Active hydrogen recombiner and hydrogen removal system

Abstract

The present invention relates to an active hydrogen recombiner and a hydrogen elimination system. The active hydrogen recombiner is a reaction tower structure, which includes a cache tower section, a reaction tower section and a heat dissipation tower section connected in sequence. An air inlet is provided on the outer wall of the cache tower section; the reaction tower section is located at the upper part of the cache tower section, and a preheating layer is arranged on the outer wall of the reaction tower section. The active hydrogen recombiner can directly eliminate hydrogen in the mixed gas without hydrogen separation, and has a simple structure and low cost; the hydrogen elimination system includes: a hydrogen transmission pipeline, an oxygen transmission pipeline and an active hydrogen recombiner, and the active hydrogen recombiner has a first state and a second state; in the first state, the metal oxide can undergo a reduction reaction with hydrogen to generate a metal object; in the second state, the metal object can undergo an oxidation reaction with oxygen to generate a metal oxide. The hydrogen elimination system can achieve the regeneration of the metal oxide, and the metal oxide can be reused, and the hydrogen elimination cost is low.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen removal systems, and in particular to an active hydrogen recombiner and a hydrogen removal system. Background Art

[0002] In industrial production, dehydrogenation processes are often required in some complex mixed gas environments. For example, dehydrogenation is required during the operation of iron-chromium liquid flow batteries. The electrolyte of iron-chromium liquid flow batteries is a dilute hydrochloric acid solution containing iron salts and chromium salts. The electrolysis process will release a certain amount of hydrogen, and as the electrolysis process proceeds, the hydrogen in the electrolytic cell is enriched to form a high concentration of hydrogen, which will have a negative impact on the safety of the electrolyte and storage tanks.

[0003] In the prior art, because the mixed gas in the electrolytic cell contains a certain amount of hydrochloric acid vapor, the mixed gas is first neutralized by an alkali washing tower before dehydrogenation, and then separated by a palladium alloy membrane hydrogen separation device. The hydrogen is dehydrogenated by a hydrogen catalyst and then discharged into the atmosphere, and the remaining mixed gas returns to the electrolytic cell. This process method requires regular replenishment of nitrogen to the electrolytic cell, the palladium alloy hydrogen separation membrane has a high operating temperature and pressure, the system is relatively complex, and the device cost is high. Summary of the invention

[0004] Based on this, it is necessary to propose an active hydrogen recombiner and hydrogen removal system to address the problems of complex dehydrogenation systems and high device costs in the prior art.

[0005] A dynamic hydrogen recombiner, the dynamic hydrogen recombiner is a reaction tower structure, and the dynamic hydrogen recombiner comprises:

[0006] A cache tower section, used for caching the mixed gas, wherein an air inlet is provided on the outer wall of the cache tower section;

[0007] a reaction tower section, located at the upper part of the cache tower section and communicated with the interior of the cache tower section, wherein a bearing member is disposed in the reaction tower section; and

[0008] The preheating layer is arranged on the outer wall of the reaction tower section.

[0009] In one embodiment, the preheating layer comprises:

[0010] a delivery pipeline, wherein an outlet end of the delivery pipeline is connected to the air inlet; and

[0011] A heater is used to heat the reaction tower section and the transport pipeline at the same time.

[0012] In one embodiment, the delivery pipeline comprises:

[0013] A plurality of straight tubes, wherein the plurality of straight tubes are arranged at intervals along the circumferential direction of the outer wall of the reaction tower section, and the length direction of the plurality of straight tubes is the same as the axial direction of the cache tower section;

[0014] A plurality of connecting pipes, wherein the connecting pipes are arc-shaped pipes, and two adjacent straight pipes are connected in sequence through the connecting pipes.

[0015] In one embodiment, the heater is a heating rod, and there are multiple heating rods, and one heating rod is arranged between two adjacent straight tubes.

[0016] In one of the embodiments, the active hydrogen recombiner further includes: a thermal insulation layer, which is arranged radially outside the preheating layer.

[0017] In one embodiment, the active hydrogen recombiner further comprises:

[0018] The heat dissipation tower section is located at the upper part of the reaction tower section and is communicated with the reaction tower section. The heat dissipation tower section is provided with a radiator.

[0019] In one embodiment, the heat sink comprises:

[0020] A plurality of heat sinks are arranged at intervals on the outer wall of the heat sink section.

[0021] In one of the embodiments, an air outlet is provided at the upper portion of the heat dissipation tower section, and a passive hydrogen recombiner is disposed in the air outlet.

[0022] In one embodiment, the supporting member is a sieve plate, and the sieve plate is arranged at the bottom of the reaction tower section.

[0023] In one of the embodiments, a drain port is provided at the bottom of the cache tower section, and an automatic drain valve is provided in the drain port.

[0024] A hydrogen elimination system comprises: a hydrogen transmission pipeline, an oxygen transmission pipeline and the above-mentioned active hydrogen recombiner, wherein the output end of the hydrogen transmission pipeline and the output end of the oxygen transmission pipeline are both connected to the active hydrogen recombiner, and the active hydrogen recombiner has a first state and a second state;

[0025] In the first state, the hydrogen delivery pipeline is connected to the active hydrogen recombiner, and the oxygen delivery pipeline is not connected to the active hydrogen recombiner;

[0026] In the second state, the oxygen delivery pipeline is in communication with the active hydrogen recombiner, and the hydrogen delivery pipeline is not in communication with the active hydrogen recombiner.

[0027] In one of the embodiments, the number of the active hydrogen recombiners is at least two, and when one of the active hydrogen recombiners is in a first state, the other active hydrogen recombiner is in a second state.

[0028] In one embodiment, the hydrogen removal system further comprises:

[0029] A gas return line connected to the upper portion of the reaction tower section;

[0030] Hydrogen sensor: hydrogen sensors are respectively arranged on the return air pipeline and the hydrogen transmission pipeline.

[0031] The above-mentioned active hydrogen recombiner and hydrogen elimination system, when hydrogen elimination is required, place the metal oxide on the carrier, and introduce a mixed gas containing hydrogen into the cache tower section from the air inlet. Since the cache tower section and the reaction tower section are connected in sequence from bottom to top, when the mixed gas enters the reaction tower section from the cache tower section, it can react with the metal oxide in the reaction tower, thereby eliminating the hydrogen in the mixed gas, and the mixed gas after the hydrogen is eliminated can continue to move upward and then leave the reaction tower section. The reactant is a metal oxide, and when hydrogen reacts with the metal oxide to generate metal and water, the process will not produce polluting mixed gas. Therefore, when it is necessary to remove hydrogen from the mixed gas, the mixed gas can be directly introduced into the active hydrogen recombiner for reaction, and no palladium alloy hydrogen separation membrane is required. The system is simple and the cost is low. The hydrogen removal system includes: a hydrogen transmission pipeline, an oxygen transmission pipeline and an active hydrogen recombiner. The active hydrogen recombiner has a first state and a second state. In the first state, the metal oxide can undergo a reduction reaction with hydrogen to generate a metal object; in the second state, the metal object can undergo an oxidation reaction with oxygen to generate a metal oxide. That is, the hydrogen removal system can achieve the regeneration of the metal oxide, the metal oxide can be reused, and the hydrogen removal cost is low. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 This is a schematic diagram of the structure of an active hydrogen recombiner in one embodiment;

[0033] Figure 2 is a schematic plan view of a preheating layer in an embodiment;

[0034] Figure 3 is a connection diagram of a hydrogen removal system in one embodiment;

[0035] Reference numerals: 100-active hydrogen recombiner; 110-buffer tower section; 111-air inlet; 113-liquid discharge port; 114-automatic drain valve; 120-reaction tower section; 121-sieve plate; 130-heating tower section; 131-heating fin; 132-air outlet; 133-passive hydrogen recombiner; 140-preheating layer; 141-transport pipeline; 1411-connecting pipe; 1412-transport pipeline inlet; 1413-transport pipeline outlet; 1416-straight pipe; 142-heating rod; 150-insulation layer; 160-flange;

[0036] 200-Hydrogen pipeline;

[0037] 300-return gas pipeline; 310-gas-liquid separator; 320-hydrogen sensor; 330-valve;

[0038] 400-oxygen pipeline; 500-electrolytic cell; 600-alkali washing tower; 700-air compressor. DETAILED DESCRIPTION

[0039] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the specific embodiments of the present invention are described in detail below in conjunction with the accompanying drawings. In the following description, many specific details are set forth to facilitate a full understanding of the present invention. However, the present invention can be implemented in many other ways different from those described herein, and those skilled in the art can make similar improvements without violating the connotation of the present invention, so the present invention is not limited by the specific embodiments disclosed below.

[0040] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0041] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0042] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0043] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0044] It should be noted that when an element is referred to as being "fixed to" or "disposed on" another element, it may be directly on the other element or there may be a central element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be a central element at the same time. The terms "vertical", "horizontal", "upper", "lower", "left", "right" and similar expressions used herein are for illustrative purposes only and are not intended to be the only implementation method.

[0045] See also Figure 1 , Figure 1 A schematic structural diagram of an active hydrogen recombiner 100 in an embodiment of the present invention is shown. An embodiment of the present invention provides an active hydrogen recombiner 100, which is a reaction tower type structure. The active hydrogen recombiner 100 includes a buffer tower section 110, a reaction tower section 120 and a preheating layer 140.

[0046] The cache tower section 110 is used to cache the mixed gas, and an air inlet 111 is provided on the outer wall of the cache tower section 110. The mixed gas can enter the cache tower section 110 through the air inlet 111.

[0047] The reaction tower section 120 is connected to the cache tower section 110 through a flange 160. The reaction tower section 120 is located at the upper part of the cache tower section 110 and is connected to the inside of the cache tower section 110. A support is provided in the reaction tower section 120. A through hole is provided on the support, and the support is used to carry the reactants. The through hole is used to allow the mixed gas to pass through. The mixed gas in the cache tower section 110 accumulates and is pressurized in the cache tower section 110 and moves upward until it passes through the through hole and then reacts with the reactants on the support. Since the mixed gas passes through the reactants from bottom to top, the contact area between the mixed gas and the reactants in the reaction tower section 120 can be increased, thereby promoting a complete reaction.

[0048] The preheating layer 140 is disposed around the outer wall of the reaction tower section 120 . The preheating layer 140 can increase the reaction temperature and further accelerate the reaction process.

[0049] When it is necessary to remove hydrogen, the reactant is placed on the carrier, and a mixed gas containing hydrogen is introduced into the cache tower section 110 from the air inlet 111. At this time, the reactant is a metal oxide, and the metal oxide can be copper oxide, ferric oxide, aluminum oxide, zinc oxide, etc. Since the cache tower section 110 is located below the reaction tower section 120, when the mixed gas enters the reaction tower section 120 from the bottom to the top, it can react with the metal oxide in the reaction tower, thereby eliminating the hydrogen in the mixed gas, and the mixed gas after the hydrogen is eliminated can continue to move upward and then leave the reaction tower section. The reactant is a metal oxide, and when hydrogen reacts with the metal oxide to generate metal and water, that is, the process does not produce polluting mixed gas, therefore, when it is necessary to remove hydrogen in the mixed gas, the mixed gas can be directly introduced into the active hydrogen recombiner 100 for reaction, and no palladium alloy hydrogen separation membrane is required, and the system is simple and low in cost.

[0050] Combination Figure 2 , Figure 2 A schematic plan view of a preheating layer in an embodiment is shown. In some embodiments, a heater and a delivery pipeline 141 are provided in the preheating layer 140. The outlet end of the delivery pipeline 141 is connected to the air inlet 111 of the buffer tower section 110, and the heater can heat the reaction tower section 120 and the delivery pipeline 141 at the same time.

[0051] In this embodiment, the delivery pipeline 141 is provided with a delivery pipeline inlet 1412 and a delivery pipeline outlet 1413. When dehydrogenating, the mixed gas containing hydrogen is pressed into the delivery pipeline 141 from the delivery pipeline inlet 1412. The mixed gas entering the delivery pipeline 141 is first heated by the heater and then delivered to the buffer tower section 110. Since the preheating layer 140 is arranged on the outer wall of the reaction tower section 120, the preheating layer 140 includes the delivery pipeline 141 and the heater, so the heater can heat the reactants (metal oxides in the reaction tower section 120 and hydrogen in the delivery pipeline 141) and the reaction environment (reaction tower section 120) at the same time, thereby improving the dehydrogenating efficiency.

[0052] Furthermore, the conveying pipeline 141 includes a plurality of straight pipes 1416 and a plurality of connecting pipes 1411 . The plurality of straight pipes 1416 are arranged at intervals along the circumference of the outer wall of the reaction tower section 120 . The connecting pipe 1411 is an arc-shaped pipe, and two adjacent straight pipes 1416 are connected in sequence through the connecting pipe 1411 .

[0053] In this embodiment, the connecting pipe 1411 includes a first connecting pipe and a second connecting pipe, the first connecting pipe connects the bottom ends of two adjacent straight pipes 1416, and the second connecting pipe connects the upper ends of two adjacent straight pipes 1416. The first connecting pipe and the second connecting pipe are alternately arranged along the circumference of the outer wall of the reaction tower section 120, that is, a plurality of straight pipes 1416 are sequentially connected through a plurality of connecting pipes 1411 to form a serpentine coil. The reaction tower section 120 is set as a cylindrical structure, and the serpentine coil surrounds the circumference of the reaction tower section 120 of the cylindrical structure, that is, the heat exchange area of ​​the delivery pipeline 141 can be increased, and then the temperature of the mixed gas in the delivery pipeline 141 can be quickly increased; at the same time, in order to facilitate the arrangement of the straight pipes 1416, the length direction of the plurality of straight pipes 1416 is the same as the axial direction of the cache tower section 110.

[0054] Furthermore, in order to make the multiple straight tubes 1416 evenly heated and improve the heat exchange efficiency of hydrogen in the straight tubes 1416, the heater is a heating rod 142, and the number of the heating rods 142 is multiple, and the multiple heating rods 142 are respectively inserted between two adjacent straight tubes 1416.

[0055] See also Figure 1 In some embodiments, the active hydrogen recombiner 100 further includes a thermal insulation layer 150 , and the thermal insulation layer 150 is disposed on the outer side of the preheating layer 140 .

[0056] Specifically, the insulation layer 150 is used to reduce the heat dissipation of the preheating layer 140 and the reaction tower section 120 . The insulation layer 150 can be composed of silicate wool or rock wool. The outer side of the silicate wool or rock wool is wrapped by a metal plate, and the upper and lower ends of the metal plate are welded to the flange 160 .

[0057] In some embodiments, the active hydrogen recombiner 100 further includes a heat dissipation tower section 130 , which is located at the upper portion of the reaction tower section 120 and communicates with the reaction tower section 120 , and the heat dissipation tower section 130 is provided with a radiator.

[0058] Since the outer wall of the reaction tower section 120 is provided with a preheating layer, the temperature of the mixed gas is very high after the reaction tower section 120 removes hydrogen. Therefore, by providing the heat dissipation tower section 130, when the mixed gas rises to the heat dissipation tower section 130, it can be cooled by the heat dissipation tower section 130.

[0059] Furthermore, the radiator is a plurality of heat sinks 131 evenly distributed on the outer wall of the heat dissipation tower section 130. Specifically, the extension direction of the heat sink 131 can be perpendicular to the outer wall of the heat dissipation tower section 130. By providing a plurality of heat sinks 131 that increase the heat dissipation area, heat can be conducted to the external environment as quickly as possible, thereby reducing the temperature of the mixed gas after dehydrogenation, making it easier to return to the electrolytic cell for reuse.

[0060] In some embodiments, the supporting member is a sieve plate 121, which is a porous plate, wherein the diameter of the holes should be smaller than the minimum size of the metal oxide in any direction, that is, the metal oxide can be placed on the sieve plate 121, and the mixed gas from the cache tower section 110 can pass through the holes. In addition, in order to improve the reaction efficiency, the sieve plate 121 can be arranged in multiple layers.

[0061] In some embodiments, a drain port 113 is provided at the bottom of the cache tower section 110, and an automatic drain valve 114 is provided in the drain port 113. The inner cavity 112 of the cache tower section 110 can be used as a water pool. Water generated by the reaction of hydrogen and metal oxide can flow downward from the reaction tower section 120 to the water pool, and when the water in the water pool accumulates to a certain amount, the automatic drain valve 114 can automatically open to drain water.

[0062] Combination Figure 3 , Figure 3 A connection diagram of a hydrogen removal system in an embodiment of the present invention is shown. A hydrogen removal system includes: a hydrogen transmission pipeline 200, an oxygen transmission pipeline 400 and the above-mentioned active hydrogen recombiner 100. The output end of the hydrogen transmission pipeline 200 and the output end of the oxygen transmission pipeline 400 are both connected to the delivery pipeline inlet 1412. The active hydrogen recombiner 100 has a first state and a second state.

[0063] In the first state, the hydrogen transmission pipeline 200 is connected to the active hydrogen recombiner 100, and the oxygen transmission pipeline 400 is not connected to the active hydrogen recombiner 100; specifically, the input end of the hydrogen transmission pipeline 200 is connected to the alkali washing tower 600, and a pump body is provided on the input end of the hydrogen transmission pipeline 200, which is used to pump the mixed gas (containing hydrogen) after alkali washing in the alkali washing tower 600 into the hydrogen transmission pipeline 200, and the output end of the hydrogen transmission pipeline 200 is connected to the delivery pipeline inlet 1412 on the active hydrogen recombiner 100, that is, the mixed gas can enter the delivery pipeline 141 to be preheated, and the delivery pipeline outlet 1413 is connected to the air inlet 111 of the cache tower section 110, that is, the mixed gas can enter the reaction tower section 120 from the cache tower section 110 for reduction reaction.

[0064] In the second state, the oxygen delivery pipeline 400 is in communication with the active hydrogen recombiner 100, and the hydrogen delivery pipeline 200 is not in communication with the active hydrogen recombiner 100. Specifically, the input end of the oxygen delivery pipeline 400 is connected to the air compressor 700, and the air compressor 700 presses the compressed air into the oxygen delivery pipeline 400, and the output end of the oxygen delivery pipeline 400 is connected to the delivery pipeline inlet 1412 on the active hydrogen recombiner 100, that is, the compressed air can enter the reaction tower section 120 along the same path as the mixed gas for oxidation reaction.

[0065] The hydrogen delivery pipeline 200 and the oxygen delivery pipeline are respectively provided with valves 330. When used for the first time, the reaction tower section 120 is first filled with metal oxides, and then the valve 330 on the hydrogen delivery pipeline 200 is opened, and the mixed gas from the alkali washing tower 600 enters the reaction tower section 120 for hydrogen removal; when the metal oxides in the reaction tower section 120 are reduced to metal objects, the valve 330 on the hydrogen delivery pipeline 200 is closed, and the valve 330 on the oxygen delivery pipeline 400 and the air compressor 700 are opened. The air compressor 700 presses compressed air into the reaction tower section 120, and the oxygen in the compressed air reacts with the metal objects to regenerate metal oxides. Therefore, the hydrogen removal system in this embodiment can realize the regeneration of metal oxides. When the metal oxides are consumed, they can be directly generated and reused, thereby reducing the cost of hydrogen removal.

[0066] In some embodiments, an air outlet 132 is provided at the upper portion of the heat dissipation tower section 130, and a passive hydrogen recombiner 133 is provided in the air outlet 132. The hydrogen elimination system further includes a return air pipeline 300 and a hydrogen sensor 320, wherein the inlet end of the return air pipeline 300 is connected to the upper portion of the reaction tower section, and the return air pipeline 300 and the hydrogen transmission pipeline 200 are provided with hydrogen sensors 320, respectively.

[0067] In this embodiment, since the heat dissipation tower section 130 is located at the upper part of the reaction tower section, the air outlet 132 can be set at the upper part of the heat dissipation tower section 130, and then the inlet end of the return air pipeline 300 is connected to the air outlet 132 of the heat dissipation tower section 130. After the mixed gas is dehydrogenated in the reaction tower section 120, it continues to move upward to the heat dissipation section. After being cooled by the heat dissipation tower section 130, it enters the return air pipeline 300 through the air outlet 132 set at the top of the heat dissipation tower, and then returns to the electrolytic cell 500 through the return air pipeline 300, so as to facilitate the reuse of the mixed gas after dehydrogenation.

[0068] A passive hydrogen recombiner 133 is provided in the gas outlet 132. When the oxidation reaction is performed, compressed air containing oxygen needs to be introduced into the reaction tower section 120. Therefore, when the active hydrogen recombiner 100 is switched from the second state to the first state again, a certain amount of oxygen will remain in the active hydrogen recombiner 100. When the dehydrogenated mixed gas returns to the electrolytic cell 500, the passive hydrogen recombiner 133 can eliminate the oxygen therein, thereby ensuring that the mixed gas returned to the electrolytic cell 500 is an oxygen-free safe mixed gas.

[0069] A hydrogen sensor 320 is provided on the hydrogen transmission pipeline 200 for detecting and recording the hydrogen content in the mixed gas before hydrogen removal. A hydrogen sensor 320 is provided on the gas return pipeline 300 for detecting and recording the hydrogen content in the mixed gas after hydrogen removal. When the active hydrogen recombiner 100 is in the first state, the detection values ​​of the two hydrogen sensors 320 can be compared. If the two are close, it means that the metal oxides in the reaction tower have been reduced to metal objects. At this time, the active hydrogen recombiner 100 can be switched from the first state to the second state.

[0070] In some embodiments, the number of the active hydrogen recombiners 100 is at least two, and when one of the active hydrogen recombiners 100 is in the first state, the other active hydrogen recombiner 100 is in the second state.

[0071] In this embodiment, the number of active hydrogen recombiners 100 is two, and the two active hydrogen recombiners 100 are respectively the first active hydrogen recombiner and the second active hydrogen recombiner. When the metal oxide in the first active hydrogen recombiner is reduced, the valves 330 on the hydrogen delivery pipeline 200 and the return gas pipeline 300 connected to the first active hydrogen recombiner are closed respectively, and the valve 330 on the oxygen delivery pipeline connected to the first active hydrogen recombiner is opened. At the same time, the valves 330 on the hydrogen delivery pipeline 200 and the return gas pipeline 300 connected to the second active hydrogen recombiner are opened respectively, so that the first active hydrogen recombiner is oxidized, and at the same time, the second active hydrogen recombiner is dehydrogenated. Similarly, when the metal oxide in the second active hydrogen recombiner is reduced, according to the above method, the second active hydrogen recombiner is oxidized, and at the same time, the first active hydrogen recombiner is dehydrogenated. The first active hydrogen recombiner and the second active hydrogen recombiner can be used alternately, and the dehydrogenation process can be carried out continuously.

[0072] In another embodiment, when the hydrogen concentration in the mixed gas is high and only two active hydrogen recombiners 100 cannot achieve continuous hydrogen removal, the number of active hydrogen recombiners 100 can be more than two, and more than two active hydrogen recombiners 100 can be used alternately.

[0073] In other embodiments, a control unit may be further provided, and the valves 330 on the hydrogen delivery pipeline 200 and the return air pipeline 300 , the air compressor 700 , the hydrogen sensor 320 , etc. are all electrically connected to the control unit, and the control unit can realize automatic replacement of at least two active hydrogen recombiners 100 .

[0074] In some embodiments, the hydrogen elimination system further includes a steam-water separator. The return gas pipeline 300 and the hydrogen transmission pipeline 200 are respectively provided with steam-water separators for eliminating or reducing water vapor in the return gas pipeline 300 and the hydrogen transmission pipeline 200 .

[0075] The technical features of the above-described embodiments may be arbitrarily combined. To make the description concise, not all possible combinations of the technical features in the above-described embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0076] The above-mentioned embodiments only express several implementation methods of the present invention, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the scope of the invention patent. It should be pointed out that, for ordinary technicians in this field, several variations and improvements can be made without departing from the concept of the present invention, and these all belong to the protection scope of the present invention. Therefore, the protection scope of the patent of the present invention shall be subject to the attached claims.

Claims

1. A dynamic hydrogen recombiner, characterized in that: The active hydrogen recombiner is a reaction tower structure, and the active hydrogen recombiner comprises: A cache tower section, used for caching the mixed gas, wherein an air inlet is provided on the outer wall of the cache tower section; A reaction tower section, located at the upper part of the cache tower section and communicated with the interior of the cache tower section, wherein a bearing member is arranged in the reaction tower section; a preheating layer, which is arranged around the outer wall of the reaction tower section, and comprises a delivery pipeline and a heater, wherein the outlet end of the delivery pipeline is connected to the air inlet; the heater is used to heat the reaction tower section and the delivery pipeline at the same time; the delivery pipeline is formed by connecting a plurality of straight pipes in sequence through a plurality of connecting pipes, and the heater is inserted between two adjacent straight pipes; and The heat dissipation tower section is located at the upper part of the reaction tower section and is connected with the reaction tower section. The heat dissipation tower section is provided with a radiator. An air outlet is opened at the upper part of the heat dissipation tower section. The air outlet is used to be connected with the electrolytic cell through a return air pipeline.

2. The active hydrogen recombiner according to claim 1, characterized in that: The plurality of straight tubes are arranged at intervals along the circumferential direction of the outer wall of the reaction tower section, and the length direction of the plurality of straight tubes is the same as the axial direction of the cache tower section; The connecting pipe is an arc-shaped pipe, and two adjacent straight pipes are connected in sequence through the connecting pipe.

3. The active hydrogen recombiner according to claim 2, characterized in that: The heater is a heating rod, and there are multiple heating rods. One heating rod is arranged between two adjacent straight tubes.

4. The active hydrogen recombiner according to claim 1, characterized in that: The active hydrogen recombiner also includes: The heat-insulating layer is arranged on the radially outer side of the preheating layer.

5. The active hydrogen recombiner according to claim 1, characterized in that: The radiator comprises: A plurality of heat sinks are arranged at intervals on the outer wall of the heat sink section.

6. The active hydrogen recombiner according to claim 1, characterized in that: A passive hydrogen recombiner is arranged in the gas outlet.

7. The active hydrogen recombiner according to claim 1, characterized in that: The supporting member is a sieve plate, and the sieve plate is arranged at the bottom of the reaction tower section.

8. The active hydrogen recombiner according to claim 1, characterized in that: A liquid drain port is provided at the bottom of the cache tower section, and an automatic drain valve is arranged in the liquid drain port.

9. A hydrogen removal system, characterized in that: include: A hydrogen delivery pipeline, an oxygen delivery pipeline, and the active hydrogen recombiner according to any one of claims 1 to 8, wherein the output end of the hydrogen delivery pipeline and the output end of the oxygen delivery pipeline are both connected to the active hydrogen recombiner, and the active hydrogen recombiner has a first state and a second state; In the first state, the hydrogen delivery pipeline is connected to the active hydrogen recombiner, and the oxygen delivery pipeline is not connected to the active hydrogen recombiner; In the second state, the oxygen delivery pipeline is connected to the active hydrogen recombiner, and the hydrogen delivery pipeline is not connected to the active hydrogen recombiner; The hydrogen removal system also includes: A return air pipeline, one end of which is connected to the upper part of the reaction tower section, and the other end of which is connected to the electrolytic cell; A hydrogen sensor is provided on the gas return line and the hydrogen delivery line respectively; The hydrogen sensor on the hydrogen delivery pipeline is used to detect and record the hydrogen content in the mixed gas before hydrogen elimination, and the hydrogen sensor on the return gas pipeline is used to detect and record the hydrogen content in the mixed gas after hydrogen elimination; when the active hydrogen recombiner is in the first state, the detection values ​​of the two hydrogen sensors are compared, and if the two are close, the active hydrogen recombiner is switched from the first state to the second state.

10. The hydrogen removal system according to claim 9, characterized in that: The number of the active hydrogen recombiners is at least two, and when one of the active hydrogen recombiners is in a first state, the other active hydrogen recombiner is in a second state.

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