A hydrogen generation reaction chamber based on a honeycomb catalyst supported sodium borohydride

Abstract

This invention discloses a honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, belonging to the field of hydrogen production technology. The hydrogen production reaction chamber of this invention includes a reaction tank, a catalyst support mechanism, a solution distribution mechanism, and a temperature control mechanism. The reaction tank constructs an internal reaction space. The catalyst support mechanism houses catalyst units arranged in a honeycomb polygonal array, with each catalyst unit carrying the active catalyst component. The solution distribution mechanism is located in the upper space of the reaction tank, spraying sodium borohydride solution onto the catalyst units axially above the catalyst support mechanism. The temperature control mechanism controls the reaction temperature within the reaction tank between 30℃ and 80℃, with fluctuations controlled within ±2℃. This invention, by constructing a highly structured reaction field environment and controlling the reaction temperature through structural physics and precise closed-loop control, eliminates the "channeling" phenomenon and catalyst pulverization and loss problems of traditional sodium borohydride hydrogen production, greatly enhancing the gas-liquid-solid three-phase mass transfer efficiency.

Description

Technical Field

[0001] This invention relates to the field of hydrogen production technology, and more specifically to a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor. Background Technology

[0002] Hydrogen energy, as the most promising clean energy carrier of the 21st century, plays a central role in achieving the global energy structure transformation and carbon neutrality strategic goals. In the hydrogen energy industry chain, the safe storage and efficient transportation technologies for hydrogen are key barriers restricting its large-scale commercial application. Among numerous technological pathways, sodium borohydride (NaBH4) water electrolysis hydrogen production technology, due to its significant advantages such as high theoretical hydrogen storage density, high hydrogen purity, operation at room temperature and pressure, and environmentally friendly byproducts (sodium metaborate), shows great application potential in portable power sources, emergency power supplies, drones, and military individual portable equipment. This technology utilizes the exothermic reaction of sodium borohydride and water under the action of a catalyst to instantaneously output high-purity hydrogen, greatly simplifying the purification burden of the downstream fuel cell system.

[0003] Existing portable sodium borohydride hydrogen production devices mostly employ the conventional packed-bed reactor configuration found in traditional chemical engineering, where granular or fragmented catalysts are directly and randomly packed into a cylindrical cavity. Fluid distribution typically utilizes single-point nozzles or perforated plates for gravity spraying, while thermal management relies on cooling jackets on the reactor's outer wall or natural convection heat transfer. Under specific operating conditions of low power and discontinuous operation, this traditional structure can maintain basic hydrogen output functionality.

[0004] However, as application scenarios place increasingly stringent demands on hydrogen production power density, dynamic response speed, and system integration, existing reaction chamber structures based on random packed beds have revealed the following insurmountable technical shortcomings: First, the flow field distribution is mismatched, resulting in severe channeling and low mass transfer efficiency. The spatial topology of the randomly packed bed is uncontrollable, and the flow resistance within the bed varies significantly. The reaction solution tends to flow rapidly along low-resistance paths, leading to channeling and short-circuiting phenomena. This results in a large number of catalyst active sites remaining under-submerged for extended periods, leading to extremely low space utilization and a significant waste of high-value catalysts.

[0005] Second, the heat transfer is severely delayed, easily leading to localized "hot spots" and the risk of thermal runaway. Sodium borohydride hydrolysis is a strongly exothermic reaction (standard enthalpy change as high as -217 kJ / mol). Within the compact, portable structure, the instantaneous rate of heat accumulation far exceeds the heat transfer limit of traditional external heat exchange components. This superposition of conductive and convective thermal resistances makes it extremely easy for localized high temperatures to form inside the bed. According to the Arrhenius equation, localized temperature rises exponentially accelerate the chemical reaction rate, causing the system to fall into a vicious cycle of "temperature rise - reaction acceleration - further temperature rise," which not only shortens the thermal stability lifetime of the catalyst but also easily triggers serious safety hazards such as violent self-decomposition of the solution.

[0006] Third, the catalyst has poor mechanical stability and is prone to pulverization and loss, leading to system failure. Under the high flow rate required for high hydrogen production, the disordered catalyst particles will experience frequent mechanical friction and collisions, resulting in severe physical pulverization. Pulverization not only causes irreversible loss of active materials with the liquid flow and a significant decrease in hydrogen production performance, but the large number of micron-sized particles generated can also easily clog downstream pressure reducing valves, mass flow controllers, and filters, seriously threatening the reliability and service life of the entire unit.

[0007] In summary, the existing sodium borohydride hydrogen production reaction chamber structure has performance bottlenecks inherent in its physical structure, which are determined by its ability to enhance three-phase mass transfer, precisely control heat, and suppress catalyst pulverization and loss. Summary of the Invention

[0008] 1. The technical problem that the invention aims to solve To address the aforementioned problems in existing sodium borohydride hydrogen production technologies, this invention provides a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported structure. This chamber achieves synergistic control of mass transfer rate, heat transfer, and catalyst mechanical stability during sodium borohydride hydrolysis, thereby improving the power density, feed conversion rate, and reliability of continuous operation in hydrogen production.

[0009] 2. Technical Solution To achieve the above objectives, the technical solution provided by the present invention is as follows: A honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber includes a reaction tank, a catalyst support mechanism, a solution distribution mechanism, and a temperature control mechanism. The reaction tank constructs an internal reaction space. The catalyst support mechanism houses catalyst units arranged in a honeycomb polygonal array, with each catalyst unit carrying the active catalyst component. The solution distribution mechanism is located in the upper space of the reaction tank, spraying sodium borohydride solution onto the catalyst units axially above the catalyst support mechanism. The temperature control mechanism maintains the reaction temperature within the reaction tank between 30℃ and 80℃, with fluctuations controlled within ±2℃. By constructing a highly structured reaction environment and controlling the reaction temperature through structural physics and precise closed-loop control, the "channeling" phenomenon and catalyst pulverization and loss problems of traditional sodium borohydride hydrogen production are eliminated, greatly enhancing the gas-liquid-solid three-phase mass transfer efficiency. While achieving a highly compact and lightweight reaction chamber, the long-term stability and safety of the hydrogen production process are ensured.

[0010] Further, a honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber is developed. The catalyst support structure includes a central cylinder, a support bracket, and catalyst units. The central cylinder is fixedly connected to the inside of the reaction tank. The support bracket is fixedly connected to the inside of the central cylinder and has an axial through hole. The catalyst units are inserted into the through holes, and the active catalyst component inside is a cobalt-boron alloy. This achieves a honeycomb polygonal array arrangement of the catalyst units, constructs regular flow channels, eliminates "channeling" and "short circuit" phenomena, and reduces the flow velocity distribution non-uniformity (coefficient of variation, CV) to less than 10%. The hydrogen production rate is increased by about 40%, and the single-pass conversion rate of sodium borohydride can stably reach over 98.5%.

[0011] Further, a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support is proposed. The catalyst unit includes a three-dimensional network support and a catalyst active component loaded on its pore surface. The three-dimensional network support is a foamed nickel or porous ceramic material with a pore density of 60 to 100 pores / inch (PPI), which greatly increases the effective contact area of ​​the reaction.

[0012] Furthermore, a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support is developed. The three-dimensional mesh support has three-dimensional micropores with a cross-shaped cross section. The horizontal pores carry the active components of the catalyst, while the vertical pores serve as solution channels. This division of labor and cooperation not only compresses and fixes the catalyst but also does not affect the downward flow of the solution, fundamentally eliminating "channeling" and "short circuit".

[0013] Further, in the sodium borohydride hydrogen production reaction chamber supported by a honeycomb catalyst, the solution distribution mechanism includes a microporous sprayer and a spiral guide plate: the microporous sprayer is fixedly connected to the reaction tank body above the catalyst support mechanism; the spiral guide plate includes a central shaft and spiral blades fixedly connected to the shaft body, and the central shaft passes through the microporous sprayer and is rotatably connected to the top of the reaction tank body.

[0014] Furthermore, in the honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, the microporous sprayer includes micro-spray holes arrayed at its bottom; the solution ejected from the micro-spray holes is transformed into a rotating liquid film covering the top surface of the catalyst support mechanism after being guided by the spiral blades, which greatly enhances the wetting and spreading of the liquid phase on the catalyst surface.

[0015] Further, in the honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, the micro-spray orifice diameter is 0.5mm to 1.0mm, and the positions of all micro-spray orifices on the projection plane follow the Archimedes' spiral equation in spatial arrangement. The equation is: r = aθ, where r is the radial distance from the center of the micro-spray orifice to the central axis, θ is the rotation angle, and a is the spiral coefficient ranging from 0.5mm / rad to 2.0mm / rad. The distance between the spiral guide plate and the upper end face of the middle cylinder is 10mm to 30mm. The spiral lift angle of the spiral blades is set to 30° to 60°, and the axial height is 10mm to 25mm. The vertical distance from the nozzle end face of the micro-spray orifice to the top of the spiral guide plate is 15mm to 35mm. The jet with an initial velocity of 2m / s to 4m / s passes through the spiral blades, ensuring the formation of a rotating liquid film while ensuring a high degree of consistency in droplet flux.

[0016] Further, based on the honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, the temperature control mechanism is a three-layer sleeve integrated structure radially nested from the inside to the outside, including an inner cylinder reaction chamber inside the middle cylinder, a middle cylinder cooling chamber between the reaction tank and the middle cylinder, and an outer cylinder insulation chamber in the reaction tank interlayer; a radial annular gap is formed between the inner cylinder reaction chamber and the middle cylinder cooling chamber, and a spiral with a pitch of 20mm to 35mm is fixed in the annular gap to form a spiral condenser tube, and a regulating valve is set at the bottom opening of the spiral condenser tube.

[0017] Furthermore, in the honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, a temperature sensor and an ARM-based intelligent controller are fixed on the inner cylinder reaction chamber wall to lock the reaction temperature between 30℃ and 80℃ and control the fluctuation range within ±2℃.

[0018] Furthermore, in the honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, the intelligent controller is electrically connected to the temperature sensor and has a built-in proportional-integral-derivative control algorithm. Its control output function is: , in: This refers to the valve opening ratio. This is the temperature deviation value fed back by the temperature sensor. This is the proportionality coefficient. For integration time, For the differential time.

[0019] 3. Beneficial effects Compared with the prior art, the technical solution provided by this invention has the following advantages: (1) The honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber of the present invention significantly enhances the gas-liquid-solid three-phase mass transfer efficiency and improves the raw material conversion rate. By introducing a three-dimensional mesh support with high specific surface area and high porosity, the effective contact area of ​​the reaction is greatly increased; the honeycomb arrangement constructs regular flow channels, fundamentally eliminating the phenomena of "channeling" and "short circuit"; the flow velocity distribution non-uniformity (coefficient of variation CV) is less than 10%, the hydrogen production rate is increased by about 40%, and the single-pass conversion rate of sodium borohydride can be stably reached above 98.5%; a brand-new reaction chamber structure design is formed to achieve efficient fluid distribution, rapid reaction heat removal and stable catalyst structure in a very limited portable space; (2) The sodium borohydride hydrogen production reaction chamber based on the honeycomb catalyst support of the present invention achieves thermodynamic stability control and intrinsic safety of the reaction process; the three-layer sleeve spiral cooling channel significantly enhances turbulent kinetic energy, increasing the overall heat transfer coefficient K to 800-1000 W / (m²). 2 • K) level. Combined with high-precision PID closed-loop control, thermal balance reconstruction is completed within 30 seconds, effectively preventing the formation of local "hot spots" and catalyst sintering deactivation, eliminating safety hazards; (3) The sodium borohydride hydrogen production reaction chamber based on the honeycomb catalyst support of the present invention greatly extends the physical life of the catalyst and reduces the maintenance cost; the “unitized-structured” support mode eliminates the friction and collision between catalyst particles during operation, and inhibits pulverization and loss from the source; after 500 hours of continuous operation, the catalyst mass loss rate is less than 2% (10%-15% for traditional packed beds). (4) The sodium borohydride hydrogen production reaction chamber based on the honeycomb catalyst of the present invention achieves a highly compact and lightweight integration of the system; it completes the reconstruction of complex flow field and temperature field within a very small physical volume (diameter ≤120mm, height ≤220mm), and the overall weight is controlled below 5kg, which perfectly fits the field operation and individual soldier portable scenarios that are extremely sensitive to space and load. (5) The honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber of the present invention improves the system's adaptability to raw material fluctuations; the spiral guide plate and the Archimedes spiral microporous sprayer work together to ensure that the solution can still uniformly cover the bed in a swirling flow under inclined conditions; the hydrogen flow fluctuation coefficient is reduced to 3%-5%, providing a high-quality hydrogen source guarantee for the downstream fuel cell. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of an explosion in a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor, according to a specific embodiment. Figure 2This is a front view of a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported structure, according to a specific embodiment. Figure 3 This is a schematic diagram of a specific embodiment of a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support, hidden in the lower part of the reaction tank. Figure 4 This is a top cross-sectional view of a sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor, according to a specific embodiment. Figure 5 for Figure 4 An enlarged view of the upper part; Figure 6 A bottom view of the micro-spray nozzle arrangement of a micro-sprayer according to a specific embodiment; Figure 7 This is a top view of the catalyst support mechanism in a specific embodiment; Figure 8 This is a magnified cross-sectional view of the three-dimensional mesh micropores in the catalyst unit of a specific embodiment.

[0021] In the diagram: 1. Reaction vessel; 2. Catalyst support structure; 20. Middle cylinder; 21. Three-dimensional mesh carrier; 22. Support bracket; 23. Through hole; 24. Three-dimensional mesh micropores; 25. Catalyst unit; 3. Solution distribution mechanism; 31. Micro-orifice sprayer; 32. Spiral guide plate; 33. Micro-spray orifice; 34. Archimedes spiral; 4. Temperature control mechanism; 41. Inner cylinder reaction chamber; 42. Middle cylinder cooling chamber; 43. Outer cylinder insulation chamber; 44. Condenser pipe; 45. Regulating valve; 46. Fluororubber O-ring; 47. Flexible graphite gasket. Detailed Implementation

[0022] To further understand the content of this invention, a detailed description of the invention is provided in conjunction with the accompanying drawings.

[0023] Example This embodiment is based on a honeycomb catalyst-supported sodium borohydride hydrogen production reaction chamber, such as... Figure 1 , 2 As shown, the system includes a reaction vessel 1, a catalyst support mechanism 2 disposed inside the reaction vessel 1, a solution distribution mechanism 3 disposed axially above the catalyst support mechanism 2, and a temperature control mechanism 4 covering the radial outer periphery of the reaction vessel 1. The entire reaction vessel 1 has a diameter ≤120mm, a height ≤220mm, and an overall weight controlled to around 5kg. Through vertical integration, the hydrolysis reaction of sodium borohydride solution is confined within a highly ordered and controllable physical space, which is suitable for field operations and individual soldier portable scenarios where space and load are extremely sensitive.

[0024] In this embodiment, the reaction vessel 1, serving as the pressure-bearing and reaction body of the entire device, is made of 316L stainless steel with excellent corrosion resistance. The cavity undergoes precision boring and internal grinding processes to ensure its inner diameter is between 70mm and 80mm and its height is between 150mm and 170mm. To minimize the nucleation and retention of the hydrolysis product sodium metaborate (NaBO2) on the wall surface, the surface roughness Ra of the inner wall of the cavity is strictly controlled below 0.4μm. This mirror-like inner wall treatment, combined with the fluid dynamics design, effectively prevents the risk of flow channel blockage caused by the crystallization of reaction byproducts.

[0025] Inside the reaction vessel 1, the core functional component is the catalyst support mechanism 2; (refer to...) Figure 4 , 7 8. The mechanism comprises multiple cylindrical catalyst units 25 arranged in a geometrically regular pattern, and a support 22 for fixing the catalyst units 25. The catalyst units 25 are not traditional particle packing, but are composed of a three-dimensional network support 21 with high porosity and catalyst active components loaded on its pore surface. The three-dimensional network support 21 is preferably a foamed nickel or porous ceramic material with a pore density of 60 to 100 pores per inch (PPI) to provide an extremely high specific surface area (500 to 800 m²). 2 The catalyst unit 25 (cobalt-boron (Co-B)) maintains a porosity of 90% to 98%, forming a three-dimensional microporous network 24. The cross-section of the microporous network 24 is cross-shaped, with horizontal pores carrying the active catalyst component and vertical pores serving as solution channels. This division of labor ensures the catalyst is compressed and fixed without affecting the downstream flow of the solution. The active catalyst component is a cobalt-boron (Co-B) amorphous alloy, and its loading is precisely controlled at 15% to 20% of the total mass of the catalyst unit 25. In this embodiment, the diameter of the catalyst unit 25 is set to 15mm to 25mm, and the height is set to 20mm to 35mm to avoid severe internal diffusion resistance.

[0026] The support bracket 22 is made of polytetrafluoroethylene (PTFE) material with extremely high chemical stability. The bracket is CNC machined with 12 to 24 circular through holes 23 arranged in a honeycomb hexagonal array. The diameter of the circular through holes 23 is 0.3 mm to 1.0 mm larger than the diameter of the catalyst unit 25 to allow for thermal expansion gaps. The center distance L between two adjacent through holes 23 satisfies the geometric ratio relationship with the diameter D of the catalyst unit 25: L = (1.1-1.3)D. This spacing control forms a regular triangular flow channel with an equivalent diameter of 1.5 mm to 3.0 mm between adjacent catalyst units 25, limiting the overall physical porosity of the catalyst bed to 70% to 80% and completely eliminating the channeling phenomenon commonly found in traditional packed beds.

[0027] Above the catalyst support mechanism 2 is the solution distribution mechanism 3. For example... Figure 1 , 4 As shown in Figure 5, the mechanism includes a microporous sprayer 31 at the top and a spiral guide plate 32 at the bottom. Figure 6 As shown, the bottom array of the micro-orifice sprayer 31 has 50 to 200 micro-orifices 33, with an orifice diameter of 0.5 mm to 1.0 mm. The spatial arrangement of the micro-orifices 33 follows the Archimedean spiral equation 34: r = aθ. In this equation, r represents the radial distance, θ is the rotation angle, and a is the helical coefficient ranging from 0.5 mm / rad to 2.0 mm / rad. This array ensures a high degree of uniformity in droplet flux.

[0028] like Figure 4 , 5 As shown, a spiral guide plate 32 is installed 15mm to 35mm below the micro-orifice sprayer 31. This guide plate consists of 2 to 4 spiral blades with a spiral angle set to 30° to 60° and a blade height of 10mm to 25mm. When the solution in the micro-orifice 33 is ejected with an initial velocity of 2m / s to 4m / s, it generates a controlled swirling flow under the guidance of the spiral guide plate 3210, with a flow rate of 5L / (m 2 ·h) to 20L / (m 2 The spray density of ·h) forms a uniformly covered liquid film, which greatly enhances the wetting and spreading of the liquid phase on the catalyst surface.

[0029] like Figure 3 , 4 As shown, the temperature control mechanism 4 adopts a three-layer sleeve structure: an inner cylinder reaction chamber 41 within the middle cylinder 20, a middle cylinder cooling chamber 42 between the reaction tank 1 and the middle cylinder 20, and an outer cylinder insulation chamber 43 sandwiched between the reaction tank 1 and the reaction tank 1. The cooling chamber has a gap width of 8mm to 15mm and is internally fixed with a spiral guide condenser tube 44 with a pitch of 20mm to 35mm, forming a forced-constrained spiral cooling flow channel. A regulating valve 45 is installed at the bottom of the condenser tube 44, which significantly improves the Nusselt number (Nu) and convective heat transfer efficiency at the wall surface. The outer cylinder insulation chamber 43 is filled with a thermal conductivity less than The aerogel felt; a temperature sensor and an ARM-based intelligent controller are fixed to the wall of the inner reaction chamber 41; the intelligent controller is electrically connected to the temperature sensor and has a built-in proportional-integral-derivative control algorithm, and its control output function is: , in: This refers to the valve opening ratio. This is the temperature deviation value fed back by the temperature sensor. This is the proportionality coefficient. For integration time, This is the differential time. The integrated PT100 temperature sensor transmits the real-time temperature signal to the ARM intelligent controller; the controller runs a PID control algorithm to calculate the real-time temperature deviation according to the formula. Its integral and differential terms, dynamically adjusting the regulating valve opening by 45 degrees, lock the reaction temperature fluctuation range within ±2℃, thereby increasing the overall heat transfer coefficient K to 800-1000W / (m²). 2 • K) level. Combined with high-precision PID closed-loop control, thermal balance reconstruction is completed within 30 seconds, effectively preventing the formation of local "hot spots" and catalyst sintering deactivation, eliminating safety hazards.

[0030] In terms of overall mechanical assembly, a modular design concept is adopted. Standardized flange connections are used at the interfaces of each module (3 modules of solution distribution mechanism, 2 modules of catalyst support mechanism, 1 module of reaction chamber of reaction tank, gas-liquid separation module, and temperature control module), and are coordinated with... Figure 4 The double sealing pair formed by the fluororubber O-ring 46 and the flexible graphite gasket 47 shown is convenient for independent disassembly and maintenance in the later stage.

[0031] To further quantify the technical effects of the present invention, the following specific embodiments and comparative examples are used for data demonstration: Example 1 The above-described structure is adopted in this embodiment. The reaction chamber 1 has an inner diameter of 75 mm and a height of 160 mm. The catalyst support structure 2 contains 19 catalyst units 25 (unit diameter 20 mm, 80 PPI nickel foam support, 18% Co-B loading). The center distance L = 24 mm (i.e., 1.2D). The microporous sprayer 31 has 120 micropores (Archimedean spiral 34 arranged). The temperature control system is set to 60°C.

[0032] Example 2 The basic structure is the same as in Example 1, but the catalyst unit 25 uses a 100PPI porous ceramic carrier with a loading of 20%, and the spiral guide plate 32 has a spiral angle of 45°.

[0033] Comparative Example 1 A conventional random packed bed reactor is used, in which an equal amount of 3mm diameter granular Co-B catalyst is directly and randomly filled inside, and injected using a common single-hole nozzle.

[0034] All samples were tested under standard operating conditions (NaBH4 concentration 15wt%, solution flow rate 50mL / min) for 500 hours of continuous operation. The results are shown in Table 1. Table 1: Performance Comparison Table of Embodiments and Comparative Examples of the Invention

[0035] Data Analysis: 1. Conversion Rate and Mass Transfer: The conversion rates of all examples exceeded 98.5%, the hydrogen production rate increased by approximately 40%, and the coefficient of variation (CV) of the flow velocity distribution was only 6.5% to 7.8% (compared to 32.4% in the comparative example). This directly demonstrates that the honeycomb support system and the Archimedes spiral 34-micropore distributor completely eliminated fluid dead zones and channeling.

[0036] 2. Thermal control stability: Based on the spiral cooling channel and PID algorithm, the temperature fluctuation in the embodiment is controlled within 1.2℃ (comparative example is 8.5℃), which greatly suppresses the pulsation of gas-liquid two-phase flow and eliminates the risk of local hot spots and system overpressure.

[0037] 3. Durability: After 500 hours, the catalyst loss rate of the example was less than 1.5%, which was much lower than the 14.8% of the comparative example, proving that the physical constraint of "unitization-structuring" effectively prevented the catalyst particles from being washed away and pulverized.

[0038] 4. Lightweight: Through the 316L thin-wall design and the application of PTFE bracket, the overall weight is reduced to less than 5kg (only 4.6kg in Example 1), achieving extremely high power density.

[0039] In summary, this invention successfully solved the mass and heat transfer bottleneck in the sodium borohydride hydrolysis process by systematically reconstructing the flow field, temperature field, and catalyst mechanical structure within the reaction chamber, thus constructing an efficient, stable, and long-life intrinsically safe hydrogen production environment.

[0040] The present invention and its embodiments have been described above illustratively. This description is not restrictive, and the figures shown are only one embodiment of the present invention. The actual structure and manufacturing steps are not limited thereto. Therefore, if those skilled in the art are inspired by this description and design similar structures and embodiments without departing from the spirit of the present invention, such designs should fall within the protection scope of the present invention.

Claims

1. A sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor, characterized in that, include: The reaction vessel, which forms the internal reaction space; The catalyst support structure has a built-in honeycomb polygonal array of catalyst units, and the catalyst active components are carried within the catalyst units; A solution distribution mechanism is located axially above the catalyst support mechanism to spray sodium borohydride solution onto the catalyst unit. The temperature control mechanism controls the reaction temperature inside the reaction vessel between 30℃ and 80℃, with fluctuations controlled within ±2℃.

2. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor according to claim 1, characterized in that: The catalyst support structure includes: The middle cylinder is fixedly connected inside the reaction vessel; The support bracket is fixedly connected to the inside of the middle cylinder and has an axial through hole; The catalyst unit is inserted into the through hole, and the active catalyst component inside is a cobalt-boron alloy.

3. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support according to claim 2, characterized in that: The catalyst unit includes a three-dimensional network support and a catalyst active component supported on its pore surface.

4. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor according to claim 3, characterized in that: The three-dimensional mesh carrier has three-dimensional micropores in its inner mesh. The cross-section of the three-dimensional micropores is cross-shaped. The horizontal pores carry the active components of the catalyst, and the vertical pores are solution channels.

5. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support according to claim 3, characterized in that: The solution dispensing mechanism includes: The microporous sprayer is fixedly connected to the reaction tank above the catalyst support mechanism; The spiral guide plate includes a central shaft and spiral blades fixedly connected to the shaft body. The central shaft passes through the microporous sprayer and is rotatably connected to the top of the reaction tank.

6. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support according to claim 5, characterized in that: The micro-orifice sprayer includes micro-orifices distributed in an array at its bottom; The solution ejected from the micro-jet nozzle is transformed into a rotating liquid film covering the top surface of the catalyst support mechanism after being guided by the spiral blades.

7. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor according to claim 6, characterized in that: The diameter of the micro-spray orifice is 0.5mm to 1.0mm, and the positions of all micro-spray orifices on the projection plane are arranged spatially according to the Archimedes spiral equation, which is: r=aθ, where r is the radial distance from the center of the micro-spray orifice to the central axis, θ is the rotation angle, and a is the spiral coefficient ranging from 0.5mm / rad to 2.0mm / rad. The distance between the spiral guide plate and the upper end face of the middle cylinder is 10mm to 30mm; the spiral lift angle of the spiral blade is set to 30° to 60°, and the axial height is 10mm to 25mm; the vertical distance from the nozzle end face of the micro-spray orifice to the top of the spiral guide plate is 15mm to 35mm, and the jet is made to pass through the spiral blade with an initial velocity of 2m / s to 4m / s.

8. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support according to claim 6, characterized in that: The temperature control mechanism is a three-layer sleeve-type integrated structure that is radially nested from the inside to the outside, including: The inner reaction chamber inside the middle cylinder; The intermediate cylinder cooling chamber between the reaction vessel body and the intermediate cylinder; and, The outer insulation cavity of the reaction vessel body jacket; A radial annular gap is formed between the inner cylinder reaction chamber and the middle cylinder cooling chamber. A spiral with a pitch of 20mm to 35mm is fixed in the annular gap to form a spiral condenser tube. A regulating valve is installed at the bottom opening of the spiral condenser tube.

9. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst-supported reactor according to claim 8, characterized in that: The inner cylinder reaction chamber wall is fixed with a temperature sensor and an ARM-based intelligent controller, which is used to lock the reaction temperature between 30℃ and 80℃ and control the fluctuation range within ±2℃.

10. The sodium borohydride hydrogen production reaction chamber based on a honeycomb catalyst support according to claim 8, characterized in that: The intelligent controller is electrically connected to the temperature sensor and has a built-in proportional-integral-derivative control algorithm. Its control output function is: ， in: This refers to the valve opening ratio. This is the temperature deviation value fed back by the temperature sensor. This is the proportionality coefficient. For integration time, For the differential time.

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