A kind of thousand mark level methanol reforming hydrogen reactor structure

Abstract

The application discloses a kind of thousand mark level methanol reforming hydrogen reactor structures, including sequentially from bottom to top and form cylindrical reaction cavity first splicing shell, second splicing shell, third splicing shell and fourth splicing shell, gas from first splicing shell enters last from fourth splicing shell output;Dispersed methanol water vapor distribution mechanism is arranged in first splicing shell, catalytic mechanism is arranged in the inside of second splicing shell, catalytic mechanism is generated with methanol water vapor reforming reaction rich hydrogen conversion gas, spray mechanism and dispersion mechanism are installed in third splicing shell and are distributed in upper and lower, after conversion gas passes through dispersion mechanism, residual methanol is removed with spray mechanism output desalted water and conversion gas reverse contact;The spray mechanism of the application solves the methanol poisoning problem of PSA adsorbent, and the system annual operation length is more than 8000 hours, to realize maintenance-free stable operation.

Description

Technical Field

[0001] This invention relates to the field of hydrogen production equipment technology, specifically to a structure for a methanol reforming hydrogen production reactor with a capacity of 1,000 standard cubic meters. Background Technology

[0002] Hydrogen energy serves as a core protective element in strategic high-end manufacturing sectors such as nuclear power, aerospace, and semiconductors. Especially in the heat treatment process of stainless steel components for nuclear power plants, it places extremely stringent comprehensive requirements on the purity of hydrogen, the stability of its supply, and the operational reliability of hydrogen production equipment. Four core technical indicators must be met simultaneously: firstly, the hydrogen production scale must reach 1000 Nm³. 3 The system boasts a capacity of 1,000 cubic meters per hour, suitable for large-scale continuous heat treatment production; secondly, the hydrogen purity reaches 5N level (≥99.999%), and the total amount of key impurities CO+CO2 is controlled below 10ppm, eliminating quality defects such as oxidation, carburization, and intergranular corrosion in stainless steel components; thirdly, the annual continuous operation time of the hydrogen production system exceeds 8,000 hours, ensuring uninterrupted and non-stop nuclear power production processes; and fourthly, it has a wide load adjustment capability of 20% to 110%, adapting to the dynamically fluctuating hydrogen demand during heat treatment.

[0003] Methanol steam reforming for hydrogen production has become the mainstream technology for meeting the on-site supply of high-purity hydrogen in high-end manufacturing sectors due to its convenient raw material storage and transportation, flexible on-site hydrogen production, and strong process adaptability. However, current conventional methanol reforming hydrogen production reactors and supporting systems suffer from several insurmountable technical bottlenecks, making them completely unsuitable for the stringent operating conditions required for nuclear power plants. Specific technical deficiencies are as follows: Firstly, the reformed gas contains excessive impurities, which can easily cause downstream purification units to fail: the reformed gas produced by the existing reactor has a CO concentration as high as 1.5%, and is accompanied by a large amount of unreacted residual methanol. This not only significantly increases the difficulty of downstream purification, but the residual methanol can also directly cause the adsorbent in the downstream pressure swing adsorption (PSA) hydrogen extraction system to be poisoned and deactivated, resulting in a significant reduction in the lifespan of the PSA system, frequent equipment maintenance, and making it impossible to achieve long-term maintenance-free stable operation.

[0004] Secondly, the system integration is insufficient, and the core performance cannot be taken into account: Traditional reactors are not designed with a dedicated pre-protection unit for PSA systems. They rely solely on conventional purification processes to treat impurities, making it difficult to simultaneously achieve stable preparation of 5N-grade high-purity hydrogen, long-cycle operation of over 8000 hours, and wide-load dynamic adjustment. The reliability, continuity, and flexibility of equipment operation are seriously insufficient.

[0005] Third, the catalyst has shortcomings in performance and lacks the ability to control impurities at the source: the copper-based catalysts used in conventional methanol reforming to produce hydrogen mostly use traditional materials such as alumina as carriers, which have the core problems of poor thermal conductivity and low catalytic selectivity. They cannot suppress the generation of CO byproducts at the source of the reaction and can only rely on multi-stage purification at the back end to reduce the impurity content, resulting in a long process flow and high system energy consumption.

[0006] Fourth, the scale and load adaptability of the existing commercial methanol reforming hydrogen production units are insufficient: most of them are small-capacity units with hydrogen production scales far below the thousand standard cubic meter level, and the load adjustment range is generally narrow. They cannot meet the large-scale, wide-range fluctuating continuous hydrogen demand in the nuclear power field, making it difficult to achieve industrial-scale application.

[0007] In summary, existing methanol reforming hydrogen production reactors have significant shortcomings in terms of impurity control, system protection, catalyst performance, scale and load adaptability. They cannot simultaneously meet the four core requirements of nuclear power stainless steel heat treatment for hydrogen production at the 1,000-cubic-meter level, 5N-grade high purity, long-cycle operation, and wide load adjustment, which seriously restricts the localization and self-sufficiency of hydrogen equipment in high-end manufacturing.

[0008] Therefore, it is necessary to develop a methanol reforming hydrogen production reactor structure suitable for the harsh operating conditions of nuclear power plants. Summary of the Invention

[0009] The purpose of this invention is to provide a structure for a methanol reforming hydrogen production reactor with a capacity of 1,000 standard cubic meters, which aims to improve the shortcomings of existing methanol reforming hydrogen production reactors in terms of impurity control, system protection, catalyst performance, scale and load adaptability.

[0010] The present invention is implemented as follows: a thousand-standard-cubic-meter methanol reforming hydrogen production reactor structure includes a first splicing shell, a second splicing shell, a third splicing shell, and a fourth splicing shell connected end to end from bottom to top to form a cylindrical reaction chamber. Gas enters from the first splicing shell and exits from the fourth splicing shell. A distribution mechanism for dispersing methanol water vapor is provided in the first splicing shell. A catalytic mechanism is provided on the inner side of the second splicing shell. The catalytic mechanism reacts with the methanol water vapor to generate hydrogen-rich conversion gas. A spray mechanism and a dispersion mechanism are installed vertically in the third splicing shell. After the conversion gas passes through the dispersion mechanism, it comes into countercurrent contact with the demineralized water output from the spray mechanism to remove residual methanol. The catalytic mechanism includes a support frame, which includes a vertical shaft and support plates distributed at the upper and lower ends of the vertical shaft. A fixing plate is fixedly installed on the side of the middle of the two support plates that are far apart from each other. A clamping plate is detachably installed on the side of the fixing plate. The upper end of the vertical shaft extends into the space formed by the fixing plate and the clamping plate through a bearing connection. A support plate is detachably installed at the end of each support plate, and the support plate is fixed in the second splicing shell.

[0011] As an embodiment of the present invention, the catalytic mechanism further comprises a plurality of sets of catalytic modules distributed outside the vertical shaft, and the catalytic modules are located between the tray and the lower pressure ring; each set of catalytic modules comprises a sector-shaped outer bin and a sector-shaped inner bin, both the arc-shaped surface of the sector-shaped outer bin and the top surface of the sector-shaped inner bin are provided as openings, vent holes are provided on end faces of both the sector-shaped outer bin and the sector-shaped inner bin, and the sector-shaped inner bin is filled with hydroxyl-rich boron nitride nanosheet supported copper-based catalyst.

[0012] As an embodiment of the present invention, a disassembly hole is provided on the side wall of the second spliced shell, a filling plate is provided at the disassembly hole, a fitting plate is fixed outside the filling plate, and the fitting plate is detachably connected to the second spliced shell; the size of the disassembly hole is larger than that of the sector-shaped inner bin, and a pulling groove is provided on the arc-shaped surface of the sector-shaped inner bin.

[0013] As an embodiment of the present invention, a clamping post is installed at the end of the sector-shaped outer bin, the clamping post is located in a clamping groove, and the clamping groove is arranged along the height direction of the vertical shaft. The distribution mechanism comprises a second separating disc and a third supporting ring plate which are detachably connected up and down, a plurality of frustum-shaped holes are evenly distributed on the second separating disc, and the diameter of the lower end of the frustum-shaped hole is larger than that of the upper end.

[0014] As an embodiment of the present invention, the third supporting ring plate is fixedly installed in the first spliced shell, located above the inlet pipe and below the manhole of the first spliced shell.

[0015] As an embodiment of the present invention, the spray mechanism comprises a spray member, and the spray member comprises fan blades, a main pipe and a plurality of spray pipe groups which are distributed vertically; the plurality of spray pipe groups are divided into upper and lower layers, the two layers of spray pipe groups are distributed in a crossed manner and are both in communication connection with the main pipe; an end shaft is installed at the top of the main pipe, and the end shaft is connected to the central shaft of the fan blades through a coupling.

[0016] As an embodiment of the present invention, the spray mechanism further comprises a bracket, the bracket comprises a first supporting ring plate and a transverse plate, the transverse plate is detachably installed below the first supporting ring plate, and the first supporting ring plate is fixedly installed above the manhole of the third spliced shell; the main pipe is connected through a central pipe penetrating through the transverse plate through a bearing.

[0017] As an embodiment of the present invention, air inlet holes are circumferentially distributed on the side wall of the main pipe, an external connecting pipe is rotatably and mechanically sealed sleeved on the main pipe at a position facing the air inlet holes, the external connecting pipe is of an I-shaped structure, and the middle part of the external connecting pipe is communicated with a spray liquid pipe penetrating through the spliced shell.

[0018] As an embodiment of the present invention, an output pipe is installed at the top of the fourth spliced shell, the fan blades are located in the output pipe, and the gas flowing out from the output pipe agitates the fan blades to drive the plurality of spray pipe groups to rotate.

[0019] In one embodiment of the present invention, the dispersing mechanism includes a second support ring plate, a first partition plate installed above the second support ring plate, and multiple vertical pipes evenly installed on the first partition plate, with an umbrella shell provided at the top of each vertical pipe; the second support ring plate is installed below the manhole of the third splicing shell.

[0020] The beneficial effects of this invention are: 1. This invention solves the methanol poisoning problem of PSA adsorbent by setting up a spray mechanism, enabling the entire system to run for more than 8,000 hours per year and achieve maintenance-free and stable operation; by using boron nitride nanosheet supported copper-based catalyst, its high thermal conductivity and high selectivity inhibit CO generation and can produce 5N grade high-purity hydrogen, which meets the requirements of nuclear power stainless steel heat treatment.

[0021] 2. The catalytic mechanism of the present invention adopts a fan-shaped modular design, with special disassembly holes and pull-out grooves on the side wall of the second splicing shell. Each catalytic module can be independently and quickly disassembled and assembled without disassembling the entire reactor, thus shortening maintenance downtime and significantly reducing operation and maintenance costs and production losses.

[0022] 3. The spray element of the present invention is driven by the airflow output from the reactor to rotate the fan blades, which does not require an external motor and power supply, has no additional energy consumption and no electrical fault points; the double-layer cross spray pipe group rotates and sprays, realizing no dead corner coverage of the purification area and improving the de-alcoholization efficiency of the entire system. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the overall structure of the present invention; Figure 2 This is a schematic diagram of the overall internal structure of the present invention; Figure 3 This is a structural schematic diagram of the third and fourth splicing shells of the present invention; Figure 4 This is a schematic diagram of the structure of the second splicing shell of the present invention; Figure 5 This is a schematic diagram of the distribution mechanism of the present invention; Figure 6 This is a schematic diagram of the spray mechanism of the present invention; Figure 7 This is a schematic diagram of the structure of the bracket of the present invention; Figure 8 This is a schematic diagram of the structure of the spray component of the present invention; Figure 9 This is a schematic diagram of the dispersing mechanism of the present invention; Figure 10 This is a schematic diagram of the catalytic mechanism of the present invention; Figure 11 This is a schematic diagram of the support frame of the present invention; Figure 12This is a schematic diagram of the catalytic module of the present invention.

[0024] In the diagram: First splicing shell 1; base 11; inlet pipe 12; second splicing shell 2; disassembly hole 21; filling plate 22; bonding plate 23; third splicing shell 3; spray liquid pipe 31; manhole 32; fourth splicing shell 4; output pipe 41; spraying mechanism 5; bracket 51; first support ring plate 511; horizontal plate 512; central pipe 513; outer pipe 52; spray component 53; fan blade 531; end shaft 532; spray pipe assembly 533; main pipe 534; air inlet 535; dispersion mechanism 6; second support ring plate 61; External drain pipe; 62; First partition plate; 63; Vertical pipe; 64; Umbrella shell; 7; Catalytic mechanism; 71; Catalytic module; 711; Fan-shaped outer compartment; 712; Pull-out groove; 713; Vent hole; 714; Snap-on column; 715; Opening; 716; Support frame; 72; Vertical shaft; 721; Snap-on groove; 722; Tray; 723; Lower pressure ring; 724; Support plate; 725; Clamping plate; 726; Fixing plate; 727; Support plate; 728; Distribution mechanism; 8; Second partition plate; 82; Conical hole; 83; Third support ring plate. Detailed Implementation

[0025] The following will be based on embodiments of the present invention. Figures 1-12 The technical solutions in the embodiments of the present invention are clearly and completely described herein. 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.

[0026] It should be noted that all directional indicators (such as up and down, inner side, end, center, and outer side) in the embodiments of the present invention are only used to explain the relative positional relationship, installation method, and direction of movement of each component in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indicator will also change accordingly.

[0027] In this invention, unless otherwise explicitly specified and limited, the terms "end-to-end connection," "detachable connection," "fixed installation," "interconnection," "rotating sleeve," and "through-type setting," etc., should be interpreted broadly. For example, they can refer to end-to-end connection with flange sealing or bolted sealing connection; they can refer to detachable connection with snap-fit ​​or quick assembly / disassembly with bolt locking; they can refer to fixed installation with welding or stable installation with bolt positioning; they can refer to interconnection with pipelines or airflow conduction with cavity communication; they can refer to rotating sleeve with mechanical seal or flexible rotation with bearing adaptation; they can refer to through-type setting with coaxial insertion or pipeline through-type setting with sealing and limiting. For those skilled in the art, the specific meaning of the above terms in this invention can be understood according to the operating conditions of methanol steam reforming to produce hydrogen at the cubic meter level.

[0028] To address the problems of excessive residual methanol and CO impurities in the reformed gas of existing methanol reforming hydrogen production reactors, which can easily lead to poisoning and failure of downstream PSA adsorbents, low system integration, and inability to simultaneously handle 5N-grade high-purity hydrogen and 8000-hour long-term operation, this invention provides a 1000 Nm³-scale methanol reforming hydrogen production reactor structure. The reactor adopts an integrated design with a four-section modular shell, a uniform gas distribution mechanism, a fan-shaped detachable catalytic mechanism, a gas-driven rotary spray mechanism, and an umbrella-type airflow dispersion mechanism. This design achieves uniform distribution of methanol and water vapor from top to bottom, efficient catalytic reforming, and deep removal of residual methanol, suppressing impurity generation at the source, efficiently removing residual methanol, protecting the downstream PSA system, and simultaneously achieving 1000 Nm³ of hydrogen peroxide. 3 With its h-level hydrogen production, 5N-level high-purity hydrogen preparation, wide load adjustment, and long-term stable operation, it meets the high-quality hydrogen demand of high-end manufacturing fields such as nuclear power and stainless steel heat treatment.

[0029] like Figures 1-12 As shown, this invention provides a structure for a methanol reforming hydrogen production reactor with a capacity of 1,000 standard cubic meters. The structure comprises a first spliced ​​shell 1, a second spliced ​​shell 2, a third spliced ​​shell 3, and a fourth spliced ​​shell 4, connected end-to-end from bottom to top to form a cylindrical reaction chamber. Gas enters from the first spliced ​​shell 1 and exits from the fourth spliced ​​shell 4. A distribution mechanism 8 for dispersing methanol and water vapor is provided inside the first spliced ​​shell 1. A catalytic mechanism 7 is provided inside the second spliced ​​shell 2. The catalytic mechanism 7 reacts with the methanol and water vapor to generate hydrogen-rich conversion gas. A spray mechanism 5 and a dispersion mechanism 6 are installed vertically inside the third spliced ​​shell 3. After passing through the dispersion mechanism 6, the conversion gas comes into counter-current contact with the demineralized water output from the spray mechanism 5 to remove residual methanol.

[0030] Specifically, such as Figures 1-2As shown, the methanol reforming hydrogen production reactor disclosed in this invention has an overall vertical cylindrical cavity structure, consisting of a first splicing shell 1, a second splicing shell 2, a third splicing shell 3, and a fourth splicing shell 4 connected end to end from bottom to top. The reaction gas is input from the inlet pipe 12 of the first splicing shell 1, flows through the distribution mechanism 8, the catalytic mechanism 7, the dispersion mechanism 6, and the spray mechanism 5 in sequence, and finally discharges high-purity hydrogen-rich conversion gas from the outlet pipe 41 of the fourth splicing shell 4. The entire shell is designed in sections to facilitate the installation, maintenance, and catalyst replacement of internal components. Both the first splicing shell 1 and the third splicing shell 3 have manholes 32 or disassembly holes 21 to meet the needs of maintenance and component replacement.

[0031] like Figure 1 , Figure 3 , Figure 4 As shown, the housing adopts a segmented modular sealed assembly, which balances structural strength, ease of installation, and maintenance, specifically including: The bottom of the first splicing shell 1 is provided with a base 11, which serves as the overall support base for the reactor; an inlet pipe 12 and a manhole 32 are opened on the side wall. The inlet pipe 12 is a methanol water vapor inlet. The internal distribution mechanism 8 is installed in the first splicing shell 1 to achieve uniform dispersion of raw material gas.

[0032] The second splicing shell 2 is located above the first splicing shell, and the catalytic mechanism 7 is installed inside, which is the core cavity for methanol steam reforming reaction; the side wall has a disassembly hole 21, the size of which is larger than the inner diameter of the catalytic module 71, which is sealed with the filling plate 22 and the bonding plate 23 to realize the quick pull-out replacement of the catalytic module 71.

[0033] The third splicing shell 3 is located above the second splicing shell. Inside, a spraying mechanism 5 and a dispersion mechanism 6 are distributed vertically to complete the uniform dispersion of the conversion gas and the reverse spraying removal of residual methanol. A manhole 32 and a spray liquid pipe 31 are opened on the side wall, and the spray liquid pipe 31 is connected to the demineralized water supply system.

[0034] The top of the fourth splicing shell 4 is provided with an output pipe 41, which is the output port of high-purity hydrogen. The output pipe 41 contains the fan blades 531 of the spray mechanism 5. The output airflow drives the spray component 53 to rotate, achieving no external power drive.

[0035] like Figures 2-5 As shown, the distribution mechanism 8 is installed inside the first splicing shell 1, located above the inlet pipe 12 and below the manhole 32. Its function is to evenly disperse the input methanol water vapor onto the catalytic mechanism 7, avoiding uneven reaction and excessive impurities caused by local airflow concentration. Specifically, it includes: multiple frustum holes 82 are evenly distributed on the body of the second separator plate 81, with the lower diameter of the frustum hole being larger than the upper diameter, forming a gradually narrowing airflow channel to improve the uniformity of airflow distribution; the third support ring plate 83 is fixedly welded to the inner wall of the first splicing shell 1, providing detachable support for the second separator plate 81, facilitating disassembly, cleaning, and maintenance.

[0036] Methanol vapor enters the first splicing shell 1 through the inlet pipe 12, is evenly dispersed through the conical hole 82 of the distribution mechanism 8, and smoothly enters the catalytic mechanism 7 throughout the entire area, avoiding local flow deviation and achieving uniform gas distribution.

[0037] like Figure 2 , Figure 10 , Figure 11 , Figure 12 As shown, the catalytic mechanism 7 is installed inside the second splicing shell 2. The catalytic mechanism 7 is the core reaction component of this invention. The catalytic mechanism 7 includes: a support frame 72 providing stable support and positioning for the catalytic module 71, specifically including a vertical shaft 721, a support plate 725, a fixing plate 727, a clamping plate 726, a support plate 728, a tray 723, and a lower pressure ring 724. The vertical shaft 721 is connected to the support plate 725 at both ends, and the end of the support plate 725 is fixed to the inner wall of the second splicing shell 2 via the support plate 728, forming a central support frame. The fixing plate 727 and the clamping plate 726 are detachably connected, providing bearing rotation support for the vertical shaft 721 to ensure structural stability. The tray 723 and the lower pressure ring 724 clamp the catalytic module 71 from above and below, preventing the catalytic module from shaking and ensuring uniform airflow through the catalytic reaction zone. This design features high catalytic selectivity, detachable maintenance, and uniform airflow contact throughout the entire process, suppressing the generation of CO byproducts from the source. The catalyst module 71 has a fan-shaped modular structure with multiple groups evenly distributed around the vertical axis 721. It not only has good thermal conductivity but also allows for rapid replacement. Specifically, each group consists of a fan-shaped outer chamber 711 and a fan-shaped inner chamber 712. Both the inner and outer shells have openings 716 and vents 714 to ensure that methanol and water vapor can pass through smoothly and fully contact the catalyst. The outer wall of the fan-shaped inner chamber 712 has a pull-out groove 713, which, together with the disassembly hole 21 of the second splicing shell 2, can be pulled out directly from the outside of the shell without disassembling the entire reactor, greatly reducing maintenance downtime. The fan-shaped inner chamber is filled with a copper-based catalyst supported on boron nitride nanosheets (BNNS-OH) with hydroxyl-rich surfaces. The active components are CuO (55~65wt%) and ZnO (25~35wt%), and the support BNNS-OH accounts for about 10wt%. It is prepared by reverse co-precipitation method.

[0038] A uniform gas flow passes through the fan-shaped catalytic module 71, where a methanol steam reforming reaction occurs under the action of a highly selective catalyst. This process inhibits CO generation at the source and produces low-impurity, hydrogen-rich reformed gas, achieving highly efficient catalysis.

[0039] The catalyst bed in the reforming reaction chamber is filled with a BNNS-OH supported copper-based catalyst. The reaction temperature is 220~280℃. The methanol steam reforming reaction produces hydrogen-rich conversion gas, and the CO concentration in the conversion gas is controlled at 0.3%~0.6%. A snap-fit ​​post 715 is installed at the end of the fan-shaped outer chamber 711. The snap-fit ​​post 715 is located in the snap-fit ​​groove 722, which is set along the height direction of the vertical axis 721.

[0040] like Figure 2 , Figure 9 As shown, the dispersion mechanism 6 is located inside the third splicing shell 3, below the spray mechanism 5 and below the manhole 32. Its main function is to uniformly disperse the catalytically converted gas throughout the entire area, ensuring full counter-current contact with the sprayed demineralized water and improving the residual methanol removal efficiency.

[0041] Specifically, the second support ring plate 61 is fixedly welded to the inner wall of the third splicing shell 3 to provide support for the overall component; multiple vertical pipes 64 are evenly distributed above the first partition plate 63, and an umbrella shell 65 is set at the top of the vertical pipes 64. The umbrella shell 65 blocks the spray liquid from falling directly, forcing the converted gas to flow out evenly from the edge of the umbrella shell, forming a uniform gas layer throughout the area; an external drain pipe 62 is set at the bottom of the first partition plate 63 to discharge spray waste liquid and condensate.

[0042] The converted gas flows upward through the dispersion mechanism 6, and the umbrella shell 65 disperses the gas flow throughout the entire area, making full contact with the demineralized water from the rotating spray, deeply removing residual methanol, preventing PSA adsorbent poisoning, and achieving deep purification of the raw material.

[0043] like Figure 2 , Figure 6 , Figure 7 , Figure 8 As shown, the spraying mechanism 5 is installed inside the third splicing shell 3 and above the dispersion mechanism 6. Its main function is to remove residual methanol from the conversion gas through reverse spraying of demineralized water, protecting the downstream PSA adsorbent from poisoning. It adopts a gas-driven self-rotating design, eliminating the need for an external motor, thus saving energy and ensuring stable operation. Specifically, it includes: The bracket 51 provides rotational support and sealing positioning for the spray component 53, specifically including a first support ring plate 511, a horizontal plate 512, and a central tube 513: the first support ring plate 511 is fixed above the manhole 32 of the third splicing shell 3, and the horizontal plate 512 is detachably installed below it; the central tube 513 provides bearing rotational support for the main pipe 534 of the spray component 53, ensuring smooth rotation without leakage.

[0044] The spray unit 53 includes fan blades 531 distributed vertically, main pipe 534, and multiple spray pipe groups 533. Each spray pipe group 533 is divided into upper and lower layers, and the upper and lower spray pipe groups 533 are distributed in a cross pattern and are all connected to the main pipe 534. An end shaft 532 is installed on the top of the main pipe 534, and the end shaft 532 is connected to the central shaft of the fan blades 531 through a coupling.

[0045] The fan blade 531 is located inside the output pipe 41 of the fourth splicing shell 4. The high-speed airflow output from the reactor impacts the fan blade 531 to rotate, and drives the main pipe 534 and the spray pipe assembly 533 to rotate synchronously through the end shaft 532. It has no external power and is energy-saving and reliable. The spray pipe assembly 533 is divided into upper and lower layers and is distributed crosswise. It is connected to the main pipe 534 and achieves full-area spraying without dead corners when rotating. The side wall of the main pipe 534 has an air inlet 535 and a Chinese-shaped external pipe 52 is fitted on the outside. The external pipe 52 is connected to the spray liquid pipe 31 and is connected by a mechanical seal to ensure continuous supply of demineralized water without leakage.

[0046] The purified high-purity hydrogen is discharged from the output pipe 41. The airflow drives the fan blade 531 to rotate, which in turn drives the spray pipe group 533 to rotate and spray the entire area. It has no external motor, is energy-saving and stable, and realizes the self-driving spray function.

[0047] In this invention, all components in contact with the reactant gas are made of high-temperature resistant, corrosion-resistant, and carburized stainless steel, which is suitable for the high-temperature and corrosive conditions of methanol reforming to produce hydrogen and has a long service life. The catalytic module adopts a fan-shaped modular design, and a single module can be replaced individually if it fails, without having to stop the entire reactor and disassemble it, thus improving maintenance efficiency by more than 90%.

[0048] The reactor's hydrogen production capacity has been stably reached 1000 Nm³. 3 With a capacity of 1,000 cubic meters per hour, the hydrogen produced has a purity of ≥99.999% (5N grade), a total CO+CO2 content of ≤10ppm, an annual continuous operating time exceeding 8,000 hours, and a load adjustment range of 20% to 110%, fully meeting the stringent hydrogen requirements of high-end manufacturing fields such as nuclear power and stainless steel heat treatment.

[0049] The self-rotating spray mechanism requires no external power drive, utilizing the reactor's own output airflow for power, resulting in reduced energy consumption, noiseless operation, and an extremely low failure rate; the four-section splicing shell design significantly reduces transportation and installation difficulties, adapting to the needs of rapid deployment in industrial sites.

[0050] Furthermore, the technical solutions of the various embodiments of the present invention can be combined with each other. For example, a temperature sensor can be added to the catalytic module to achieve real-time monitoring, a flow regulating valve can be added to the spray liquid pipe to achieve precise control of the spray volume, and a flow equalization net can be added to the distribution mechanism to further improve the uniformity of gas distribution. However, this must be based on the ability of those skilled in the art to implement it. When the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such combination of technical solutions does not exist and is not within the scope of protection claimed by the present invention.

[0051] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these modifications and improvements all fall within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the appended claims.

Claims

1. A structure for a 1000-cubic-meter methanol reforming hydrogen production reactor, characterized in that, The system includes a first splicing shell (1), a second splicing shell (2), a third splicing shell (3), and a fourth splicing shell (4) connected end to end from bottom to top to form a cylindrical reaction chamber. Gas enters from the first splicing shell (1) and exits from the fourth splicing shell (4). A distribution mechanism (8) for dispersing methanol water vapor is provided in the first splicing shell (1). A catalytic mechanism (7) is provided on the inner side of the second splicing shell (2). The catalytic mechanism (7) reacts with methanol water vapor to generate hydrogen-rich conversion gas. A spraying mechanism (5) and a dispersion mechanism (6) are installed vertically in the third splicing shell (3). After the conversion gas passes through the dispersion mechanism (6), it comes into countercurrent contact with the demineralized water output by the spraying mechanism (5) to remove residual methanol. The catalytic mechanism (7) includes a support frame (72), which includes a vertical shaft (721) and support plates (725) distributed at the upper and lower ends of the vertical shaft (721). A fixing plate (727) is fixedly installed on the side of the two support plates (725) that are far apart from each other. A clamping plate (726) is detachably installed on the side of the fixing plate (727). The upper end of the vertical shaft (721) is connected by a bearing and extends into the space formed by the fixing plate (727) and the clamping plate (726). A support plate (728) is detachably installed at the end of each support plate (725), and the support plate (728) is fixed in the second splicing shell (2).

2. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 1, characterized in that, The catalytic mechanism (7) also includes multiple sets of catalytic modules (71) distributed on the outside of the vertical axis (721). The catalytic modules (71) are located between the tray (723) and the lower pressure ring (724). Each set of catalytic modules (71) includes a fan-shaped outer chamber (711) and a fan-shaped inner chamber (712). The arc surface of the fan-shaped outer chamber (711) and the top surface of the fan-shaped inner chamber (712) are both set as openings (716). Ventilation holes (714) are provided on the end faces of the fan-shaped outer chamber (711) and the fan-shaped inner chamber (712). Meanwhile, the fan-shaped inner chamber (712) is filled with a copper-based catalyst supported on boron nitride nanosheets with hydroxyl-rich surfaces.

3. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 2, characterized in that, A disassembly hole (21) is provided on the side wall of the second splicing shell (2), a filling plate (22) is provided at the disassembly hole (21), and an adhesive plate (23) is fixed on the outside of the filling plate (22). The adhesive plate (23) is detachably connected to the second splicing shell (2). The size of the disassembly hole (21) is larger than the size of the fan-shaped inner compartment (712), and the arc surface of the fan-shaped inner compartment (712) is provided with a pull-out groove (713).

4. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 3, characterized in that, The end of the fan-shaped outer compartment (711) is equipped with a snap-fit ​​post (715), which is located in a snap-fit ​​groove (722) and is set along the height direction of the vertical axis (721).

5. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 1, characterized in that, The distribution mechanism (8) comprises a second separation disc (81) and a third support ring plate (83) which are detachably connected up and down, a plurality of frustum-shaped holes (82) are evenly distributed on the second separation disc (81), the diameter of the lower end of each frustum-shaped hole (82) is larger than that of the upper end, and the third support ring plate (83) is fixedly installed in the first spliced shell (1), located above the inlet pipe (12) and simultaneously located below the manhole (32) of the first spliced shell (1).

6. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 1, characterized in that, The spray mechanism (5) comprises a spray member (53), and the spray member (53) comprises fan blades (531), a main pipe (534) and a plurality of spray pipe groups (533) which are distributed up and down; the plurality of spray pipe groups (533) are divided into an upper layer and a lower layer, the two layers of spray pipe groups (533) are distributed in a crossed manner and are both in communication connection with the main pipe (534); an end shaft (532) is installed at the top of the main pipe (534), and the end shaft (532) is connected with a central shaft of the fan blades (531) through a coupling.

7. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 6, characterized in that, The spray mechanism (5) further comprises a bracket (51), the bracket (51) comprises a first support ring plate (511) and a transverse plate (512), the transverse plate (512) is detachably installed below the first support ring plate (511), and the first support ring plate (511) is fixedly installed above the manhole (32) of the third spliced shell (3); the main pipe (534) is arranged to penetrate through a central pipe (513) of the transverse plate (512) through bearing connection.

8. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 7, characterized in that, Air inlet holes (35) are circumferentially distributed on the side wall of the main pipe (534), an external connecting pipe (52) is rotatably and mechanically seal-sleeved on the main pipe (534) at a position facing the air inlet holes (535), the external connecting pipe (52) is arranged in an I-shaped structure, and the middle part of the external connecting pipe (52) is in communication with a spray liquid pipe (31) arranged to penetrate through the spliced shell.

9. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 6, characterized in that, An output pipe (41) is installed at the top of the fourth spliced shell (4), the fan blades (531) are located in the output pipe (41), and gas flowing out from the output pipe (41) agitates the fan blades (531) to drive the plurality of spray pipe groups (533) to rotate.

10. The structure of a 1000-cubic-meter methanol reforming hydrogen production reactor according to claim 1, characterized in that, The dispersion mechanism (6) comprises a second support ring plate (61), a first separation disc (63) installed above the second support ring plate (61) and a plurality of vertical pipes (64) evenly installed on the first separation disc (63), an umbrella-shaped shell (65) is arranged at the top of each vertical pipe (64); the second support ring plate (61) is installed below the manhole (32) of the third spliced shell (3).

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