Reaction kettle for producing hydrogen from methanol and hydrogen production method

Abstract

The invention discloses a reaction kettle for producing hydrogen from methanol and a hydrogen production method. The reaction kettle comprises a tank body, a supporting frame is arranged in the tank body, a plurality of mutually independent reaction boxes are arranged on the supporting frame, each reaction box is filled with a catalyst, and electromagnetic valves are arranged at the inlet end and the outlet end of each reaction box; a gas inlet pipe and an exhaust pipe are further arranged on the tank body, one end of the gas inlet pipe is communicated with an external gas source, and a flow sensor, a flow regulating valve and a methanol sensor are further arranged on the gas inlet pipe; one end of the exhaust pipe is connected with the hydrogen collection and storage device, and the other end of the exhaust pipe is connected with the outlet end of each reactor in parallel; a controller is also arranged on the tank body and is electrically connected with the flow sensor, the flow regulating valve, the methanol sensor and the electromagnetic valves respectively; the catalyst is divided into a plurality of modules through the plurality of reaction boxes which are connected in parallel, and the reaction boxes of corresponding stages are started as required, so that the catalyst is ensured to be matched with input methanol steam.

Description

Technical Field

[0001] This application relates to the technical field of methanol-to-hydrogen equipment, specifically to a reaction vessel and hydrogen production method for methanol-to-hydrogen production. Background Technology

[0002] Methanol-to-hydrogen is an important technology for hydrogen production. In existing technologies, methanol vapor and water vapor are first generated by heating. Then, the mixture of methanol vapor and water vapor is introduced into a reactor. The reactor is equipped with a large number of reaction tubes, which are filled with catalysts, and the spaces between the reaction tubes are filled with heating oil. Methanol vapor and water vapor enter from one end of the reaction tubes and are converted into hydrogen under the action of the catalyst. The tail gas is discharged from the other end of the reaction tubes.

[0003] However, in systems using solar energy for methanol-to-hydrogen production, the concentrations of methanol vapor and water vapor fluctuate due to factors such as heat loss during transport and the stability of circulating heat mass temperature. Since the amount of catalyst in the reaction tube is fixed, the two cannot be matched. If the concentrations of methanol vapor and water vapor are too high, the hydrogen recovery rate will easily decrease. If the concentrations are low, the catalyst in the latter half of the reaction tube cannot be utilized. The equipment has poor adaptability to the concentrations of methanol vapor and water vapor. Summary of the Invention

[0004] The main objective of this application is to provide a reaction vessel and hydrogen production method for methanol-to-hydrogen production, aiming to solve the shortcomings of the prior art in terms of poor adaptability to the concentration of the input gas.

[0005] A reaction vessel for methanol-to-hydrogen production, comprising a tank body; A support frame is disposed inside the tank; several independent reaction chambers are disposed on the support frame, each reaction chamber is filled with a catalyst; and a solenoid valve is disposed at the inlet and outlet ends of each reaction chamber. An air inlet pipe is installed on the tank body. One end of the air inlet pipe is connected to an external air source. The air inlet pipe is also equipped with a flow sensor, a flow regulating valve, and a methanol sensor. The other end of the air inlet pipe is connected in parallel to the inlet of each of the reaction chambers. An exhaust pipe is provided on the tank body, one end of which is connected to a hydrogen collection and storage device, and the other end is connected in parallel to the outlet of each of the reactors. The controller is mounted on the tank and is electrically connected to the flow sensor, the flow regulating valve, the methanol sensor, and each of the solenoid valves.

[0006] Optionally, the reaction chambers are arranged sequentially in height along the axial direction of the tank.

[0007] Optionally, the support frame includes a frame body, and along the height direction of the frame body, several layers of support plates are provided on the frame body, and each of the reaction boxes is disposed on the support plates.

[0008] Optionally, the reaction chamber includes an interconnected chamber body and a cover plate. Several guide plates are provided inside the chamber body, each of which has an arc-shaped structure and is arranged in a concentric circle structure inside the chamber body. A dividing plate for separating the air inlet and the air outlet is also provided inside the chamber body.

[0009] Optionally, the tank body is also provided with a heating module. The tank body has a ring structure with a heating chamber in the middle. Each of the support plates is provided with a heating hole. The heating module passes through each of the heating chambers and each of the heating holes in sequence.

[0010] Optionally, the tank body is also equipped with a mixing box, the outlet end of which is connected to the air inlet pipe, and its inlet end is connected to a water vapor source and a methanol vapor source respectively; a mixing roller is rotatably installed inside the mixing box, and a number of stirring blades are installed on the mixing roller, with the stirring blades facing the inlet end of the mixing box.

[0011] Optionally, the mixing box is provided with a heating jacket, the heating jacket is provided with a spiral plate, and the heating jacket is also provided with an inlet pipe and an outlet pipe for the heating medium to enter and exit.

[0012] Accordingly, this application also discloses a hydrogen production method based on the above-mentioned reactor, including the following steps: Obtain the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time; Calculate the actual amount to be processed based on the flow rate and concentration parameters; Obtain the processing capacity parameters of a single reaction chamber, and calculate the number of stages of the reaction chamber based on the actual amount to be processed; Control the on / off state of each solenoid valve to open the reaction chamber with the same number of stages; The steps of repeatedly obtaining the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time interval T are repeated.

[0013] Optionally, the processing capacity parameters of a single reaction chamber are obtained, and the number of stages of the reaction chamber is calculated in combination with the actual amount to be processed, including the following steps: Retrieve the preset list of processing capacity parameters; Obtain hydrogen recovery rate parameters, and select processing capacity parameters from the processing capacity parameter list based on the hydrogen recovery rate parameters.

[0014] Optionally, the formula for calculating the actual amount to be processed is A=t0*v*c, where t0 represents the unit time, v represents the flow rate parameter, and c represents the concentration parameter of methanol vapor; the formula for calculating the number of stages is n=A / A0, where A0 represents the processing capacity parameter of the reaction chamber; and the time T is 5-15 min.

[0015] Compared with the prior art, this application has the following beneficial effects: This application includes a tank body, within which a support frame is provided. Several independent reaction chambers are mounted on the support frame, each filled with a catalyst. Each reaction chamber has an inlet and an outlet valve. The tank body also includes an inlet pipe and an outlet pipe. One end of the inlet pipe is connected to an external gas source, and a flow sensor, a flow regulating valve, and a methanol sensor are mounted on the inlet pipe. The other end of the inlet pipe is connected in parallel to the inlet of each reaction chamber. One end of the outlet pipe is connected to a hydrogen storage device, and the other end is connected in parallel to the outlet of each reactor. The tank body also includes a controller, which is electrically connected to the flow sensor, the flow regulating valve, the methanol sensor, and each of the solenoid valves. Accordingly, this application also discloses a hydrogen production method based on the above-mentioned reactor. First, the flow rate parameter of the inlet pipe and the concentration parameter of methanol vapor per unit time are obtained; then, the actual amount to be processed is calculated based on the flow rate parameter and the concentration parameter; then, the number of stages of the reactor is calculated based on the processing capacity parameter of a single reactor and the actual amount to be processed; the number of reactors participating in hydrogen production is controlled according to the number of stages; finally, the above operation is repeated once at intervals. First, this application encapsulates the catalyst into several independent reaction chambers, with each chamber operating independently. Compared to the monolithic structure of existing technologies, the gas involved in the reaction no longer needs to move from the top to the bottom of the tank, resulting in a shorter gas flow path and allowing the generated hydrogen to be discharged more quickly. Simultaneously, due to the separate packaging of the reaction chambers, the contact area between methanol vapor and water vapor and the catalyst is increased, which is beneficial to improving the overall hydrogen production efficiency of the equipment. Secondly, since each reaction chamber is independent and some chambers can be shut down as needed, other chambers can still function normally even when the catalyst in one or more reaction chambers fails, thus enhancing the equipment's fault tolerance. Furthermore, during prolonged operation under low-concentration conditions, this application not only concentrates methanol vapor for hydrogen production, which helps increase the concentration of the feed gas and improve hydrogen production efficiency, but also protects the catalyst in the closed reaction chambers, thereby staggering the catalyst failure times in different reaction chambers and further improving the equipment's fault tolerance.

[0016] Finally, when the input of methanol gas and water vapor increases and exceeds the catalytic capacity of one or more reaction tanks, the catalytic hydrogen production capacity of the entire reactor can be expanded as quickly as possible by starting a backup reaction tank. This allows excess gas to be directly introduced into a new reaction tank for hydrogen production, avoiding prolonged waiting of gas at the inlet. This ensures both hydrogen production efficiency and gas turnover efficiency, while also preventing unconverted methanol vapor from entering the tail gas, thus ensuring that the hydrogen recovery rate at the outlet fluctuates within an acceptable range. Furthermore, the parallel arrangement of several reaction tanks effectively makes the catalytic hydrogen production capacity of the equipment more flexible, adapting it to the gas concentration at the input end and meeting the working requirements of different operating conditions. Meanwhile, the above purpose can be achieved by setting up a parallel structure, which is simple in structure and does not require additional equipment, thus helping to reduce equipment costs. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the structure of a reaction vessel for methanol-to-hydrogen production provided in Embodiment 1 of this application; Figure 2 A front view of a reaction vessel for methanol-to-hydrogen production provided in Embodiment 1 of this application; Figure 3 This is an exploded view of the reaction chamber; Figure 4 This is a cross-sectional view of the reaction chamber; Figure 5 This is a schematic diagram of the mixing tank. Figure 6 A flowchart of the hydrogen production method provided in Embodiment 2 of this application;

[0018] Reference numerals: 1-Tank body, 2-Support frame, 3-Reaction chamber, 4-Solenoid valve, 5-Inlet pipe, 6-Flow sensor, 7-Flow regulating valve, 8-Methanol sensor, 9-Exhaust pipe, 10-Controller, 11-Heating chamber, 12-Heating hole, 13-Mixing box, 14-Mixing roller, 15-Agitator blade, 16-Heating jacket, 17-Spiral plate, 18-Inlet pipe, 19-Outlet pipe, 20-Heating rod, 201-Frame, 202-Support plate, 301-Box body, 302-Cover plate, 303-Guide plate, 304-Divider plate.

[0019] The purpose, features, and advantages of this application will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0020] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0021] It should be noted that all directional indications (such as up, down, left, right, front, back, etc.) in the embodiments of the present invention are only used to explain the relative positional relationship and movement of each component in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indication will also change accordingly.

[0022] In this invention, unless otherwise explicitly specified and limited, the terms "connection," "fixed," etc., should be interpreted broadly. For example, "fixed" can mean a fixed connection, a detachable connection, or an integral part; it can mean a mechanical connection or an electrical connection; it can mean a direct connection or an indirect connection through an intermediate medium; it can mean the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0023] Furthermore, if the embodiments of this invention involve descriptions such as "first" or "second," these descriptions are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of those features. Additionally, the meaning of "and / or" throughout the text includes three parallel solutions; for example, "A and / or B" includes solution A, solution B, or a solution where both A and B are satisfied simultaneously. Furthermore, the technical solutions of the various embodiments can be combined with each other, but this must be based on the ability of those skilled in the art to implement them. When the combination of technical solutions is contradictory or impossible to implement, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection claimed by this invention.

[0024] Implementation Method 1 Reference Figures 1 to 5 This embodiment, as an optional embodiment of this application, discloses a reaction vessel for methanol-to-hydrogen production, including a tank body 1. The tank body 1 includes a tank body with a cylindrical structure. Both the upper and lower sides of the tank body are open and sealed by a sealing cap. The sealing cap is connected to the tank body by connecting bolts. The above-mentioned structural design facilitates the maintenance of equipment inside the pipe and improves the maintainability of the equipment; The reactor also includes a support frame 2, which includes a frame body 201 and a plurality of support rods. Preferably, there are three support rods arranged in a triangular structure. Connecting frames are provided at the top and bottom of the support rods to connect the support rods and ensure the stability of the structure. The support frame 2 also includes a plurality of support plates 202, which are distributed sequentially along the height direction of the frame 201 and are respectively connected to the frame 201; It should be noted that the number of support plates 202 can be flexibly adjusted as needed to make fuller use of the internal space of the tank 1; In the above structure, each reaction chamber 3 is arranged sequentially along the height direction, which not only makes better use of the space inside the tank 1, but also effectively controls the length of the airflow path, thereby avoiding long-distance ineffective paths and ensuring that the hydrogen produced by catalysis can be discharged at the fastest speed, thus improving the hydrogen production efficiency of the equipment.

[0025] A reaction chamber 3 is provided on each of the support plates 202. The reaction chamber 3 includes a box body 301 and a cover plate 302 connected to each other. The reaction chamber 3 has an overall annular structure, and the central cavity is a heating chamber 11. The heating chamber 11 expands the contact area between the reaction chamber 3 and the heat exchange medium such as heating oil, thereby improving the heat transfer efficiency. On the other hand, the heating chamber 11 can guide the heat exchange medium such as heating oil into the middle area of ​​the reaction chamber 3, thereby heating the annular heating chamber in both the inner and outer directions. This effectively avoids heating blind spots, improves the temperature uniformity inside the reaction chamber 3, and ensures the efficiency of catalytic hydrogen production. Meanwhile, the structural design of the chamber 301 and the cover plate 302 also makes it convenient for staff to disassemble the reaction chamber 3 and replace the catalyst.

[0026] A partition is provided inside the housing 301. The two ends of the partition are integrally connected to the inner walls on both sides of the housing 301. The housing 301 is also provided with an air inlet and an air outlet, both of which are connected to a gas supply pipe. The air inlet pipe 5 and the air outlet pipe are respectively placed on both sides of the partition. By setting the partition, the air inlet and the air outlet are isolated, so that the gas can only rotate around the axis of the housing 301 once before being discharged. This ensures that methanol vapor and water vapor can only flow along the prescribed path in the housing 301, ensuring their residence time and preventing a large amount of methanol vapor and water vapor from mixing into the tail gas, thereby ensuring the hydrogen recovery rate. Meanwhile, a plurality of guide plates 303 are also provided inside the housing 301. The guide plates 303 are arranged in an arc shape, and the arc of each guide plate 303 is preferably 250°-270°. The radius of each guide plate 303 increases sequentially. With the center of the housing 301 as the center point, each guide ring is arranged in a concentric circle structure. The space between two adjacent guide plates 303 is a filling area, which is filled with catalyst. The 250°-270° arc ensures that an empty area is formed inside the box 301. The partition is set in the empty area and divides the empty area into two separate parts. The two areas are respectively connected to the inlet and outlet of each filling area. In the above structure, the guide plates 303 arranged in a concentric circle structure can be connected in parallel to set up several airflow channels in the box 301. On the one hand, this increases the contact area between the catalyst and methanol vapor, which is beneficial to improving the catalytic reaction efficiency. On the other hand, it can distribute the airflow more rationally, ensuring that the catalyst in different areas has a high concentration of methanol vapor passing through, and avoiding the accumulation of methanol vapor at the inlet end. Finally, the above-mentioned structural design can make more rational use of the space inside the reaction chamber 3 and improve the efficiency of catalytic hydrogen production.

[0027] It should be noted that in the above technical solution, one or two filling areas can be combined by setting a closed outlet and setting a new opening, thereby forming a maze-like airflow path in the box 301, thus ensuring the residence time of the airflow in the box 301 and ensuring the hydrogen recovery rate. Furthermore, in the inner filling zone, since it is close to the center of the box 301, its radius is smaller and its path is shorter. Therefore, in order to ensure catalytic conversion efficiency, baffles can be added in the filling zone. The baffles are staggered to form an S-shaped airflow path, thereby ensuring that the airflow paths in different channels are basically equal and ensuring hydrogen recovery rate.

[0028] Moreover, the above setup is simple in structure and low in cost.

[0029] It should be noted that the support frame 2 is connected to the sealing plate located on the lower side of the tank body, and the equipment can be quickly disassembled and assembled by means of the lifting frame. A mixing tank 13 is also provided on the top of the tank body 1. Two gas supply pipes are provided on the top of the mixing tank 13. Methanol vapor and water vapor are respectively introduced into the two gas supply pipes. A gas supply pipe for discharging the mixed gas is provided at the bottom of the mixing tank 13. An air inlet pipe 5 is also provided on the tank body 1. The inlet end of the air inlet pipe 5 is connected to the gas supply pipe to input the mixed gas into the pipe body. A mixing roller 14 is also rotatably installed inside the mixing tank 13, and a plurality of stirring blades 15 are provided on the mixing roller 14; the stirring blades 15 are directly facing the methanol vapor inlet and the water vapor inlet. Meanwhile, a heating box is also fitted on the mixing box 13. A heating interlayer 16 is between the heating box and the mixing box 13. A spiral plate 17 is provided in the heating interlayer 16. An inlet pipe 18 and an outlet pipe 19 for conveying the heating medium are respectively provided on the upper and lower sides of the heating box. In actual operation, when methanol vapor and water vapor enter the mixing tank 13, they will first drive the stirring roller to rotate, and then the stirring blades 15 will stir the methanol vapor and water vapor, thereby ensuring that the two are mixed faster and more evenly, and ensuring that the proportion of each component in the mixed gas entering the reaction tank 3 is within the ideal range; and the above mixing is non-powered mixing, without the need to add additional structures and power equipment. Secondly, the mixing tank 13, while mixing methanol vapor and water vapor, also serves as a buffer tank. It can regulate the airflow rate entering the pipe body to ensure that the mixed gas enters the reaction tank 3 at a stable flow rate, avoiding drastic fluctuations in flow rate. This not only helps to ensure the stability of hydrogen recovery rate, but also offsets drastic changes in flow rate over a period of time, avoiding frequent start-ups or shutdowns of some reaction tanks 3, and ensuring the stability of equipment operation. Finally, the spiral plate 17 can guide the heating medium in the heating jacket 16 to flow in an orderly manner, so that the heating medium can effectively ensure the temperature in the mixing box 13, thereby avoiding the re-condensation of methanol vapor and water vapor, and thus ensuring the gas quality at the inlet of the reaction box 3. During the pipeline transportation of methanol vapor and water vapor, heat loss is inevitable. The heating medium in the heating jacket 16 can preheat and supplement the gas before it enters the tank 1, thereby ensuring that the temperature difference between the reaction gas and the temperature inside the reaction chamber 3 is within a controllable range, thus ensuring the temperature stability inside the reaction chamber 3, achieving stable hydrogen production, and improving the stability of hydrogen recovery rate at the outlet.

[0030] The reactor also includes an inlet pipe 5 and an exhaust pipe 9. The inlet end of the inlet pipe 5 is connected to the mixed gas outlet end of the mixing tank 13, and the other end of the inlet pipe 5 is sealed. Along the axial direction of the inlet pipe 5, several branch pipes are provided on the outer circumferential surface of the inlet pipe 5. Several connecting sleeves are also provided on the tank body. One end of the connecting sleeve is connected to each of the branch pipes, and the other end is connected to the inlet end of each of the reaction tanks 3, thereby realizing the parallel connection between the inlet pipe 5 and each of the reaction tanks 3.

[0031] Solenoid valves 4 are installed on each branch of the intake pipe 5. Flow sensor 6, flow regulating valve 7, and methanol sensor 8 are also installed on the intake pipe 5. The outlet end of the exhaust pipe 9 is connected to a hydrogen receiving tank or a separating tank, and the other end is closed. At the same time, along the axial direction of the exhaust pipe 9, several branch pipes are also provided on the outer circumferential surface of the exhaust pipe 9. The branch pipes are also connected to the outlet ends of each of the reaction tanks 3 through connecting sleeves, thereby forming a closed-loop gas circuit.

[0032] In the above structure, both the air inlet pipe 5 and the air outlet pipe are located outside the tank body 1, while the reaction chamber 3 is located inside the tank body 1. On the one hand, this allows for the convenient placement of various sensors on the outside, ensuring their operational stability; on the other hand, it effectively reduces the number of pipes inside the tank body 1, thereby simplifying the disassembly and assembly process and improving the maintenance efficiency of the equipment.

[0033] The tank body 1 is also equipped with a controller 10, which includes a touch screen and a PLC. The PLC is electrically connected to the touch screen and is also electrically connected to the flow sensor 6, the flow regulating valve 7, the methanol sensor 8, and each of the solenoid valves 4. A heating module is also provided on the top of the tank body 1. The heating module includes several heating rods 20, which are inserted into the tank body 1 from the top. At the same time, heating holes 12 are provided on each of the support plates 202. Each heating hole 12 is coaxially arranged with each of the heating chambers 11. The heating rods 20 pass through each of the heating chambers 11 and each of the heating holes 12. The heating module is electrically connected to the PLC. Thermocouples are also installed inside the tank 1, and the thermocouples are electrically connected to the PLC; Thermocouples can be used to easily monitor the temperature inside tank 1. When the temperature drops, the heating module can quickly heat the tank to ensure the stability of the temperature inside tank 1. Secondly, since the heating module is located in the middle of the tank 1, and the heating medium diffuses from the outside to the inside of the tank 1, the heating module can effectively reduce the temperature difference between the heat exchange medium in different areas and ensure temperature consistency.

[0034] Implementation Method 2 Reference Figure 6 This embodiment, as an optional embodiment of this application, discloses a hydrogen production method based on the reactor described in Embodiment 1, including the following steps: S1. Obtain the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time; During equipment operation, the air volume of the intake pipe is controlled by a flow regulating valve, and the air volume is detected by a flow sensor to obtain flow parameters. Simultaneously, the methanol sensor detects the methanol concentration in the gas and obtains the concentration parameter of methanol vapor. S2. Calculate the actual amount to be processed based on the flow rate and concentration parameters; Substitute the flow rate and concentration parameters obtained in step S1 into the calculation formula for the actual amount to be processed. The calculation formula for the actual amount to be processed is A=t0*v*c, where t0 represents the unit time (its value is 1 minute or other time period, which is determined according to the actual situation. If the time is long, the average flow rate value within the time period is used as the flow rate parameter), v represents the flow rate parameter, and c represents the concentration parameter of methanol vapor. S3. Obtain the processing capacity parameters of a single reaction chamber, and calculate the number of stages of the reaction chamber based on the actual amount to be processed; S31. Retrieve the preset list of processing capacity parameters; The processing capacity parameter list is a list pre-stored in the controller; it describes the catalytic reaction amount of methanol vapor under different hydrogen recovery rates. S32. Obtain hydrogen recovery rate parameters, and select processing capacity parameters from the processing capacity parameter list based on the hydrogen recovery rate parameters.

[0035] The corresponding processing capacity parameters are retrieved from the processing capacity parameter list based on the pre-set hydrogen recovery rate parameters. Substitute the actual amount to be processed calculated in step S2 into the stage calculation formula to calculate the stage. The stage calculation formula is n=A / A0, where A0 represents the processing capacity parameter of the reaction chamber. S4. Control the on / off state of each solenoid valve to open the reaction chamber with the same number of stages. If the calculated stage number is 3, it means that 3 reaction chambers need to be turned on and all other reaction chambers need to be turned off. The specific reaction chambers are selected randomly or according to pre-set rules. After selection, the on / off state of the controller can be controlled by controlling the solenoid valves at the inlet and outlet of each reaction chamber, thereby achieving the adjustment of the reaction chambers.

[0036] S5. Repeat the steps of obtaining the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time at intervals T.

[0037] During operation, the amount of methanol vapor is constantly changing, so data needs to be collected again at regular intervals. The interval is 5-15 minutes, but can be set according to the actual situation. When the interval time is reached, the system repeats step S1 until the reaction chamber is readjusted. Repeating the above process can dynamically adapt to changes in methanol concentration.

[0038] Compared with the prior art, this application encapsulates the catalyst into several independent reaction chambers, which do not interfere with each other. Compared with the monolithic structure of the prior art, the gas participating in the reaction no longer needs to move from the top of the tank to the bottom of the tank, and the gas flow path is shorter, so the generated hydrogen can be discharged more quickly. At the same time, due to the separate packaging of the reaction chambers, the contact area between methanol vapor and water vapor and the catalyst is increased, which is beneficial to improving the hydrogen production efficiency of the entire equipment. Secondly, since each reaction chamber is independent and some chambers can be shut down as needed, other chambers can still function normally even when the catalyst in one or more reaction chambers fails, thus enhancing the equipment's fault tolerance. Furthermore, during prolonged operation under low-concentration conditions, this application not only concentrates methanol vapor for hydrogen production, which helps increase the concentration of the feed gas and improve hydrogen production efficiency, but also protects the catalyst in the closed reaction chambers, thereby staggering the catalyst failure times in different reaction chambers and further improving the equipment's fault tolerance.

[0039] Finally, when the input of methanol gas and water vapor increases and exceeds the catalytic capacity of one or more reaction tanks, the catalytic hydrogen production capacity of the entire reactor can be expanded as quickly as possible by starting a backup reaction tank. This allows excess gas to be directly introduced into a new reaction tank for hydrogen production, avoiding prolonged waiting of gas at the inlet. This ensures both hydrogen production efficiency and gas turnover efficiency, while also preventing unconverted methanol vapor from entering the tail gas, thus ensuring that the hydrogen recovery rate at the outlet fluctuates within an acceptable range. Furthermore, the parallel arrangement of several reaction tanks effectively makes the catalytic hydrogen production capacity of the equipment more flexible, adapting it to the gas concentration at the input end and meeting the working requirements of different operating conditions. Meanwhile, the above purpose can be achieved by setting up a parallel structure, which is simple in structure and does not require additional equipment, thus helping to reduce equipment costs.

[0040] The above are merely preferred embodiments of this application and do not limit the patent scope of this application. Any equivalent structural or procedural transformations made using the content of this application's specification and drawings, or direct or indirect applications in other related technical fields, are similarly included within the patent protection scope of this application.

Claims

1. A reaction vessel for methanol-to-hydrogen production, characterized in that, Including the tank body (1); A support frame (2) is installed inside the tank (1); several independent reaction boxes (3) are installed on the support frame (2), and each reaction box (3) is filled with a catalyst; each reaction box (3) is equipped with a solenoid valve (4) at its inlet and outlet ends. An air inlet pipe (5) is installed on the tank body (1). One end of the air inlet pipe (5) is connected to an external air source. A flow sensor (6), a flow regulating valve (7), and a methanol sensor (8) are also installed on the air inlet pipe (5). The other end of the air inlet pipe (5) is connected in parallel to the inlet end of each of the reaction tanks (3). An exhaust pipe (9) is provided on the tank (1). One end of the exhaust pipe (9) is connected to the hydrogen storage device, and the other end is connected in parallel to the outlet end of each of the reactors. The controller (10) is disposed on the tank (1) and is electrically connected to the flow sensor (6), the flow regulating valve (7), the methanol sensor (8) and each of the solenoid valves (4).

2. The reaction vessel for methanol-to-hydrogen production according to claim 1, characterized in that, Along the axial direction of the tank (1), each of the reaction chambers (3) is arranged in order of height.

3. A reaction vessel for methanol-to-hydrogen production according to claim 2, characterized in that, The support frame (2) includes a frame body (201), and several layers of support plates (202) are provided on the frame body (201) along the height direction of the frame body (201), and each of the reaction boxes (3) is provided on the support plate (202).

4. A reaction vessel for methanol-to-hydrogen production according to claim 3, characterized in that, The reaction chamber (3) includes a box body (301) and a cover plate (302) connected to each other. A plurality of guide plates (303) are provided inside the box body (301). Each guide plate (303) has an arc-shaped structure and is arranged in a concentric circle structure inside the box body (301). A dividing plate (304) for separating the air inlet and the air outlet is also provided inside the box body (301).

5. A reaction vessel for methanol-to-hydrogen production according to claim 4, characterized in that, The tank (1) is also provided with a heating module. The box (301) has a ring structure with a heating chamber (11) in the middle. Each of the support plates (202) is provided with a heating hole (12). The heating module passes through each of the heating chambers (11) and each of the heating holes (12) in sequence.

6. A reaction vessel for methanol-to-hydrogen production according to claim 1, characterized in that, The tank (1) is also provided with a mixing box (13), the outlet end of the mixing box (13) is connected to the air inlet pipe (5), and its inlet end is connected to a water vapor source and a methanol vapor source respectively; a mixing roller (14) is rotatably arranged inside the mixing box (13), and a number of stirring blades are arranged on the mixing roller (14), and the stirring blades are facing the inlet end of the mixing box (13).

7. A reaction vessel for methanol-to-hydrogen production according to claim 6, characterized in that, The mixing box (13) is provided with a heating jacket (16), a spiral plate (17) is provided inside the heating jacket (16), and an inlet pipe (18) and an outlet pipe (19) for the heating medium to enter and exit are also provided on the heating jacket (16).

8. A method for producing hydrogen from methanol using a reactor according to any one of claims 1-7, characterized in that, Includes the following steps: Obtain the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time; Calculate the actual amount to be processed based on the flow rate and concentration parameters; Obtain the processing capacity parameters of a single reaction chamber, and calculate the number of stages of the reaction chamber based on the actual amount to be processed; Control the on / off state of each solenoid valve to open the reaction chamber with the same number of stages; The steps of repeatedly obtaining the flow rate parameters of the intake pipe and the concentration parameters of methanol vapor per unit time interval T are repeated.

9. The hydrogen production method according to claim 8, characterized in that, The process of obtaining the processing capacity parameters of a single reaction chamber and calculating the number of stages of the reaction chamber based on the actual amount to be processed includes the following steps: Retrieve the preset list of processing capacity parameters; Obtain hydrogen recovery rate parameters, and select processing capacity parameters from the processing capacity parameter list based on the hydrogen recovery rate parameters.

10. The hydrogen production method according to claim 8, characterized in that, The formula for calculating the actual amount to be processed is A=t0*v*c, where t0 represents the unit time, v represents the flow rate parameter, and c represents the concentration parameter of methanol vapor; the formula for calculating the number of stages is n=A / A0, where A0 represents the processing capacity parameter of the reaction chamber; and the time T is 5-15 min.

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