Reaction apparatus

Abstract

This invention provides a reaction apparatus comprising: two inlet sections, a feed section, a cylindrical section, a palladium membrane tube, a hydrogen collection tube, and a waste liquid recovery tube. Through the combined effects of eddy current and centrifugal force, along with the palladium membrane, it effectively promotes the hydrogen production reaction efficiency, rapidly and accurately separates hydrogen and the byproduct sodium metaborate, and effectively and selectively collects hydrogen for utilization.

Description

Technical Field

[0001] This invention relates to a reaction apparatus capable of continuous feeding and utilizing centrifugal force to generate eddies for reaction. In particular, it is a hydrogen production reaction apparatus that uses centrifugal force to separate the hydrogen gas generated by the reaction towards the center of the apparatus, while byproducts such as gels move towards the outer shell of the apparatus, and the hydrogen gas is screened out through a palladium membrane tube disposed on the center of the apparatus. Prior Technology

[0002] Sodium borohydride (NaBH₄) is an inorganic compound, a white powder that readily absorbs moisture and deliquesces. It is soluble in water and lower alcohols and undergoes hydrolysis to produce hydrogen gas. Generally, chemical reactions involving the products are carried out in a reaction vessel with controlled parameters. However, when using a pump to transfer an aqueous solution of sodium borohydride to the catalyst bed within the reaction vessel, the high viscosity of the solution makes it difficult to accurately extract the required amount. To address this issue, non-reactive chemicals are sometimes added to reduce viscosity, but this also reduces reactivity.

[0003] On the other hand, the hydrolysis of sodium borohydride produces sodium metaborate (NaBO 4), a byproduct that must be removed. Sodium metaborate tends to gain water and form a gel when cooled, which hinders the approach of the catalyst, reduces efficiency, makes it difficult to utilize the water required for the reaction, and makes it difficult to separate the product hydrogen from the byproduct sodium metaborate, thus making hydrogen collection difficult. Summary of the Invention

[0004] [The technical problem that the invention aims to solve] In view of the prior art, when sodium borohydride aqueous solution is subjected to hydrolysis to produce hydrogen in a reaction tank, it is usually necessary to add non-reactive chemical substances to reduce the viscosity of the sodium borohydride aqueous solution, but at the same time reduce the reactivity; and during the hydrolysis reaction of sodium borohydride, it is necessary to effectively separate the by-product sodium metaborate, otherwise it will affect the hydrolysis to produce hydrogen from the sodium borohydride aqueous solution and make it difficult to collect and utilize the product hydrogen.

[0005] Therefore, the present invention provides a hydrogen production reaction device that can effectively promote the hydrogen production reaction, quickly and accurately separate the product hydrogen and the byproduct sodium metaborate, and effectively and selectively collect the product hydrogen.

[0006] [Technical means] In order to solve the above-mentioned problems, after in-depth research, the present invention provides a hydrogen production reaction device, which can effectively solve the problems of poor reactivity caused by excessively high viscosity of sodium borohydride aqueous solution, and the need to separate by-products to avoid affecting the reaction rate and hydrogen collection.

[0007] Specifically, the hydrogen production reactor of the present invention comprises: two inlet sections, a feed section, a cylindrical section, a palladium membrane tube, a hydrogen collection tube, and a waste liquid recovery tube.

[0008] The reactants are injected and mixed through two inlets before being fed into the feed section. The feed section injects the reactants upwards from the bottom of the cylindrical section. Accordingly, a hydrogen collection pipe can be installed at the top of the cylindrical section. The feed section and the hydrogen collection pipe are symmetrically fixed to the top and bottom of the cylindrical section using fixed bearings, ensuring a stable connection between the cylindrical section and the feed section and the hydrogen collection pipe during rotation, and maintaining a simple and straightforward structural design. Furthermore, installing the hydrogen collection pipe at the top of the cylindrical section facilitates the collection of the upward-flowing product gas, hydrogen. A palladium membrane tube is connected to the hydrogen collection pipe and fixed to the center of the cylindrical section to filter the product hydrogen; a waste liquid recovery pipe is located at the bottom of the cylindrical section to discharge byproducts such as gel and the reacted catalyst.

[0009] In this invention, the cylindrical section is designed to rotate as a whole at a speed of 500-3000 rpm, and more preferably 600-2500 rpm, and even more preferably 1000-2000 rpm, to generate a vortex effect. The rotation of the cylindrical section generates vortices, increasing the fluidity of the solution, enhancing the collision opportunities of reactants, and thus promoting the hydrogen production reaction.

[0010] The rotation of the cylindrical section generates centrifugal force, causing the lighter product gas, hydrogen, to move towards and enter the palladium membrane tube at the center of the cylindrical section, while the heavier byproducts, such as gel and the reacted catalyst, move towards the outer shell of the cylindrical section for separation. Hydrogen enters the palladium membrane tube through the palladium membrane on the palladium membrane tube and is collected using a hydrogen collection tube. The byproducts and the reacted catalyst are separated and flow out through a waste liquid recovery tube located on the lower side of the cylindrical section by the vortex.

[0011] Furthermore, to better separate byproducts, catalyst, and product hydrogen, the cylindrical section is designed as a single-piece shape consisting of a cylinder and a truncated cone. The truncated cone is a downwardly tapered structure with an angle of inclination between the extended straight line of the cylindrical sidewall and the sidewall of the truncated cone, ranging from 0 to 15 degrees. The ratio of the height L of the truncated cone to the total height H of the truncated cone and the cylinder, L / H, is between 0.1 and 0.5. When the inclination angle is greater than 0 degrees, the centrifugal force at the bottom of the cylindrical section is less than at the top, making it easier for byproducts and the reacted catalyst to be discharged from the waste liquid recovery pipe below. However, when the inclination angle is greater than 15 degrees, the centrifugal force at the bottom of the cylindrical section will be too small, causing byproducts and the reacted catalyst to easily get stuck at the feed section. When the ratio L / H is between 0.1 and 0.5, the centrifugal force at the bottom of the cylindrical section will be such that byproducts and reacted catalysts can be more easily discharged from the waste liquid recovery pipe below, and the centrifugal force will not be too small, causing byproducts and reacted catalysts to get stuck at the feed section.

[0012] Furthermore, a temperature regulating mechanism can be installed at the bottom of the cylindrical section to promote the separation and outflow of by-products and the reacted catalyst from the waste liquid recovery pipe through temperature control.

[0013] Furthermore, the feed section is designed to extend radially into the cylindrical section, allowing reactants to be injected at different radii within the cylindrical section, thus enabling the reactants to enter the cylindrical section from different positions. Since the centrifugal force varies with radius, adjusting the feed location at different radii within the cylindrical section, based on the viscosity and concentration characteristics of the reactants, can promote the separation of products and byproducts after the reaction. Specifically, adjusting the ratio of the straight-line distance *r* between the feed section opening and the center of the cylindrical section to the radius *R* of the cylindrical section can promote the separation of products and byproducts after the reaction. In one embodiment of the present invention, a separation effect is better when the *r* / *R* ratio is 0.1 to 0.9, more preferably 0.2 to 0.8, and even more preferably 0.4 to 0.7.

[0014] Furthermore, the present invention can be continuously fed from two inlets, thereby continuously generating hydrogen gas for use.

[0015] Furthermore, the waste liquid recovery pipe can be automatically switched on and off by remote control with a timer. The switching time is set according to the degree of reaction. After the reaction is completed, it is opened to discharge the catalyst and by-products after the reaction and then closed. During the process, the cylindrical part continues to rotate, so the reaction continues.

[0016] Furthermore, this invention achieves a hydrogen purification rate of 99.999% by using a palladium membrane sieve on a palladium membrane tube. The palladium membrane tube can be a waterproof and breathable tube, which can prevent the solution from entering the palladium membrane tube and effectively separate the product hydrogen.

[0017] Furthermore, the palladium membrane tube can be a palladium alloy membrane tube, such as a palladium membrane or palladium alloy membrane prepared using porous stainless steel as a carrier, which absorbs hydrogen gas through its chemical properties to improve the efficiency of hydrogen separation. Alternatively, the palladium membrane tube can also be made of metal powder or a microporous structure sintered from activated carbon, which can also promote the hydrogen production reaction.

[0018] Furthermore, a catalyst can be disposed on the palladium film of the palladium film tube. The catalyst is selected from transition metals in groups IB-VIIB and VIIIB of the periodic table, thereby achieving the effect of accelerating the reaction.

[0019] In addition, the reactants may include a borohydride solution and a catalyst aqueous solution, and the product of the reaction is hydrogen gas. The borohydride solution and the catalyst aqueous solution may be designed to be injected from the first inlet and the second inlet of the two inlets, and mixed before entering the feed section, and then injected into the cylindrical section for reaction.

[0020] Furthermore, the borohydride solution contains a borohydride at a concentration of 1-60 wt% of the total borohydride solution, preferably 20-40 wt%.

[0021] Furthermore, the viscosity of the borohydride solution is 1~300 cp (centipoise), preferably 10~150 cp, and more preferably 20~80 cp. The concentration and viscosity of the borohydride solution used in this invention can have a wide range because the hydrogen production reaction device in this invention can inject reactants at different radii in the cylindrical section. Different radii will generate different centrifugal forces when the cylindrical section rotates. Therefore, the feed position can be adjusted according to the concentration and viscosity of the borohydride solution used to promote a more complete reaction.

[0022] Furthermore, the borohydride solution contains a hydroxide at a concentration of 1-15 wt% in the total borohydride solution, which can accelerate the reaction.

[0023] Furthermore, the borohydride solution contains an aqueous solution of sodium borohydride, or a solution containing a mixture of sodium borohydride and methanol.

[0024] Furthermore, the catalyst contained in the aqueous catalyst solution is selected from transition metals in groups IB-VIIB and VIIIB of the periodic table, particularly transition metals such as rhodium, copper, cobalt, iron, nickel, manganese, ruthenium, rhenium, platinum, palladium, chromium, silver, osmium, or iridium, and the particle size of the transition metal is between 1 and 10,000 μm. By selecting a transition metal as a catalyst, the reaction can be accelerated; and by limiting the particle size of the transition metal, the recycling application of this invention can be facilitated. The concentration of the aqueous catalyst solution can be 0.1-10 wt%; by adjusting the concentration of the aqueous catalyst solution, the efficiency of the hydrogen production reaction can be changed.

[0025] Furthermore, the hydrogen production reaction apparatus of the present invention may include a first electric field element and a second electric field element. The first electric field element is disposed in the cylindrical part, and the second electric field element is disposed in the palladium membrane tube. This design enables an electric field to be generated between the first electric field element and the second electric field element, so that the products generated after the reaction of the reactants are affected by the electric field and the by-products are separated more quickly.

[0026] Furthermore, the first electric field element can be a ring-shaped electrode plate, and the second electric field element can be a strip-shaped electrode rod, thereby enhancing the generated electric field and its stability.

[0027] Furthermore, the first electric field element can be an anode, and the second electric field element can be a cathode. Based on this, water can be electrolyzed so that hydrogen gas is generated at the cathode and quickly absorbed by the palladium membrane tube, thereby promoting the continuous reaction. [Effects of the Invention]

[0028] The hydrogen production reaction apparatus of the present invention can effectively improve the reaction efficiency of hydrogen production, quickly and accurately separate the product hydrogen gas and by-products such as sodium metaborate and catalyst, and more effectively and selectively collect hydrogen gas for utilization.

[0029] This invention, through the combined effects of eddy current and centrifugal force, along with the addition of a palladium membrane, not only improves the reaction rate but also effectively separates byproducts and hydrogen, demonstrating high practicality and industrial applicability. Simple Explanation of the Diagram

[0030] [Figure 1] is a diagram of one embodiment of the hydrogen production reaction device of the present invention. [Figure 2] is a diagram of one embodiment of the hydrogen production reaction device of the present invention. Implementation

[0031] The hydrogen production reactor of the present invention will now be described in detail using embodiments, examples, and reference drawings. However, the embodiments and examples are not intended to limit the scope of the present invention, and any implementation that does not depart from the intent of the present invention should also be considered within the scope of the present invention.

[0032] [Implementation Method 1]

[0033] Figure 1 is a schematic diagram of the hydrogen production reactor 8 according to an embodiment of the present invention. The hydrogen production reactor 8 includes a first inlet 1 with two inlets, a second inlet 2, a feed section 3, a cylindrical section 4, a palladium membrane tube 5, a hydrogen collection tube 6, and a waste liquid recovery tube 7. In the hydrogen production reactor 8, the reactants undergo chemical and electrolytic water electrolysis to produce hydrogen in the cylindrical section 4. Through the combined effect of eddy current and centrifugal force, along with the palladium membrane, the reaction efficiency of hydrogen production is effectively promoted, and hydrogen and the byproduct sodium metaborate can be separated quickly and accurately, with highly selective collection of the generated hydrogen.

[0034] The hydrogen production reactor 8 of this invention utilizes the injection of reactants into a cylindrical section 4 via a feed section 3. Rotating the cylindrical section 4 causes the reactants within it to rotate, generating a vortex that increases the fluidity of the solution and enhances the collision opportunities of the reactants, thereby promoting a hydrolysis reaction within the cylindrical section 4 to produce hydrogen gas. Furthermore, the rotation of the cylindrical section 4 also generates centrifugal force, causing the product hydrogen gas to move towards the palladium membrane tube 5 located at the center of the cylindrical section 4, while the reaction byproducts, sodium metaborate gel and the reacted catalyst, move towards the outer shell of the cylindrical section 4, separating them from each other. Finally, the product hydrogen gas is filtered through the palladium membrane tube 5 into the hydrogen collection tube 6, and the byproducts, sodium metaborate gel and the reacted catalyst, are discharged through the waste liquid recovery tube 7, maintaining the reaction stability within the cylindrical section 4.

[0035] [Example 1]

[0036] Specifically, one embodiment of the hydrogen production reactor 8 is shown in Figure 1. The feed section 3 and the hydrogen collection pipe 6 are symmetrically fixed to the lower and upper parts of the cylindrical section 4 respectively using fixed bearings (not shown). This ensures a stable connection between the cylindrical section 4 and the feed section 3 and the hydrogen collection pipe 6 when the cylindrical section 4 rotates, and the structural design is simple and straightforward. Furthermore, the hydrogen collection pipe 6 is installed at the upper part of the cylindrical section 4 to continuously and conveniently collect the upward-flowing product gas hydrogen.

[0037] In this embodiment, the reactants for hydrogen production are a borohydride solution (not shown) and a catalyst aqueous solution (not shown). The two are introduced into the first inlet 1 and the second inlet 2 respectively and pre-mixed, and then introduced into the cylindrical section 8 through the feed section 3 to react and generate hydrogen gas.

[0038] The borohydride solution of the reactants is a sodium borohydride solution or a potassium borohydride solution, but is not limited to these; it can also be a metal hydride solution. Furthermore, the borohydride solution used in this embodiment contains a borohydride, such as sodium borohydride or potassium borohydride, with a concentration of 1-60 wt%, ideally 20-40 wt%. In addition, the borohydride solution may also contain a hydroxide, such as sodium hydroxide or potassium hydroxide, with a concentration of 1-15 wt%.

[0039] The catalyst aqueous solution contains a catalyst selected from transition metals in groups IB-VIIB and VIIIB of the periodic table, such as rhodium, copper, cobalt, iron, nickel, manganese, ruthenium, rhenium, platinum, palladium, chromium, silver, osmium, or iridium (overplated metals). The particle size of the catalyst is between 1 and 10,000 μm, ideally between 1 and 50 μm. The concentration of the catalyst aqueous solution is 0.1 to 10 wt%. By adjusting the particle density and size of the catalyst, the catalyst can be smoothly discharged from the waste liquid recovery pipe 7, thereby facilitating recycling and reuse. By adjusting the concentration of the catalyst aqueous solution, the efficiency of the hydrogen production reaction can be changed.

[0040] The hydrogen production reactor 8 in this embodiment produces hydrogen gas using a borohydride solution of reactants and an aqueous catalyst solution as follows: In this embodiment, the feed section 3 is configured to connect the first inlet section 1 and the second inlet section 2. The reactants entering the first inlet section 1 and the second inlet section 2 are first mixed before being injected into the feed section 3, thereby ensuring that the reactants are mixed evenly before the reaction takes place.

[0041] Next, the feed is introduced into the space contained in the cylindrical section 4 through the feed section 3, where a hydrolysis reaction occurs to produce hydrogen gas. Although in this embodiment the feed section 3 is introduced into the cylindrical section 4 through an opening at the tail end, in other embodiments, the arrangement of the feed section 3 can be varied, for example, the tail end can be closed and openings can be made at other parts of the feed section 3 pipeline. In addition, the radius r of the feed section 3 can be adjusted, for example, by adjusting the length of the feed section 3 in the radial direction of the cylindrical section 4, or by setting openings at different positions of the feed section 3 and injecting reactants through openings at different radii, so that the feed enters the cylindrical section 4 from different positions. Since centrifugal force acts in the r direction, adjusting the value of r can better promote the separation of substances after the reaction. The ratio r / R of r to the radius R of the cylindrical section 4 is preferably between 0.1 and 0.9, which can ensure better separation effect.

[0042] Furthermore, to ensure effective separation of byproducts, catalyst, and product hydrogen, the cylindrical section 4 in this embodiment is integrally formed by connecting a cylinder and a truncated cone. The truncated cone portion has a downwardly tapered structure with an angle θ between the extended straight line of the cylindrical sidewall and the sidewall of the truncated cone, where θ is 0~15 degrees, and the ratio L / H of the height L of the truncated cone to the total height H of the truncated cone and the cylinder is between 0.1 and 0.5. When θ is greater than 0 degrees, the centrifugal force at the bottom of the cylindrical section 4 is less than that at the top, making it easier for byproducts and the reacted catalyst to be discharged from the waste liquid recovery pipe 7 below. However, when θ is greater than 15 degrees, the centrifugal force at the bottom of the cylindrical section 4 will be too small, causing byproducts and the reacted catalyst to easily get stuck near the feed section 3 pipeline. When the ratio L / H is between 0.1 and 0.5, the centrifugal force at the bottom of the cylindrical section 4 will be such that byproducts and reacted catalysts can be more easily discharged from the waste liquid recovery pipe 7 below, and the centrifugal force will not be too small to cause byproducts and reacted catalysts to get stuck near the feed section 3 pipeline.

[0043] The hydrogen production reactor 8 of the present invention can be continuously fed into the first inlet 1 and the second inlet 2, thereby continuously producing hydrogen through the reaction.

[0044] When the borohydride solution and catalyst aqueous solution are introduced into the cylindrical section 4 via pipelines from the first inlet 1 and the second inlet 2, mixed evenly, and then injected into the cylindrical section 4 from the feed section 3, the rotation of the cylindrical section 4 causes the mixture of borohydride solution and catalyst aqueous solution inside the cylindrical section 4 to rotate, generating eddies. This increases the fluidity of the mixed solution, enhances the collision opportunities of the reactants, and thus promotes the hydrogen production reaction. The cylindrical section rotates as a whole at a speed of 500~3000 rpm. This generates larger eddies, increasing the fluidity of the solution, enhancing the collision opportunities of the reactants, and thus promoting the hydrogen production reaction.

[0045] In addition to promoting the reaction through eddy currents, the rotation of the cylindrical section 4 also generates centrifugal force. This centrifugal force causes the product hydrogen gas to move towards the palladium membrane tube 5 at the center of the cylindrical section 4, while the reaction byproducts sodium metaborate gel and the catalyst after the reaction move towards the outer shell of the cylindrical section 4. This is because the heavier sodium metaborate gel and catalyst are more affected by centrifugal force, while hydrogen gas is less affected. As a result, the product and byproduct flow in opposite directions, thus achieving separation.

[0046] After hydrogen is separated from sodium metaborate gel and catalyst, it is screened out through palladium membrane tube 5 to obtain product hydrogen. Palladium membrane tube 5 is located at the center of cylindrical section 4 and is absorbed by the palladium membrane on palladium membrane tube 5. In this embodiment, palladium membrane tube 5 is made of porous stainless steel and covered with palladium membrane and palladium alloy membrane. Its chemical properties can absorb hydrogen, thereby improving the efficiency of hydrogen separation. In addition, a catalyst formed by vapor deposition or electroplating can be further disposed on palladium membrane. Therefore, when the borohydride solution of reactants and the catalyst aqueous solution enter cylindrical section 4 from feed section 3 and come into contact with palladium membrane tube 5, they are immediately catalyzed by the catalyst on palladium membrane tube 5 to produce hydrogen, thereby improving the efficiency of hydrogen production reaction. Furthermore, the hydrogen entering palladium membrane tube 5 through palladium membrane is continuously collected by hydrogen collection tube 6 connected to palladium membrane tube 5, thereby ensuring a continuous supply of hydrogen.

[0047] Furthermore, the sodium metaborate gel thrown towards the outer wall of the cylindrical section 4 by centrifugal force, and the catalyst after the reaction, will sink to the bottom of the cylindrical section 4 due to gravity, and be discharged in liquid form through the waste liquid recovery pipe 7 located below the cylindrical section 4 for recycling. Since the by-products and the catalyst after the reaction will not remain in the cylindrical section 4, the present invention can better ensure the stability of the reaction compared to the negative impact of by-products on the reaction in the prior art. In addition, in this embodiment, the waste liquid recovery pipe 7 is set to be automatically switched on and off by remote control with a timer, which discharges the catalyst and by-products after the reaction at regular intervals and then closes the pipe. Throughout the process, the cylindrical section 4 continues to rotate to carry out the reaction, thereby ensuring that the reaction continues and hydrogen is continuously produced.

[0048] [Implementation Method 2]

[0049] Similar to the configuration in Embodiment 1, an outer frame 9 is further provided outside the cylindrical part 4 to receive the catalyst and by-products discharged from the waste liquid recovery pipe 7 after the reaction.

[0050] [Example 2]

[0051] As shown in Figure 2, the hydrogen production reactor 8 of Example 2 is configured similarly to that of Example 1. An outer frame 9 is further provided outside the cylindrical section 4. The outer frame 9 is fixed to the pipeline of the first inlet section 1 or the second inlet section 2 and remains stationary when the cylindrical section 4 rotates. The outer frame 9 collects the reactant and byproducts discharged from the waste liquid recovery pipe 7. The outer frame 9 is not connected to the pipelines of the two inlets, but an opening can be provided on the outer frame 9 to remove the reactant and byproducts, filter them, and then reinject the still-reacting catalyst into the first inlet section 1 or the second inlet section 2 through a separately installed pipeline to improve the efficiency of hydrogen production.

[0052] 1: First Entrance Section 2: Second Entrance 3: Feeding Section 4: Cylindrical section 5: Palladium film tube 6: Hydrogen collection tube 7: Waste liquid collection pipe 8: Hydrogen production reaction unit 9: Outer frame r: Straight-line distance between the feed opening and the center of the cylindrical section R: Radius of the cylindrical section L: Height at the tilt angle H: Height of the cylindrical section

Claims

1. A reaction apparatus comprising: two inlets, a first inlet and a second inlet, a feed section, a cylindrical section, a palladium membrane tube, a hydrogen collection tube, and a waste liquid recovery tube; reactants are injected and mixed through the two inlets and then injected into the feed section; the feed section is configured to be connected to the two inlets; the feed section is configured to inject the mixed reactants into the cylindrical section from bottom to top for reaction; the feed section and the hydrogen collection tube are symmetrically fixed to the lower and upper parts of the cylindrical section respectively using fixed bearings; the palladium membrane tube is disposed on the central side of the cylindrical section and connected to the hydrogen collection tube; the cylindrical section generates eddies and centrifugal force by rotating as a whole to generate product hydrogen and separate byproducts; the byproducts are discharged through the waste liquid recovery tube disposed at the lower part of the cylindrical section.

2. The reaction apparatus as described in claim 1, wherein, The rotational speed of the cylindrical section is 500~3000 rpm.

3. The reaction apparatus as described in claim 1, wherein, The cylindrical part is integrally formed from a cylinder connected to a frustum; the shape of the frustum is tapered downwards; the angle of inclination between the extended straight line of the cylinder sidewall and the sidewall of the frustum is 0 to 15 degrees.

4. The reaction apparatus as described in claim 3, wherein, The ratio of the height of the frustum to the height of the frustum and the cylinder is 0.1 to 0.

5.

5. The reaction apparatus as described in claim 1, wherein, The ratio of the straight-line distance r between the opening of the feed section and the center of the cylindrical section to the radius R of the cylindrical section is 0.1 to 0.

9.

6. The reaction apparatus as described in claim 1, wherein, The palladium film tube system has a catalyst disposed on the palladium film, which is selected from transition metals in groups IB-VIIB and VIIIB of the periodic table.

7. The reaction apparatus as described in claim 1, wherein, The reactant system comprises a borohydride solution and an aqueous catalyst solution; the borohydride solution contains a borohydride at a concentration of 1 to 60 wt% in the borohydride solution.

8. The reaction apparatus as described in claim 7, wherein, The viscosity of this borohydride solution is 1~300 cp.

9. The reaction apparatus as described in claim 1, wherein, The waste liquid recovery system is automatically switched on and off via remote control at a set time.

10. The reaction apparatus as described in claim 1, wherein, It further includes a first electric field element and a second electric field element; the first electric field element is an anode disposed on the cylindrical portion, and the second electric field element is a cathode disposed on the palladium film tube.

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