controller being used for controlling the adjusting parameter of the first valve, the adjusting parameter including the opening time, opening duration and opening degree of the first valve, and the controller being used for controlling the adjusting assembly to adjust the reaction condition of the reactor to a set condition before the decarburization hydrogen production unit works, the reaction condition including temperature and oxygen concentration.

[0020] Based on the above structure, it should be noted that ① the reactor is provided with a reaction tank, compared with the prior art of directly introducing natural gas into the reaction zone, the reaction tank reduces the reaction space of natural gas and catalyst, realizes the gathering of natural gas, and enables the natural gas entering the reaction tank from the natural gas inlet to directly contact with the catalyst and react with the catalyst, which reduces the problem that in the prior art, natural gas is injected from the top of the reaction zone, and after filling the upper space of the reaction zone, the natural gas can move downward to contact with the catalyst, thereby accelerating the rate of natural gas entering the reaction tank to contact with the catalyst to start the reaction;

[0021] ② In the present application, a plurality of natural gas inlets are uniformly distributed on the reaction tank, which enables the natural gas entering the reaction tank from the natural gas inlet to react with sufficient catalyst in the area where the natural gas inlet is located, so that the hydrogen production reaction of natural gas can be fully catalyzed, and the problem of low hydrogen production efficiency caused by excessive or insufficient amount of natural gas or catalyst participating in the reaction is reduced;

[0022] ③ The first valves are independently arranged between each other, and the first valves are signal connected with the controller, and the controller can change the adjustment parameters of the first valves, including opening time, opening opportunity and opening degree, which enables the present application to gradually add the required natural gas for reaction into the reaction tank, so that the catalyst in the reaction tank can efficiently and fully react with the appropriate amount of natural gas in unit time, and the problem of excessive catalyst caused by adding too much natural gas into the reaction tank at one time, which leads to excessive catalyst, excessive carbon deposition adsorbed on the catalyst, deactivation of the catalyst and reduction of hydrogen production efficiency of natural gas is reduced, thereby further improving the hydrogen production efficiency of natural gas in the present application;

[0023] From the above, the present application effectively reduces the problems of insufficient contact between catalyst and coalbed natural gas and deactivation of catalyst caused by carbon deposition, and further significantly improves the hydrogen production efficiency of coalbed natural gas. BRIEF DESCRIPTION OF DRAWINGS

[0024] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed in the embodiments will be briefly introduced as follows. Obviously, the drawings in the following description are only some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor.

[0025] Figure 1 is a structure diagram of the coalbed natural gas decarburization hydrogen production automatic control system;

[0026] Figure 2 is a front view schematic diagram of the coalbed natural gas decarburization hydrogen production automatic control system;

[0027] Figure 3 The side schematic view of the coal seam natural gas decarburization hydrogen production automatic control system after the side shell is removed;

[0028] Figure 4 The structural schematic view of the transfer mechanism;

[0029] Figure 5 The longitudinal sectional view of the transfer mechanism;

[0030] Figure 6 The top view of the coal seam natural gas decarburization hydrogen production automatic control system;

[0031] Figure 7 The structural schematic view of the feeding part and the distributing part;

[0032] Figure 8 The side schematic view of the feeding part and the distributing part;

[0033] Figure 9 The structural schematic view of the reaction tank;

[0034] Figure 10 The longitudinal sectional schematic view of the reaction tank;

[0035] Wherein, 1, the reactor; 2, the reaction tank; 3, the hydrogen outlet; 4, the observation window; 5, the feeding part; 6, the distributing part; 7, the stock bin; 8, the dosing device; 9, the discharging plate; 10, the feeding port; 11, the discharging port; 12, the second track; 13, the product collection area; 14, the catalyst filling area; 15, the first cover plate; 16, the second cover plate; 17, the first collection bin; 18, the preheating area; 19, the reaction area; 20, the cooling area; 21, the temperature adjusting part; 22, the heat exchanger; 23, the external coal seam natural gas source; 24, the hydrogen storage tank; 25, the reaction tank replacement submarine cabin; 26, the first valve; 27, the sealing cover; 28, the second evacuation valve; 29, the gas replacement valve; 30, the second dosing plate; 31, the gas inlet; 32, the glove box; 33, the partition plate; 34, the fourth driving part; 35, the rotary driving device; 36, the hydrogen area; 37, the nitrogen area; 38, the boundary line; 39, the receiving box. DETAILED DESCRIPTION

[0036] The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments of the present application. Based on the embodiments in the present application, all the other embodiments obtained by those skilled in the art without creative work fall within the scope of protection of the present application.

[0037] In order to make the above objectives, characteristics and advantages of the present application more apparent, further detailed description will be given below in conjunction with the drawings and specific embodiments.

[0038] As shown in Figures 1-10 The present application discloses a coal seam natural gas decarburization hydrogen production automatic control system, which comprises a plurality of decarburization hydrogen production mechanisms, and each decarburization hydrogen production mechanism comprises a decarburization hydrogen production unit.

[0039] The detection assembly is used for detecting the state of the catalyst in the reaction tank, and comprises a first detection member arranged at the hydrogen outlet and a second detection member arranged on the reaction tank. The second detection member can be arranged in or on the reaction tank, and can be an image sensor, a weight sensor or an ultrasonic sensor. The second detection member is made of a high-temperature-resistant material or has a high-temperature-resistant layer on the surface to ensure that the second detection member can withstand high temperature without being damaged after entering the reactor with the reaction tank. The detection assembly further comprises a third detection member arranged outside the reactor, which can be an infrared sensor or an acoustic sensor. The third detection member is arranged towards the reaction tank and can rotate with the movement of the reaction tank, thereby realizing remote detection of the state of the catalyst in the reaction tank. The controller is signal-connected with the first valve, the detection assembly and the adjusting assembly. Before the decarburization hydrogen production unit is in a working state, the controller controls the adjusting assembly to adjust the reaction conditions of the reactor 1 to the set conditions, and the reaction conditions include temperature and oxygen concentration. When the decarburization hydrogen production unit is in a working state, the detection assembly is used for feeding back the state of the catalyst in the reaction tank 2 to the controller, and the controller is used for controlling the adjusting parameters of the first valve 26 according to the feedback of the detection assembly. The adjusting parameters include the opening time, the opening time length and the opening degree of the first valve 26.

[0040] Based on the above structure, it is pointed out that ① the present application adds a certain amount of catalyst into the reaction tank 2 through the feeding member 5, which alleviates the problem that the hydrogen production reaction of natural gas cannot be fully catalyzed due to insufficient addition of catalyst, resulting in low hydrogen production efficiency, and also reduces the problem that excessive addition of catalyst leads to excessive or uneven contact between catalyst and natural gas, resulting in excessive reaction, a large amount of carbon deposition adsorbed on the catalyst, deactivation of the catalyst, and reduction of natural gas hydrogen production efficiency; and the present application uniformly distributes the catalyst in the reaction tank 2 through the distributing member 6, which increases the catalytic surface area in the reaction zone 19 and the contact area between natural gas and catalyst, reduces the problem that the catalyst is concentrated in a local area of the reaction tank 2, resulting in accumulation of carbon deposition produced by natural gas on the catalyst in this area, deactivation of the catalyst, and reduction of natural gas hydrogen production efficiency, and improves the natural gas hydrogen production efficiency;

[0041] ② The reactor 1 is provided with the reaction tank 2, compared with 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 catalyst, realizes the gathering of natural gas, and enables natural gas entering the reaction tank 2 from the natural gas inlet to directly contact with the catalyst and react with the catalyst, which reduces the problem in the prior art that natural gas is injected from the top of the reaction zone 19, and natural gas can only move downward to contact with the catalyst after filling the upper space of the reaction zone 19, thereby accelerating the rate of natural gas entering the reaction tank 2 and starting to contact with the catalyst;

[0042] ③ The reaction tank 2 in the present application is uniformly provided with a plurality of natural gas inlets, which enables the natural gas entering the reaction tank 2 from the natural gas inlets to react with sufficient catalyst in the area where the natural gas inlets are located, so that the hydrogen production reaction of natural gas can be fully catalyzed, and the problem of low hydrogen production efficiency caused by excessive or insufficient amount of natural gas or catalyst participating in the reaction is reduced;

[0043] ④ The first valves 26 are independently arranged between each other, the reaction tank 2 is provided with a detection assembly for detecting the state of the catalyst, the detection assembly and the first valves 26 are signal connected with the controller, the controller can change the adjustment parameters of the first valves 26 according to the change of the catalyst state fed back by the detection, the adjustment parameters include opening time, opening opportunity and opening degree, which enables the present application to gradually add the required natural gas into the reaction tank 2, so that the catalyst in the reaction tank 2 can efficiently and fully react with an appropriate amount (not too much or too little) of natural gas in unit time, and reduces the problem that the catalyst is deactivated and the natural gas hydrogen production efficiency is reduced due to excessive addition of natural gas into the reaction tank 2 at one time, resulting in excessive catalyst and excessive carbon deposition adsorbed on the catalyst, thereby further improving the hydrogen production efficiency of natural gas in the present application;

[0044] From the above, the present application effectively reduces the problems of insufficient contact of catalyst with coal seam natural gas and deactivation of catalyst by carbon deposition, and further significantly improves the hydrogen production efficiency of coal seam natural gas.

[0045] It should be noted that: in this paper, in addition to the type of natural gas specified, the natural gas mentioned in this paper refers to coal seam natural gas, but the coal seam natural gas decarburization hydrogen production process and automatic control system in the present application can also be applied to natural gas, or other types of efficient hydrogen production with CH4 as the main component. The coal seam natural gas decarburization hydrogen production automation control system in the present application can set the corresponding number of decarburization hydrogen production mechanisms according to the working conditions, and each decarburization hydrogen production mechanism can also set the corresponding number of decarburization hydrogen production units according to the working conditions. The automation control in the coal seam natural gas decarburization hydrogen production process and automation control system in the present application refers to being able to control at least 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 of coal seam natural gas hydrogen production in the present application is CH4=C+2H2, and the process of natural gas generating carbon products and hydrogen is decarburization and hydrogen production, respectively. In the reaction formula, C can be carbon nanotubes, carbon black and other carbon products according to different reaction temperatures and catalysts and other factors; 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, having a volume smaller than the shell or box of the reactor 1, and the reaction tank 2 needs to have a feeding port for feeding catalyst. It can be a structure including a bottom plate and a side plate, such as a reaction tank 2 with a longitudinal section in the shape of U or trapezoid, which is equivalent to arranging a reaction tank 2 including only a bottom plate in the reactor 1, further reducing the space for natural gas hydrogen production reaction, reducing the problem that natural gas needs to wait for a certain time to diffuse after entering the reaction tank 2 before contacting the catalyst for reaction, so that the natural gas can directly contact the catalyst after entering the reaction tank 2, and quickly start the natural gas hydrogen production reaction, thereby improving the hydrogen production efficiency of natural gas.

[0047] Alternatively, only the natural gas inlet can be arranged at the bottom of the reaction tank 2 and communicated with the bottom of the reaction tank 2, so that the natural gas can contact the catalyst for reaction after entering the bottom of the reaction tank 2, thereby accelerating the contact rate of the natural gas and the catalyst and the hydrogen production rate of the natural gas. In addition, because the density of the natural gas is less than that of the air, the natural gas inlet is directed to the top of the reaction tank 2, which makes the natural gas move upward under the action of the nozzle structure and its own force after entering the reaction tank 2. In the prior art, the natural gas is injected from the top of the reaction tank 2, and because the density of the natural gas is less than that of the air, it means that the natural gas has a tendency to move upward. Because the natural gas and the catalyst are instantaneously reacted, the hydrogen produced after the reaction of the natural gas rises and drives a part of the natural gas to move upward, which further reduces the amount of natural gas actually reacted with the catalyst, that is, the natural gas injection mode from the top of the reaction tank 2 in the prior art cannot make the natural gas and the catalyst fully react, and the hydrogen purity and hydrogen production efficiency are low. In contrast, when the natural gas is arranged at the bottom of the reaction tank 2, the natural gas has a greater upward movement force in the present application, which makes the natural gas contact the catalyst more quickly to start the decarburization and hydrogen production reaction.

[0048] Furthermore, the present application is provided with a guide plate at each natural gas inlet at the bottom of the reaction tank 2, and the guide plate is arranged obliquely relative to the natural gas inlet, which makes the force for sending the natural gas into the reaction tank 2 decomposed into a force along the direction of the guide plate and a force perpendicular to the direction of the guide plate, thereby reducing the force driving the natural gas to rise, reducing the rising rate of the natural gas, and making the natural gas move horizontally along the reaction tank 2 to contact more catalysts, increasing the contact area and reaction time of the natural gas and the catalyst, and further improving the hydrogen production efficiency of the natural gas in the present application.

[0049] All the guide plates in the reaction tank 2 are arranged obliquely in the same direction, for example, all the 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, which makes the natural gas flow from left to right, and the natural gas can contact all the catalysts on the bottom surface of the reaction tank 2. Alternatively, the guide plates on the left half side 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 side 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 makes the natural gas on the left half side of the reaction tank 2 flow from right to left, and the natural gas on the right half side of the reaction tank 2 flow from left to right, which makes the natural gas flow to the corners of the reaction tank 2, reducing the problem that the catalyst at the corners of the reaction tank 2 is not reacted with the natural gas due to the inability of the natural gas to reach the corners of the reaction tank 2, thereby 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 towards the feeding direction. The arrangement of the guide plate is not limited to the above form, but the guide plate needs to meet the function of "reducing the rising rate of the natural gas".

[0050] And, when the natural gas inlet is located at the bottom of the reaction tank 2, the natural gas inlet is provided with a first nozzle extending into the reaction tank 2 from bottom to top, and a plurality of spray holes are arranged along the circumference of the first nozzle, so that when the natural gas is supplied into the reaction tank 2, the natural gas is sprayed from the spray holes, that is, the natural gas is supplied in a way of spreading around the first nozzle, which is suitable for the “sprout growth” of the carbon product, which makes the natural gas fill the bottom of the reaction tank 2 first and then gradually rise, which further reduces the rising rate of the natural gas, prolongs the contact time of the natural gas and the catalyst, and ensures that the natural gas hydrogen production reaction has a high hydrogen production 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 towards the second side of the reaction tank 2, and the first side and the second side are oppositely arranged, which realizes the stepwise directional flow of the gas from one side to the other side, and the second nozzle is arranged in parallel relative to the bottom of the reaction tank 3, which is suitable for the “mushroom growth” of the carbon product, which makes the natural gas entering the reaction tank 2 flow from one side to the other side of the reaction tank 2, so that the natural gas can “cover” the reaction tank, and then rise, which obviously prolongs the contact time of the natural gas and the catalyst, and ensures that the natural gas hydrogen production reaction has a high hydrogen production efficiency.

[0051] Alternatively, the natural gas inlets can also be arranged at the bottom, side, and even top of the reaction tank 2, and the natural gas inlets are all arranged towards the catalyst, at this time, when the natural gas inlets need to release natural gas into the reaction tank 2, the controller controls all the first valves 26 to be opened at the same time, which makes the natural gas released from multiple directions of the reaction tank 2 all contact with the catalyst, which reduces the problem in the prior art that when the natural gas is introduced from the top of the reaction tank 2, the carbon product produced by the reaction of the natural gas and the catalyst covers the surface of the catalyst, which causes the active sites of the catalyst to be covered, and the subsequent natural gas is difficult to contact with the catalyst, the hydrogen production reaction of the natural gas is difficult to be fully catalyzed, and the hydrogen production efficiency of the natural gas is low.

[0052] The external coalbed natural gas source 23 can be a storage tank storing coalbed natural gas, the storage tank is connected in communication with the natural gas inlet through a pipeline, or a coalbed storing coalbed natural gas, at this time, the coalbed natural gas mined from the coalbed can be transported to the natural gas inlet through a conveying pipeline; and the pipeline and the conveying pipeline are both provided with a pump capable of inputting the natural gas into the reaction tank 2 through the natural gas inlet, and a valve controlling the opening and closing of the pipeline or the conveying pipeline.

[0053] The first valve 26 can be an explosion-proof electromagnetic valve, which can control whether the natural gas inlet enters the natural gas. The first valve 26 is independently arranged, which means that the controller can control a certain first valve 26 without affecting other first valves 26, thereby facilitating independent control of each valve in the reaction tank 2, and then enabling the controller to supply different amounts of natural gas in 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 assembly, thereby maintaining the efficient reaction rate of the natural gas and the catalyst.

[0054] Furthermore, the feeding member 5 has various different forms to meet the requirement of adding a set amount of catalyst into the reaction tank 2, and the distributing member 6 also has various different structures to meet the requirement of uniformly distributing the catalyst in the reaction tank 2. Figures 1-3 , Figure 8 、 Figure 9 As shown in the drawings, the feeding assembly includes a bin 7 for storing the catalyst, the bin 7 has a first outlet, and the feeding member 5 has a second outlet; wherein the feeding member 5 includes a dosing device 8 connected to the bin 7, the dosing device 8 includes a first dosing plate and a second dosing plate 30 arranged in a vertical manner, and the dosing device 8 can rotate relative to the bin 7, and the first outlet and the second outlet are intermittently connected during the rotation of the dosing device 8 or the bin 7, and the first outlet and the second outlet can accommodate the same set amount of catalyst, so that the feeding member 5 can output the set amount of catalyst required for the current reaction by rotating the bin 7 or the dosing device 8 by a corresponding number of turns, for example, if the first outlet and the second outlet can only accommodate 10 g of catalyst, the dosing device 8 can be rotated relative to the bin 7 by one turn, and the bin 7 can release 10 g of catalyst. The rotation of the dosing device 8 relative to the bin 7 can be driven by a rotating drive structure such as a rotating motor, the dosing device 8 can be understood as a plate provided with a dosing hole grid, and the rotation of the dosing device 8 relative to the bin 7, i.e. the discharging function of the feeding member 5, can be achieved by manually operating the drive structure to rotate the dosing device 8 or the bin 7 by a corresponding number of turns, or the drive structure can be connected to the controller, and a displacement sensor such as an angle sensor can be arranged on the dosing device 8 or the bin 7 in transmission connection with the drive structure, and the displacement sensor can be connected to the controller, at this time, the controller can periodically start the drive structure according to the feeding instruction input by the operator in advance, and rotate the dosing device 8 relative to the bin 7 by a corresponding number of turns through the drive structure, thereby adding a set amount of catalyst into the reaction tank 2.

[0055] The feeding device 5 can also not adopt the structure of the dosing device 8, in which case, the feeding device 5 comprises a weight sensor arranged on the bin 7, a baffle arranged at the first outlet, and a first driving member in driving connection with the baffle and used to drive the baffle to close and open the first outlet; the weight sensor is in signal connection with the display screen; in this case, the operator can control the time of opening the first outlet through the first driving member according to the weight data change of the catalyst in the bin 7 displayed on the display screen, and then add a set amount of catalyst into the reaction tank 2, or the weight sensor, the first driving member and the controller can be in signal connection, and the operator can input an instruction into the controller, so that the controller can add the catalyst into the reaction tank 2 regularly and quantitatively according to the instruction. The baffle needs to be large enough to completely close the first outlet, and according to the different movement modes of the baffle, a linear driving device such as a cylinder or a rotary driving device 35 such as a rotary motor can be selected. At the same time, another weight sensor can also be arranged in the reaction tank 2, and the two indications of the weight sensor on the reaction tank 2 and the weight sensor on the bin 7 are comprehensively compared, so as to accurately know that the set amount of catalyst is released into the reaction tank 2, and then whether the feeding device 5 continues to feed the catalyst into the reaction tank 2 is controlled.

[0056] In addition, the above two forms of the feeding device 5 can be combined to realize the quantitative feeding function of the feeding device 5 by combining the structures of the dosing device 8, the weight sensor and the baffle. In this way, even if the dosing device 8 has an unexpected failure, the first outlet can be closed in advance or delayed to ensure that the quantitative feeding function can be smoothly realized. It should be noted that the dosing device 8 and the baffle are arranged to avoid each other so that their respective functions can be smoothly realized.

[0057] As Figure 8 and Figure 9As shown, the distributing member 6 comprises a discharging plate 9 arranged on the feeding member 5 close to the reaction tank 2. The discharging plate 9 is arranged obliquely relative to the dosing device 8 and towards the reaction tank 2. The second outlet is in communication with the discharging plate 9. The discharging plate 9 is in driving connection with a driving device. The driving device is used to drive the discharging plate 9 to rotate or move along the reaction tank 2, so that the catalyst is uniformly dispersed into the reaction tank 2. In order to realize this function, when the driving device drives the discharging plate 9 to rotate, the discharging plate 9 needs to be located in a relatively central region of the reaction tank 2. When the driving device drives the discharging plate 9 to move in a certain direction (such as the length direction or the width direction) along the reaction tank 2, the discharging plate 9 not only needs to be located above the reaction tank 2, but also needs to be able to move from one side of the reaction tank 2 to the opposite side. In addition, no matter whether the driving device drives the discharging plate 9 to rotate or drives the discharging plate 9 to move along the reaction tank 2, the discharging plate 9 needs to be able to receive the catalyst released by the feeding member 5, so that the catalyst can be uniformly dispersed into the reaction tank 2. According to the movement type of the discharging 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. Alternatively, the driving device can be omitted. The discharging plate 9 is connected with the dosing device 8. By driving the dosing device 8 to rotate, the discharging plate 9 is also driven to rotate synchronously. In addition, the distributing member 6 comprises a first vibrator arranged on the feeding member 5 and / or the reaction tank 2. By arranging the first vibrator on the reaction tank 2 and / or the feeding member 5, the catalyst will not be blocked at the second outlet, and can be more dispersed and uniformly dropped into the reaction tank 2. The operating frequency and operating time of the above-mentioned driving device and the first vibrator, as well as the timing, can be manually controlled by the operator. Alternatively, the driving device and the first vibrator can be connected with the controller in signal, and the controller is inputted with instructions, 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 feeding member 5 does not mean that the feeding member 5 is also provided with a first outlet. The second outlet is only used to distinguish the first outlet of the hopper 7. The third outlet to the eighth outlet in the following are also for this purpose. The set amount of catalyst refers to the catalyst that can meet the reaction requirement.

[0059] The reaction tank 2 in the application also has various setting forms. The de-carbonization hydrogen production unit comprises a conveying assembly, the conveying assembly comprises a first track arranged along a feeding direction, the first track extends from the feeding port 10 of the reactor 1 to the discharging port 11 of the reactor 1, and a plurality of reaction tanks 2 are arranged on the first track, the reaction tank 2 is in transmission connection with a second driving member, the driving member is used for driving the reaction tank 2 to move towards the feeding direction and to enter and leave the reactor 1. The feeding direction refers to the direction in which the catalyst moves with the reaction tank 2 after a certain amount of catalyst is added into the reaction tank 2, that is, the movement direction of the reaction tank 2 in the reactor 1. The driving member can drive the reaction tank 2 to move along the feeding direction on the first track until the catalyst in the reaction tank 2 completes the catalytic reaction on the corresponding amount of natural gas. According to the setting mode and the movement type of the reaction tank 2, the driving member can be selected to have a corresponding structure. For example, if the reaction tank 2 is in sliding connection with the first track, the driving member can be a linear driving device such as a cylinder, at this time, the output shaft of the linear driving device needs to be long enough to push the reaction tank 2 out of the discharging port 11 from the feeding port 10, or the reaction tank 2 can be arranged on the first track, at this time, when the 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 driving device does not need to be additionally lengthened, the linear driving device is arranged towards the feeding port 10, after the linear driving device pushes the reaction tank 2 filled with catalyst into the reactor 1, the reaction tank 2 that completes the reaction is automatically output from the reactor 1 under the pushing of the subsequent reaction tank 2; if the reaction tank 2 is provided with a pulley at the bottom, the pulley is in rolling connection with the first track, and the driving member can be a rotary driving device 35 such as a servo motor, at this time, the driving member can be arranged on the reaction tank 2, so that the reaction tank 2 can run along the feeding direction on the first track.

[0060] As Figure 1 , Figure 2 , Figure 6 , Figure 7As shown, the decarburization hydrogen production structure comprises two decarburization hydrogen production units arranged side by side and in opposite directions; a transfer mechanism, which is arranged close to the feed inlet 10 of one of the reactors 1 and the discharge outlet 11 of the other reactor 1, and comprises a second track 12 arranged from the feed inlet 10 of one of the reactors 1 towards the discharge outlet 11 of the other reactor 1, a product collection area 13 arranged on the path of the second track 12, a third driving member for driving the reaction tank 2 to move along the second track 12; a detector group, which comprises a first detector arranged in the reaction tank 2, a second detector arranged in the reaction tank 2 and / or a second detector arranged on the second track 12, the feed inlet 10 and the discharge outlet 11, the first detector being used for detecting the product retention state in the reaction tank 2, and the second detector being used for detecting the moving position of the reaction tank 2; a discharge assembly for completely transferring the product in the reaction tank 2 to the product collection area 13; a transfer assembly, which transfers the reaction tank 2 at the discharge outlet 11 of one of the reactors 1 to the second track 12 when the transfer mechanism is in a working state, drives the reaction tank 2 on the second track 12 to move towards the feed inlet 10, and transfers the reaction tank 2, which has finished discharging in the product collection area 13, to the first track at the feed inlet 10 of the other reactor 1.

[0061] The distance between the feed inlet and the discharge outlet of the reactor is greater than the length of the first track in the direction from the discharge outlet of one of the reactors to the feed inlet of the other reactor, which shortens the path of the reaction tank from the discharge outlet of the reactor to the feed inlet of the reactor, and shortens the interval time between the two reactions of the reactor.

[0062] When the conveying assembly of one of the decarburization hydrogen production units pushes the product, such as carbon product, received by the reaction tank 2 out of the reactor 1, the transfer assembly transfers the reaction tank 2 from the first track of the decarburization hydrogen production unit to the second track 12, and drives the reaction tank 2 to move on the second track 12 towards the feed inlet 10 of the other decarburization hydrogen production unit by the third driving member, and in the moving process, the reaction tank 2 will pass through the product collection area 13, and the discharge assembly completely transfers the product in the reaction tank 2 to the product collection area 13, so as to prevent the accumulated carbon in the reaction tank 2 from being adsorbed on the surface of the subsequently filled catalyst, causing the catalyst to be deactivated and the hydrogen production rate of natural gas to be reduced; after the discharge assembly completely transfers the product in the reaction tank 2 to the product collection area 13, the third driving member drives the reaction tank 2 to continue moving towards the feed inlet 10 of the other decarburization hydrogen production unit until the reaction tank 2 reaches the feed inlet 10 of the other decarburization hydrogen production unit, and then the transfer assembly transfers the reaction tank 2 from the second track 12 to the first track of the other decarburization hydrogen production unit, and the second driving member of the other decarburization hydrogen production unit drives the reaction tank 2 to move towards the reactor 1.

[0063] Obviously, the transfer mechanism realizes the circulation of feeding and discharging of two decarburization hydrogen production units, that is, when a reaction tank 2 is output from a reactor 1 of one decarburization hydrogen production unit, the reaction tank 2 can be moved towards the feeding direction of another decarburization hydrogen production unit after the reaction tank 2 is completely discharged, and then the reaction tank 2 continues to move towards the feeding direction after being filled with a set amount of catalyst, so as to realize the feeding of another decarburization unit. This alleviates the problem that when only one decarburization hydrogen production unit is provided, after the reaction tank 2 is discharged, the reaction tank 2 needs to be transferred from the discharge port 11 of the decarburization hydrogen production unit to the feeding port 10 of the decarburization hydrogen production unit, resulting in an interval in the feeding of the decarburization hydrogen production unit, discontinuous production of hydrogen, and low hydrogen production efficiency. The coal seam natural gas decarburization hydrogen production automation control system of the present application is accelerated to increase the hydrogen production efficiency.

[0064] In the present application, the first detector can be a weight sensor, an image sensor, an infrared sensor or other structure capable of detecting the residual product in the reaction tank 2, and the second detector can be a position sensor or an image sensor, and the second detector can also be a Hall sensor. The second detector can be arranged on the reaction tank 2, and the real-time position coordinates of the reaction tank 2 can be obtained through the feedback of the second detector, so as to determine the position of the reaction tank 2. Alternatively, the second detector can also be arranged on the feeding port 10 of one reactor 1, the discharge port 11 of the other reactor 1, and the region corresponding to the product collection area 13 on the second track 12, and the position of the reaction tank 2 can be determined through the feedback of the Hall sensor.

[0065] The transfer assembly and the discharging assembly have various configurations. For example, the transfer assembly comprises a receiving box 39 movably arranged on the second track 12, the receiving box 39 is provided with an inlet and outlet for the reaction tank 2 to enter and leave on one 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, the cavity is provided with a limiting piece for limiting the reaction tank 2 from leaving the receiving box 39, the receiving box 39 is provided with a pushing window with a smaller longitudinal section than the inlet and outlet on the side away from the discharge port 11, and the top of the receiving box 39 is provided with a discharge port communicating with the reaction tank 2; a third driving member is in transmission connection with the receiving box 39 for driving the receiving box 39 to move along the second track 12, when the receiving box 39 moves to the discharge port 11, the inlet and outlet are aligned with the reaction tank 2, and when the receiving box 39 moves to the inlet port 10, the third driving member is aligned with the pushing window; a fourth driving member 34 is arranged close to and towards the inlet port 10 of the other reactor 1, and the fourth driving member 34 is located on the extension line of the first track; the reaction tanks 2 are continuously distributed from one end of the first track close to the inlet port 10 to the other end of the first track close to the discharge port 11, the distance between the discharge port 11 and the second track 12, and the distance between the inlet port 10 and the second track 12 are all less than the length of the reaction tank 2 in the feeding direction; the discharging assembly comprises a second track 12 arranged perpendicularly to the plane on which the reactors 1 are arranged, and the second track 12 is annular, and the discharging assembly comprises a second vibrator arranged on the reaction tank 2 and / or the receiving box 39; the product collection area 13 comprises 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 capable of causing the structure on which the vibrator is installed to vibrate up and down, or left and right, or swing around itself, and the specific structure of the vibrator will not be described here.

[0066] As shown in Figure 4 , the second track 12 is composed of two rows of parallel chains, the chains are supported and driven to rotate by a plurality of supporting wheels, the supporting wheels are arranged on a rotating shaft, and a rotating motor or other rotating driving device 35 is connected to the other end of the rotating shaft. The second track 12 is not limited to the above-mentioned form, and can also be a slide rail, a guide rail or other structure capable of satisfying the functions of the second track.

[0067] When the second driving member pushes the reaction tank 2 out of the discharge port 11 of the reactor 1, the third driving member drives the receiving box 39 to move to the position of the discharge port 11 of the reactor 1 (according to the judgment of the second detector on the position of the reaction tank 2), 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, then the second driving member continues to move the reaction tank 2 towards the direction close to the second track 12, so that the reaction tank 2 is separated from the first track and enters the receiving box 39, after the reaction tank 2 enters the receiving box 39, the limiting member acts on the reaction tank 2, so that the reaction tank 2 will not be separated from the receiving box 39 when moving along the direction of the second track 12, and will not fall out of the receiving box 39; then the third driving member drives the reaction tank 2 to move on the second track 12 towards the direction close to the inlet port 10 of the other reactor 1, because the plane of the second track 12 is perpendicular to the plane of the reactor, the product collection area 13 is located below the second track 12, the receiving box 39 is provided with a discharge port communicated with the reaction tank 2, so when the reaction tank 2 moves to the product collection area 13, the discharge port will be downward, i.e. arranged towards the first collection bin 17, the first inlet of the first collection bin 17 needs to be large enough to prevent the product in the reaction tank 2 from leaking to the outside when the product is discharged, and the second vibrator is started synchronously, so that the product in the reaction tank 2 can be completely discharged into the first collection bin 17, and whether the reaction tank 2 is completely discharged is judged according to the feedback of the first detector, if the first detector feedbacks that there is still material remaining in the reaction tank 2, the reaction tank 2 continues to discharge in the product collection area 13 until the product in the reaction tank 2 is completely discharged, after the reaction tank 2 is completely discharged, the third driving member drives the receiving box 39 to continue to push on the second track 12 towards the direction close to the inlet port 10 of the other reactor 1, and when it is judged according to the feedback of the second detector that the reaction tank 2 reaches the position on the second track 12 corresponding to the inlet port 10 of the other reactor 1, the fourth driving member 34 is started, the output shaft of the fourth driving member 34 extends towards the feeding direction and extends into the pushing window to contact the reaction tank 2 (at this time, the reaction tank 2 needs to have a side shell capable of being pushed by the third driving member), and continues to push the reaction tank 2 towards the feeding direction until the reaction tank 2 is pushed onto the first track of the other reactor 1, and then the second driving member of the other reactor 1 drives the reaction tank 2 to move in the feeding direction.

[0068] In the present application, the feeding member is located near the inlet port of the reactor, and in the process of pushing the reaction tank towards the inlet port of the reactor by the fourth driving member 34, the feeding member adds catalyst and other reactants to the reaction tank.

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

[0070] The limiting member can be a magnet arranged in the cavity, and in this case, the reaction tank 2 is made of a magnetic material that can be attracted by the magnet. Alternatively, the limiting member can be a limiting block arranged in the cavity and on both sides of the feeding direction, and a spring or other reset member is arranged between the limiting block and the cavity. The side of the limiting block close to the reactor 1 is provided with a guide surface, and the guide surface is arranged obliquely relative to the cavity. A space is arranged between the two guide surfaces, and the space on the side of the guide surface close to the reactor 1 is larger than the space on the side of the guide surface away from the reactor 1. The cross section of the space between the two guide surfaces is in the shape of Y. The bottom of the reaction tank 2 is provided with a pulley matched with the second track 12, and in this case, the third driving member can be a rotary driving device 35, such as a servo motor, arranged on the reaction tank 2 and in transmission connection with the pulley, and capable of driving the pulley to move on the second track 12. The fourth driving member 34 can be a linear driving device, such as a pneumatic cylinder or a hydraulic cylinder, and the fourth driving member 34 needs to be arranged to avoid the first track and the second track 12.

[0071] Alternatively, the transfer assembly can not adopt the structure described in the above section. The transfer assembly includes a mechanical arm and a driving part in transmission connection with the mechanical arm. The driving part is used to drive the mechanical arm to move from the feeding port 10 towards the second track 12, and to drive the mechanical arm to move from the second track 12 towards the feeding port 10. The mechanical arm includes a transmission part connected with the driving part. The transmission part can be a joint or a connecting rod structure connecting the driving part with a gripper, and the gripper is arranged at the end of the transmission part away from the driving part and is used to clamp and release the reaction tank 2. The discharging assembly includes a first bin door and a third vibrator arranged on the reaction tank 2. The first bin door is arranged at a discharging port at the bottom of the reaction tank 2, and the second track 12 is provided with a discharging port corresponding to the discharging port. The first bin door is in transmission connection with a fifth driving member. 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 unblock the discharging port. The product collection area 13 includes a second collection bin located below the second track 12 and having a second inlet at the top. In this case, 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 mechanical arm, the driving part includes driving structures arranged in multiple directions. The driving part needs to include a first driving structure capable of driving the gripper to clamp and release, a second driving structure capable of driving the mechanical arm to move along the second track 12 from the discharging port 11 of one of the reactors 1, a third driving structure capable of driving the mechanical arm to move from the discharging port 11 of one of the reactors 1 towards the feeding port 10 of the other reactor 1, a fourth driving structure capable of driving the mechanical arm to move from the second track 12 towards the feeding port 10 of the other reactor 1, and a fifth driving structure capable of driving the mechanical arm to move in a vertical plane towards and away from the second track 12. The first to fifth driving structures can be linear driving devices, such as pneumatic cylinders, or rotary driving devices 35, such as rotary motors, according to the movement type of the mechanical arm.

[0073] After the reaction tank 2 is output from the discharge port 11 of one of the reactors 1, the driving part can drive the mechanical arm to move, and the reaction tank 2 is moved to the second track 12. When the reaction tank 2 moves to the product collection area 13, the first door is driven to move by the fifth driving part, and then the unloading port is unblocked. The product in the reaction tank 2 is discharged through the unloading port, the discharge port and the second inlet into the second collection bin. After the reaction tank 2 is completely discharged, the mechanical arm is driven by the driving part to move, and the reaction tank 2 is moved to the first track of the other reactor 1.

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

[0075] According to different working conditions, the transfer mechanism can be manually operated by an operator, or the detector group, the transfer assembly, the discharge assembly, the third driving part, the fourth driving part 34 and the fifth driving part in the transfer mechanism can be connected with the controller, and the operator manually inputs the operation instruction, so that the controller automatically controls the transfer mechanism according to the operation instruction. The feeding part 5 can be arranged between the second track 12 and the feeding port 10 of the reactor 1, so that the reaction tank 2 can be filled with catalyst before entering the reactor 1.

[0076] It should be noted that the structures in the detector group and the detection assembly which enter the reactor 1 with the reaction tank 2 are made of high-temperature-resistant materials, or a high-temperature-resistant layer is arranged on the surface of the corresponding structures in the detector group and the detection assembly, so that the structures in the detector group and the detection assembly which enter the reactor 1 with the reaction tank 2 can withstand the high temperature of natural gas reaction without damage or failure.

[0077] As Figure 1 , Figure 2 , Figure 6 , Figure 7As shown, the decarburization hydrogen production machine set includes two decarburization hydrogen production units, and the catalyst filling area 14 is formed at the feed inlet 10 of the reactor 1, and the product collection area 13 is formed at the discharge outlet 11, and the catalyst filling area 14 of one of the reactors 1 and the product collection area 13 of the other reactor 1 are adjacently arranged; the transfer mechanism further includes a partition plate 33 arranged between the adjacently arranged product collection area 13 and catalyst filling area 14, the partition plate 33 is arranged to avoid the second track 12, 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 boundary 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 further includes a shell sleeved on the second track 12 and the fourth driving member 34, the shell is provided with a reaction tank replacement submarine cabin 25, a glove box 32, an observation window 4 and the like. Before the decarburization hydrogen production is in a working state, the shell also needs to be replaced by inert gas to replace the air in the shell to create an oxygen-free environment, and a vacuum valve can be arranged on the shell, and the shell is communicated with the inert gas source through a pipeline, when being emptied, the pump and valve on the inert gas source and the pipeline of the shell are opened, and the air is discharged through the inert gas, and whether the air is discharged can be judged through the detection mechanism such as the gas sensor arranged on the shell.

[0078] The decarburization hydrogen production unit further comprises a first cover plate 15 arranged at the feed inlet 10 and a second cover plate 16 arranged at the discharge outlet 11, when the reactor 1 is independently arranged with the intermediate mechanism, the first cover plate 15 seals the feed inlet 10 under a first action force, and the second cover plate 16 seals the discharge outlet 11 under a second action force; the gas phase environment in the reactor 1 is maintained by sealing the feed inlet 10 and the discharge outlet 11 by the first cover plate 15 and the second cover plate 16 respectively, when the reactor 1 is in the feeding state, the first cover plate 15 unseals the feed inlet 10 under a third action force, and the second cover plate 16 unseals the discharge outlet 11 under a fourth action force; the first cover plate 15 and the second cover plate 16 have various forms, for example, the first cover plate 15 is rotationally connected with a mounting plate arranged at the discharge outlet 11, the size of the first cover plate 15 is larger than the size of the feed inlet 10, so as to seal the feed inlet 10; or, the size of the first cover plate 15 can be slightly smaller than the size of the feed inlet 10, and a corresponding sealing element is arranged between the first cover plate 15 and the feed inlet 10, so as to maintain the sealing of the feed inlet 10 by the first cover plate 15, at this time, the first action force can be the gravity of the first cover plate 15 itself, or a torsional spring is arranged at the connection between the first cover plate 15 and the mounting plate, so that the first cover plate 15 seals the feed inlet 10 under the combined action of its own gravity and the torsional spring, at this time, the first cover plate 15 is drivingly connected with a rotary motor or other rotary driving equipment 35, the rotary driving equipment 35 drives the first cover plate 15 to rotate, thereby unsealing the feed inlet 10 by the first cover plate 15, the third action force is the force with which the rotary driving equipment 35 drives the first cover plate 15 to move away from the feed inlet 10; the second cover plate 16 is arranged in the same way as the first cover plate 15, the second action force can be the gravity of the second cover plate 16 itself, or the combined action force of the gravity of the second cover plate 16 itself and a torsional spring, and the fourth action force is the force with which the rotary driving equipment 35 drives the second cover plate 16 to move away from the discharge outlet 11. The first cover plate 15 and the second cover plate 16 can be arranged outside or inside the reactor 1, depending on the working condition.

[0079] The adjusting assembly comprises a deoxidizing element, a first emptying valve connected with the reactor 1, an external inert gas source connected with the gas inlet 31 of the reactor 1, a pipeline connecting the external inert gas source and the reactor 1, a pump for conveying inert gas arranged on the pipeline, and a second valve arranged at the gas inlet 31; before the reactor 1 starts to react, the second valve, the pump and the first emptying 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 which can inhibit or reduce the risk of hydrogen explosion; the inert gas source is a storage tank storing the inert gas; whether the air is exhausted and whether an oxygen-free environment is formed can be determined according to an oxygen sensor or a gas analyzer arranged on the reactor 1; the temperature adjusting element 21 is connected with the reactor 1, and can be an electric heating plate arranged on the reactor 1; the detecting assembly comprises a temperature sensor such as a thermocouple, a pressure sensor, a gas analyzer, an optical sensor, a camera, an ultrasonic sensor, an infrared sensor and other detectors which can detect the state of the catalyst in the reaction tank 2; according to the working condition requirements and the functions of the structures in the detecting assembly, 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 into the reaction tank 2 by the feeding element 5, the state change of the catalyst in the reaction tank 2 fed back by the structures such as the ultrasonic sensor, the infrared sensor and the camera in the detecting assembly, and the concentration and volume of the natural gas in the reaction tank 2, the controller controls the opening time, opening degree and other adjusting parameters of the first valve 26 (for example, each first valve 26 is opened for 13s, and the natural gas released in 13s can fully react with the catalyst and will not escape outside the reaction tank 2), thereby realizing the control of the amount of natural gas released into the reaction tank 2, to avoid too much natural gas and too much carbon deposition generated by the reaction of the natural gas and the catalyst; meanwhile, by controlling the adjusting parameters of the first valve 26 by the controller, it can also avoid too much natural gas released into a certain reaction tank 2, so that the remaining natural gas escapes into the space in the reactor 1 after the reaction of the natural gas, and enters the subsequent reaction tank 2 from top to bottom, so that the natural gas is blocked by the carbon deposition generated before the natural gas fully contacts with the catalyst, thereby reducing the hydrogen production efficiency of the natural gas; in addition, the first vibrator on the reaction tank 2 can be started when the natural gas is introduced into the reaction tank 2, and / or the first vibrator on the reaction tank 2 can be started according to the carbon deposition generation condition of the reaction tank 2 fed back by the structures such as the camera, the ultrasonic sensor and the infrared sensor, to reduce the coverage of the catalyst by the carbon deposition; however, it should be noted that the vibration amplitude of the first vibrator should not be too large, to prevent too large vibration amplitude from causing accidents such as hydrogen explosion.

[0081] As Figure 8 and Figure 9As shown, the top of the bin 7 is provided with a sealing cover 27, a second evacuation valve 28 and a gas replacement valve 29, the gas replacement valve 29 is connected with an inert gas source, before the reaction of the reactor 1, the second evacuation valve 28 and the gas replacement valve 29 are opened (the second evacuation valve 28 and the gas replacement valve 29 are only valves capable of controlling on-off), the inert gas enters the reactor 1 from the gas replacement valve, and the air is discharged.

[0082] As shown in the figure, Figure 1 , Figure 2 , Figure 6 , Figure 7 As shown, the reactor 1 further includes a preheating zone 18, a reaction zone 19 and a cooling zone 20 which are sequentially arranged and communicated along the feeding direction, the temperature of the reaction zone 19 is higher than that of the preheating zone 18 and that of the cooling zone 20, the feeding member 5 is communicated with the preheating zone 18, the hydrogen outlet 3 is communicated with the preheating zone 18, the gas inlet 31 is communicated with the cooling zone 20, and the natural gas inlet is communicated with an external natural gas source through the gas inlet 31; the preheating zone 18 enables the catalyst to gradually rise to a suitable reaction temperature; the cooling zone 20 is not really cooled, but compared with the reaction zone 19, the temperature is relatively low, and the preheating zone 18, the reaction zone 19 and the cooling zone 20 are respectively connected with temperature adjusting members 21 such as electric heating plates which are independent of each other and used for heating. The decarburization and hydrogen production unit further includes a heat exchanger 22, the heat exchanger 22 has a first inlet communicated with the hydrogen outlet 3, a second inlet communicated with an external coal bed natural gas source 23, a third outlet communicated with the gas inlet 31, and a fourth outlet communicated with a gas separation and purification device; the gas separation and purification device has a fifth outlet communicated with a hydrogen storage tank 24, and a sixth outlet communicated with 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 with the hydrogen gas having a certain residual heat, and is preheated for the second time in the cooling zone 20, so that the energy of the reactor 1 is utilized in stages, and the operation energy consumption is reduced. After the natural gas is stored in the hydrogen storage tank 24, it can be transported to a hydrogenation station for use.

[0083] When the reactor 1 comprises the preheating zone 18, the reaction zone 19 and the cooling zone 20, an intermediate cavity which is not directly communicated with the reaction tank 2 is further arranged in the reactor 1, the gas inlet 31 is communicated with the intermediate cavity, the intermediate cavity is at least distributed in the cooling zone 20, or alternatively, can be distributed in the whole reactor 1, the intermediate cavity is used for temporarily storing the natural gas, and ensures that the natural gas can enter the reaction tank 2 from the natural gas inlet, and makes the natural gas can exchange heat with the low-temperature zone in the reactor 1 before being released to the reaction tank 2, so as to realize the multi-stage utilization of the energy in the reactor 1. The intermediate cavity is provided with a nozzle, when the controller detects that the reaction tank 2 reaches the reaction zone 19 or other set starting reaction position according to the feedback of the position sensor on the reaction tank 2, the nozzle is just aligned with the natural gas inlet on the reaction tank 2, in order to avoid the natural gas sprayed by the nozzle from leaking, when the reaction tank 2 reaches the starting reaction position, the nozzle is just abutted with the natural gas inlet, the detection structure which can judge whether the nozzle is aligned with the natural gas inlet can be arranged on the reaction tank, such as a camera or a Hall sensor, when the controller judges that the reaction tank 2 has reached the starting reaction position and the nozzle is abutted with the natural gas inlet of the reaction tank 2 which has reached the reaction position according to the feedback of the detection structure and the position sensor, the controller controls the first valve 26 and the nozzle to be opened, and after a set amount of natural gas is released, the first valve 26 and the nozzle are closed, so as to prevent the natural gas from escaping to the outside of the reaction tank 2. When the natural gas is released into the reaction tank 2, if the opening and closing speed of the first valve 26 and the nozzle and the release rate of the natural gas are fast, the movement of the reaction tank 2 in the feeding direction does not need to be stopped; on the contrary, if the opening and closing speed of the first valve 26 and the nozzle and the release rate of the natural gas are slow, the movement of the reaction tank 2 in the feeding direction can be appropriately slowed down or even stopped.

[0084] In addition, the present application also provides a coal bed natural gas decarburization hydrogen production process, comprising the steps that: S1, discharging 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; S2, adding a set amount of catalyst into the reaction tank in the reactor 1, and uniformly dispersing the set amount of catalyst into the reaction tank; the natural gas is introduced into the reaction tank 2 towards the direction of the catalyst, and the introduction area and the release amount of the natural gas are adjusted according to the state change of the catalyst in the reaction process; S3, periodically adding catalyst into the reaction tank 2 and outputting the product in the reaction tank 2 according to the state change of the catalyst and the product in the reaction tank 2; wherein, in step S2, the natural gas is first exchanged heat with the hydrogen discharged from the reaction tank 2 before entering the reaction tank 2, then the natural gas is secondly exchanged heat in the low-temperature zone of the reactor 1, i.e. the cooling zone 20, and then enters the reaction tank.

[0085] In summary, the coal seam natural gas decarburization hydrogen production process and the automatic control system in the application have the following obvious advantages: ① Compared with the reactor in the prior art, the coal seam natural gas decarburization hydrogen production automatic control system in the application is a circulating double-channel kiln reactor, which increases the single-time catalyst feeding ratio, widens the natural gas cracking reaction area, and realizes the yield increase of hydrogen production. The temperature adjusting member is arranged in stages, which can quickly respond to the stage temperature difference in the reactor to prevent product defects. ② Coal seam natural gas multi-channel gas supply device. Adopting diversified and staged ratio supply to adapt to the morphological change of the catalyst during the reaction, increasing the surface area contact of natural gas and catalyst, avoiding reaction attenuation, and improving the natural gas cracking reaction rate. ③ Reaction tank optimization design, adopting a staged gas supply mode. Improve the utilization efficiency of the catalyst, prevent supersaturation adsorption, reduce the reaction time, and improve the product quality stability. Suitable for'sprout growth' catalyst. ④ Automatic catalyst filling equipment, adopting a rotary quantitative supply mode. With a distributing member, cooperating with the reaction tank, and synchronous feeding. Improve the quantitative controllability of the catalyst, and reduce the production process operation difficulty. ⑤ Transfer mechanism, which can realize high-efficiency reaction tank filling and by-product recovery. Reduce the production process operation difficulty, and save manpower and material resources.

[0086] The content mentioned in this paper and / or referred to, and / or the content before and / or after in the same sentence, can exist simultaneously, or exist separately, for example, A and / or B include only A or B, and A, B exist simultaneously, etc. And / or has the same meaning as and / or, which will not be repeated here.

[0087] The present application discloses a plurality of technical solutions, but there is no opposite technical inspiration.

[0088] The principles and implementation modes of the present application are described by using specific examples in the present application. The above examples are only used to help understand the method of the present application and its core idea; at the same time, for those skilled in the art, according to the idea of the present application, the specific implementation mode and application range will be changed. In summary, the content of the specification should not be understood as a limitation of the present application.

Claims

1. An automated control system for decarbonization and hydrogen production from coal seam natural gas, characterized in that, The automated control system for decarbonization and hydrogen production from coal seam natural gas includes several sets of decarbonization and hydrogen production mechanisms, and each decarbonization and hydrogen production mechanism includes a decarbonization and hydrogen production unit. The decarbonization hydrogen production unit includes: The reactor includes a reaction tank and a hydrogen outlet connected to the reaction tank. Several natural gas inlets are uniformly distributed on the reaction tank, connected to the reaction tank, and facing the catalyst within the reaction tank. Each natural gas inlet is connected to an external coalbed methane source. A first valve is provided at each natural gas inlet to control the flow of the natural gas, and these first valves are independently configured. An adjustment component, the adjustment component being used to adjust the reaction conditions within the reaction tank; The controller is signal-connected to the first valve and the regulating component respectively; Before the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment component to adjust the reaction conditions of the reactor to set conditions, including temperature and oxygen concentration; when the decarbonization and hydrogen production unit is in operation, the controller controls the adjustment parameters of the first valve, including the opening timing, opening duration, and opening degree of the first valve. The decarbonization hydrogen production unit includes a conveying assembly, which includes a first track arranged along the feeding direction. The first track extends from the feed inlet of the reactor to the discharge outlet of the reactor. A plurality of reaction tanks are arranged on the first track. The reaction tanks are drivenly connected to a second driving member. The second driving member is used to drive the reaction tanks to move in the feeding direction and enter and leave the reactor. The feeding direction is the direction of movement of the reaction tanks within the reactor. The decarbonization hydrogen production mechanism includes: Two decarbonization hydrogen production units arranged side by side with opposite feeding directions; A transfer mechanism is disposed near the feed inlet of one of the reactors and the discharge outlet of the other reactor; The transit agencies include: A second track is provided, extending from the inlet of one of the reactors toward the outlet of the other reactor, and a product collection area is provided along the path of the second track. A third driving component is used to drive the reaction tank to move along the second track; A discharge assembly for completely transferring the product in the reaction tank to the product collection area; When the transfer mechanism is in operation, the transfer component transfers the reaction tank at the outlet of one of the reactors to the second track. The third drive unit drives the reaction tank on the second track to move towards the inlet of the other reactor. The transfer component then transfers the reaction tank after it has been discharged from the product collection area to the first track at the inlet of the other reactor.

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

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

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

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

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

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

8. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The relay component includes: A receiving box is movably mounted on the second track. The receiving box has an inlet and outlet for entering and leaving the reaction tank on the side facing the discharge port of one of the reactors. The receiving box has a cavity for accommodating the reaction tank. The receiving box has a push window with a longitudinal section smaller than the inlet and outlet on the side away from the discharge port. The receiving box has a discharge port connected to the reaction tank. The third driving component is connected to the receiving box for transmission. The third driving component is used to drive the receiving box to move along the second track. When the receiving box moves to the discharge port, the inlet and outlet are aligned with the reaction tank. When the receiving box moves to the feed port, the third driving component is aligned with the push window. A fourth drive unit is disposed near and toward the feed inlet of another of the reactors, and the fourth drive unit is located on the extension of the first track; The reaction tanks are continuously distributed from one end of the first track near the feed inlet to the other end of the first track near the discharge outlet. The distance between the discharge outlet and the second track, and the distance between the feed inlet and the second track, are both less than the length of the reaction tanks in the feed direction. The discharge assembly includes a second track arranged perpendicularly to the plane of the reactor and in a ring shape; the discharge assembly includes a second vibrator disposed on the reaction tank and / or the receiving box; the product collection area includes a first collection chamber disposed below the second track and having a first inlet at the top.

9. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 1, characterized in that, The transfer assembly includes a robotic arm and a drive unit. The drive unit is connected to the robotic arm via a transmission mechanism. The drive unit is used to drive the robotic arm to move from the feed inlet toward the direction closer to the second track, and to drive the robotic arm to move from the second track toward the direction closer to the feed inlet. The robotic arm includes a transmission unit connected to the drive unit, and a gripper located at the end of the transmission unit away from the drive unit. The gripper is used to grip and release the reaction tank. The discharge assembly includes a third vibrator mounted on the reaction tank and a first gate located at the discharge port at the bottom of the reaction tank. A discharge port corresponding to the discharge port is provided on the second track. The first gate is connected to a fifth drive unit. When the third drive unit moves the reaction tank to the product collection area, the fifth drive unit drives the first gate to release the blockage of the discharge port. The product collection area includes a second collection chamber located below the second track and having a second inlet at the top.

10. The automated control system for coalbed methane decarbonization and hydrogen production according to any one of claims 1, 8, and 9, characterized in that, The decarbonization hydrogen production unit includes a first cover plate at the inlet and a second cover plate at the outlet. When the reactor and the transfer mechanism are set up independently, the first cover plate blocks the inlet under a first force, and the second cover plate blocks the outlet under a second force. When the reactor is in the feeding state, the first cover plate releases the blockage of the inlet under a third force, and the second cover plate releases the blockage of the outlet under a fourth force.

11. The automated control system for coalbed methane decarbonization and hydrogen production according to any one of claims 1, 8, and 9, characterized in that, The reactor further includes a preheating zone, a reaction zone, and a cooling zone arranged sequentially and connected along the feed direction. The temperature of the reaction zone is higher than the temperature of the preheating zone and the temperature of the cooling zone. The hydrogen outlet is connected to the preheating zone, and the natural gas inlet is connected to the inlet of the cooling zone.

12. The automated control system for coalbed methane decarbonization and hydrogen production according to claim 11, characterized in that, The adjustment component includes: The deoxidizing component includes a first vent valve connected to the reactor, an external inert gas source connected to the inlet of the reactor, and a second valve located at the inlet. A temperature regulating element, which is connected to the reactor; And / or, the decarbonization hydrogen production unit further includes: The heat exchanger has a first inlet connected to the hydrogen outlet, a second inlet connected to the external coalbed natural gas source, a third outlet connected to the gas inlet, and a fourth outlet connected to a gas separation and purification device; the gas separation and purification device has a fifth outlet connected to the hydrogen storage tank and a sixth outlet connected to the external coalbed natural gas source.

13. A coal seam natural gas decarbonization and hydrogen production process using the automated control system for coal seam natural gas decarbonization and hydrogen production according to claim 1, characterized in that, include: Step S1: Expel the air from the reactor, inject a set amount of inert gas, and adjust the temperature in the reaction tank to a set value; Step S2: Add a set amount of catalyst to the reaction tank inside the reactor and evenly disperse the set amount of catalyst in the reaction tank; introduce natural gas into the reaction tank in the direction of the catalyst, and adjust the gas introduction area and release rate; Step S3: Periodically add catalyst to the reaction tank and output the product from the reaction tank; In step S2, before the natural gas enters the reaction tank, the natural gas first exchanges heat with the hydrogen discharged from the reaction tank. Then, the natural gas enters the low-temperature zone of the reactor for a second heat exchange before entering the reaction tank.

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