CN218339415U - Movable hydrogen recombiner and hydrogen elimination system - Google Patents

Abstract

The utility model relates to an active hydrogen recombiner and a dehydrogenation system, wherein the active hydrogen recombiner is of a reaction tower structure and comprises a cache tower section, a reaction tower section and a heat dissipation tower section which are sequentially communicated, and the outer wall of the cache tower section is provided with an air inlet; the reaction tower section is positioned at the upper part of the buffer tower section, and the outer wall of the reaction tower section is provided with a preheating layer. The movable hydrogen recombiner can directly eliminate hydrogen in the mixed gas without hydrogen separation, and has simple structure and low cost; the dehydrogenation system comprises: the hydrogen supply system comprises a hydrogen conveying pipeline, an oxygen conveying pipeline and an active hydrogen recombiner, wherein the active hydrogen recombiner has a first state and a second state; in the first state, the metal oxide can generate reduction reaction with hydrogen to generate metal products; in the second state, the metal species is capable of undergoing an oxidation reaction with oxygen to form a metal oxide. The dehydrogenation system can realize the regeneration of metal oxide, the metal oxide can be reused, and the dehydrogenation cost is low.

Description

Movable hydrogen recombiner and hydrogen elimination system

Technical Field

The utility model relates to a hydrogen system technical field that disappears especially relates to a can move dynamic formula hydrogen recombiner and hydrogen system that disappears.

Background

In industrial production, some complex mixed gas environments often need to be subjected to a dehydrogenation process, for example, an iron-chromium flow battery needs to be subjected to dehydrogenation during operation, an electrolyte of the iron-chromium flow battery is a dilute hydrochloric acid solution containing iron salt and chromium salt, a certain amount of hydrogen is released during electrolysis, and hydrogen in the electrolytic cell is enriched to form high-concentration hydrogen along with the electrolysis process, so that the safety of the electrolyte and a storage tank is negatively affected.

In the prior art, because the mixed gas in the electrolytic cell contains a certain amount of hydrochloric acid steam, the mixed gas is firstly neutralized by acid and alkali in an alkali washing tower before hydrogen is eliminated, then hydrogen is separated by using a palladium alloy film hydrogen separation device, the hydrogen is exhausted out of the atmosphere after being catalyzed by a hydrogen catalyst for hydrogen elimination, and the rest mixed gas returns to the electrolytic cell. The process method needs to supplement nitrogen to the electrolytic cell periodically, the working temperature and pressure of the palladium alloy hydrogen separation membrane are high, the system is relatively complex, and the device cost is high.

SUMMERY OF THE UTILITY MODEL

Accordingly, it is necessary to provide an active hydrogen recombiner and a dehydrogenation system to solve the problems of complicated dehydrogenation system and high device cost in the prior art.

An active hydrogen recombiner, the active hydrogen recombiner being of a reaction tower type structure, the active hydrogen recombiner comprising:

the buffer tower section is used for buffering mixed gas, and an air inlet is formed in the outer wall of the buffer tower section;

the reaction tower section is positioned at the upper part of the cache tower section and is communicated with the interior of the cache tower section, and a bearing piece is arranged in the reaction tower section; and

and the preheating layer is arranged on the outer wall of the reaction tower section.

In one embodiment, the preheating layer comprises:

the outlet end of the conveying pipeline is connected with the air inlet; and

and the heater is used for heating the reaction tower section and the conveying pipeline simultaneously.

In one embodiment, the delivery conduit comprises:

the straight pipes are arranged at intervals along the circumferential direction of the outer wall of the reaction tower section, and the length direction of the straight pipes is the same as the axial direction of the cache tower section;

the connecting pipes are arc pipes, and the adjacent two straight pipes are connected in sequence through the connecting pipes.

In one embodiment, the heater is a plurality of heating rods, and one heating rod is arranged between two adjacent straight pipes.

In one embodiment, the movable hydrogen recombiner further comprises an insulating layer arranged on the radial outer side of the preheating layer.

In one embodiment, the kinetic hydrogen recombiner further comprises:

and the heat dissipation tower section is positioned at the upper part of the reaction tower section and is communicated with the reaction tower section, and the heat dissipation tower section is provided with a radiator.

In one embodiment, the heat sink includes:

and the plurality of radiating fins are arranged on the outer wall of the radiating tower section at intervals.

In one embodiment, the upper part of the heat dissipation tower section is provided with an air outlet, and a passive hydrogen recombiner is arranged in the air outlet.

In one embodiment, the carrier is a sieve plate, and the sieve plate is arranged at the bottom of the reaction tower section.

In one embodiment, the bottom of the cache tower section is provided with a liquid outlet, and an automatic drain valve is arranged in the liquid outlet.

A dehydrogenation system comprising: the output end of the hydrogen pipeline and the output end of the oxygen pipeline are both connected with the active hydrogen recombiner, and the active hydrogen recombiner has a first state and a second state;

in a first state, the hydrogen pipeline is communicated with the active hydrogen recombiner, and the oxygen pipeline is not communicated with the active hydrogen recombiner;

and in the second state, the oxygen pipeline is communicated with the active hydrogen recombiner, and the hydrogen pipeline is not communicated with the active hydrogen recombiner.

In one embodiment, the number of the dynamic hydrogen recombiners is at least two, and when one of the dynamic hydrogen recombiners is in the first state, the other dynamic hydrogen recombiner is in the second state.

In one embodiment, the dehydrogenation system further comprises:

the gas return line is communicated with the upper part of the reaction tower section;

and the gas return pipeline and the hydrogen conveying pipeline are respectively provided with a hydrogen sensor.

When the hydrogen is required to be removed, the metal oxide is placed on the bearing piece, and the mixed gas containing the hydrogen is introduced into the cache tower section from the gas inlet. Because the buffer tower section and the reaction tower section are sequentially communicated from bottom to top, when the mixed gas enters the reaction tower section from the buffer tower section, the mixed gas can react with the metal oxide in the reaction tower, so that the hydrogen in the mixed gas is eliminated, and the mixed gas after the hydrogen is eliminated can continuously move upwards and then leave the reaction tower section. The reactant is metal oxide, and when the hydrogen reacts with the metal oxide to generate metal and water, no polluting mixed gas is generated in the process, so that when the hydrogen in the mixed gas needs to be removed, the mixed gas can be directly introduced into the active hydrogen recombiner to react, a palladium alloy hydrogen separation membrane is not needed, the system is simple, and the cost is low. The dehydrogenation system comprises: the hydrogen supply system comprises a hydrogen conveying pipeline, an oxygen conveying pipeline and an active hydrogen recombiner, wherein the active hydrogen recombiner has a first state and a second state; in the first state, the metal oxide can generate reduction reaction with hydrogen to generate metal products; in the second state, the metal species is capable of undergoing an oxidation reaction with oxygen to form a metal oxide. Namely, the dehydrogenation system can realize the regeneration of the metal oxide, the metal oxide can be repeatedly used, and the dehydrogenation cost is low.

Drawings

FIG. 1 is a schematic diagram of an embodiment of an active hydrogen recombiner;

FIG. 2 is a schematic plan view of a preheat layer in one embodiment;

FIG. 3 is a schematic diagram of a hydrogen elimination system connection in one embodiment;

reference numerals: 100-active hydrogen recombiner; 110-cache tower segment; 111-an air inlet; 113-liquid drain; 114-automatic drain valve; 120-a reaction column section; 121-sieve plate; 130-a heat dissipation tower section; 131-a heat sink; 132-outlet port; 133-passive hydrogen recombiner; 140-a preheating layer; 141-a conveying pipeline; 1411-connecting tube; 1412-delivery duct inlet; 1413-delivery conduit outlet; 1416-straight tube; 142-a heating rod; 150-an insulating layer; 160-flange plate;

200-a hydrogen transmission line;

300-a return gas line; 310-a vapor-liquid separator; 320-a hydrogen sensor; 330-a valve;

400-an oxygen transfer line; 500-an electrolytic cell; 600-an alkaline washing tower; 700-air compressor.

Detailed Description

In order to make the above objects, features and advantages of the present invention more comprehensible, embodiments of the present invention are described in detail below with reference to the accompanying drawings. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein, as those skilled in the art will be able to make similar modifications without departing from the spirit and scope of the present invention.

In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", and the like, indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and "fixed" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.

In the present application, unless expressly stated or limited otherwise, the first feature may be directly on or directly under the second feature or indirectly via intermediate members. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

It will be understood that when an element is referred to as being "secured to" or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like as used herein are for illustrative purposes only and do not denote a unique embodiment.

Referring to fig. 1, fig. 1 shows a schematic structural diagram of an active hydrogen recombiner 100 according to an embodiment of the present invention, an embodiment of the present invention provides an active hydrogen recombiner 100, which is a reaction tower structure, and the active hydrogen recombiner 100 includes a buffer tower segment 110, a reaction tower segment 120, and a preheating layer 140.

The buffer tower section 110 is used for buffering mixed gas, and an air inlet 111 is formed in the outer wall of the buffer tower section 110. The mixed gas can enter the buffer tower section 110 from the gas inlet 111.

The reactor section 120 is connected to the buffer tower section 110 by a flange 160. The reaction tower section 120 is located at the upper part of the cache tower section 110 and is communicated with the inside of the cache tower section 110, and a bearing part is arranged in the reaction tower section 120. The bearing piece is provided with a through hole and is used for bearing reactants. The through holes are used for allowing the mixed gas to pass through, and the mixed gas introduced into the buffer tower section 110 moves upwards after being accumulated and pressurized in the buffer tower section 110 until passing through the through holes and then reacting with the reactant on the bearing member. Since the mixed gas passes through the reactant from the bottom to the top, the contact area of the mixed gas with the reactant in the reaction tower section 120 can be increased, thereby promoting complete reaction.

The preheating layer 140 surrounds the outer wall of the reaction tower section 120, and the preheating layer 140 can increase the reaction temperature and further accelerate the reaction process.

When dehydrogenation is needed, the reactant is placed on the carrier, and the mixed gas containing hydrogen is introduced into the buffer tower section 110 from the gas inlet 111, where the reactant is a metal oxide, and the metal oxide may be copper oxide, iron sesquioxide, aluminum oxide, zinc oxide, or the like. Because the buffer tower section 110 is located below the reaction tower section 120, when the mixed gas enters the reaction tower section 120 from bottom to top, the mixed gas can react with the metal oxide in the reaction tower, so that hydrogen in the mixed gas is eliminated, and the mixed gas after the hydrogen is eliminated can continuously move upwards to leave the reaction tower section. The reactant is metal oxide, and after the hydrogen and the metal oxide react, metal and water are generated, namely, no polluting mixed gas is generated in the process, so that when the hydrogen in the mixed gas needs to be removed, the mixed gas can be directly introduced into the active hydrogen recombiner 100 for reaction, a palladium alloy hydrogen separation membrane is not needed, the system is simple, and the cost is low.

Referring to fig. 2, fig. 2 shows a schematic plan view of a preheat layer in one embodiment, and in some embodiments, heaters and delivery conduits 141 are disposed within preheat layer 140. The outlet end of the delivery pipe 141 is connected to the air inlet 111 of the buffer tower segment 110, and the heater can heat the reaction tower segment 120 and the delivery pipe 141 at the same time.

In this embodiment, the delivery pipe 141 is provided with a delivery pipe inlet 1412 and a delivery pipe outlet 1413, and when hydrogen is eliminated, the mixed gas containing hydrogen is pressed into the delivery pipe 141 from the delivery pipe inlet 1412, and the mixed gas entering the delivery pipe 141 is heated by the heater and then delivered to the buffer tower segment 110. Since the preheating layer 140 is disposed on the outer wall of the reaction tower section 120, and the preheating layer 140 includes the conveying pipe 141 and the heater, the heater can heat the reactants (the metal oxide inside the reaction tower section 120 and the hydrogen in the conveying pipe 141) and the reaction environment (the reaction tower section 120) at the same time, so that the dehydrogenation efficiency can be improved.

Further, 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 circumferential direction of the outer wall of the reaction tower section 120, the connecting pipes 1411 are arc pipes, and two adjacent straight pipes 1416 are connected in sequence through the connecting pipes 1411.

In this embodiment, the connection pipe 1411 includes a first connection pipe and a second connection pipe, the first connection pipe connects the bottom ends of two adjacent straight pipes 1416, the second connection pipe connects the upper ends of two adjacent straight pipes 1416, the first connection pipe and the second connection pipe are alternately arranged along the circumference of the outer wall of the reaction tower section 120, that is, the plurality of straight pipes 1416 are sequentially connected through the plurality of connection pipes 1411 to form the serpentine coil. The reaction tower section 120 is arranged to be a cylindrical structure, and the serpentine coil is wound around the periphery of the reaction tower section 120 with the cylindrical structure, so that the heat exchange area of the conveying pipeline 141 can be increased, and the temperature of the mixed gas in the conveying pipeline 141 can be rapidly increased; meanwhile, for convenience of arrangement of the straight pipes 1416, the length directions of the straight pipes 1416 are the same as the axial direction of the cache tower segment 110.

Further, in order to uniformly heat the plurality of straight pipes 1416 and improve the heat exchange efficiency of hydrogen in the straight pipes 1416, the heater is a plurality of heating rods 142, the number of the heating rods 142 is multiple, and the plurality of heating rods 142 are respectively inserted between two adjacent straight pipes 1416.

Referring to fig. 1, in some embodiments, the active hydrogen recombiner 100 further includes an insulating layer 150, the insulating layer 150 being disposed outside the preheating layer 140.

Specifically, the heat insulating layer 150 is used for reducing the heat dissipation of the preheating layer 140 and the reaction tower section 120, the heat insulating layer 150 may be formed by laying silicate cotton or rock wool, the outer side of the silicate cotton or rock wool is wrapped by a metal plate, and the upper end and the lower end of the metal plate are welded to the flange plate 160.

In some embodiments, the active hydrogen recombiner 100 further includes a heat sink tower section 130, the heat sink tower section 130 is located at an upper portion of the reaction tower section 120 and is in communication with the reaction tower section 120, and the heat sink tower section 130 is provided with a heat sink.

Because the outer wall of the reaction tower section 120 is provided with the preheating layer, the temperature of the mixed gas is very high after the reaction dehydrogenation of the reaction tower section 120, and therefore, by arranging the heat dissipation tower section 130, when the mixed gas rises to the heat dissipation tower section 130, the temperature can be reduced through the heat dissipation tower section 130.

Further, the radiator is the equipartition and is in a plurality of fin 131 on the outer wall of radiator tower section 130, it is specific, the extending direction of fin 131 can with the outer wall of radiator tower section 130 is perpendicular, through setting up a plurality of fin 131 that increase heat radiating area, can be as fast as possible with heat conduction to external environment in, and then make the mist temperature after the dehydrogenation reduce, be convenient for return reuse in the electrolytic bath.

In some embodiments, the carrier is a sieve plate 121, and the sieve plate 121 is a porous plate, wherein the diameter of the holes should be smaller than the minimum size of the metal oxide in any direction, i.e. the metal oxide can be placed on the sieve plate 121 while the mixed gas from the buffer tower section 110 can pass through the holes, and furthermore, the sieve plate 121 can be provided in multiple layers in order to improve the reaction efficiency.

In some embodiments, the bottom of the cache tower segment 110 is opened with a drain port 113, and an automatic drain valve 114 is disposed in the drain port 113. The interior cavity 112 of the cache tower segment 110 may serve as a sump. The water produced by the reaction of the hydrogen and the metal oxide can flow down from the reaction column section 120 to the sump, and when a certain amount of water has accumulated in the sump, the automatic drain valve 114 can be automatically opened to drain the water.

With reference to fig. 3, fig. 3 shows a connection schematic diagram of a dehydrogenation system according to an embodiment of the present invention, which is a dehydrogenation system, and includes: the hydrogen pipeline 200, the oxygen pipeline 400 and the active hydrogen recombiner 100 are connected, wherein the output end of the hydrogen pipeline 200 and the output end of the oxygen pipeline 400 are both connected with the inlet 1412 of the conveying pipeline, and the active hydrogen recombiner 100 has a first state and a second state.

In a first state, the hydrogen pipeline 200 is communicated with the active hydrogen recombiner 100, and the oxygen pipeline 400 is not communicated with the active hydrogen recombiner 100; specifically, the input end of the hydrogen transmission pipeline 200 is connected to the caustic tower 600, and a pump body is disposed at the input end of the hydrogen transmission pipeline 200, and is configured to pump a mixed gas (containing hydrogen) after caustic washing by the caustic tower 600 into the hydrogen transmission pipeline 200, the output end of the hydrogen transmission pipeline 200 is connected to the delivery pipe inlet 1412 of the active hydrogen recombiner 100, that is, the mixed gas may enter the delivery pipe 141 to be preheated, and the delivery pipe outlet 1413 is connected to the gas inlet 111 of the buffer tower segment 110, that is, the mixed gas may enter the reaction tower segment 120 from the buffer tower segment 110 to perform a reduction reaction.

In the second state, the oxygen pipeline 400 is in communication with the active hydrogen recombiner 100, and the hydrogen pipeline 200 is not in communication with the active hydrogen recombiner 100. Specifically, the input end of the oxygen pipeline 400 is connected to the air compressor 700, the air compressor 700 presses the compressed air into the oxygen pipeline 400, and the output end of the oxygen pipeline 400 is connected to the inlet 1412 of the delivery pipe 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 to perform the oxidation reaction.

The hydrogen pipeline 200 and the oxygen pipeline are respectively provided with a valve 330, when in use for the first time, firstly, metal oxide is filled in the reaction tower section 120, then the valve 330 on the hydrogen pipeline 200 is opened, and the mixed gas from the alkaline tower 600 enters the reaction tower section 120 for dehydrogenation; after the metal oxide in the reaction tower section 120 is reduced to metal, the valve 330 on the hydrogen pipeline 200 is closed, the valve 330 on the oxygen pipeline 400 and the air compressor 700 are opened, the air compressor 700 presses the compressed air into the reaction tower section 120, and the oxygen in the compressed air reacts with the metal to regenerate the metal oxide. Therefore, the dehydrogenation system in the embodiment can realize the regeneration of the metal oxide, and after the metal oxide is consumed, the metal oxide can be directly generated and recycled, so that the dehydrogenation cost can be reduced.

In some embodiments, the upper portion of the heat dissipation tower section 130 is provided with an air outlet 132, and a passive hydrogen recombiner 133 is disposed in the air outlet 132. The hydrogen elimination system further comprises a gas return line 300 and a hydrogen sensor 320, wherein the inlet end of the gas return line 300 is communicated with the upper part of the reaction tower section, and the hydrogen sensor 320 is respectively arranged on the gas return line 300 and the hydrogen conveying line 200.

In this embodiment, because the heat dissipation tower segment 130 is located on the upper portion of the reaction tower segment, the gas outlet 132 may be disposed on the upper portion of the heat dissipation tower segment 130, and then the inlet end of the gas return line 300 is connected to the gas outlet 132 of the heat dissipation tower segment 130, the mixed gas is dehydrogenated in the reaction tower segment 120, and then continues to move upward to the heat dissipation segment, and after being cooled by the heat dissipation tower segment 130, the mixed gas enters the gas return line 300 through the gas outlet 132 disposed on the top of the heat dissipation tower, and then returns to the electrolytic cell 500 through the gas return line 300, so that the mixed gas after being dehydrogenated can be reused.

The passive hydrogen recombiner 133 is disposed in the air outlet 132, and compressed air containing oxygen needs to be introduced into the reaction tower section 120 during the oxidation reaction, so that 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, and when the mixture gas after dehydrogenation returns to the electrolytic cell 500, the passive hydrogen recombiner 133 can eliminate the oxygen therein, thereby ensuring that the mixture gas returned to the electrolytic cell 500 is an oxygen-free safe mixture gas.

The hydrogen transmission pipeline 200 is provided with a hydrogen sensor 320 for detecting and recording the content of hydrogen in the mixed gas before dehydrogenation, the gas return pipeline 300 is provided with a hydrogen sensor 320 for detecting and recording the content of hydrogen in the mixed gas after dehydrogenation, when the active hydrogen recombiner 100 is in a first state, the detection values of the two hydrogen sensors 320 can be compared, if the two hydrogen sensors are close to each other, the metal oxide in the reaction tower is reduced into a metal object, and at the moment, the active hydrogen recombiner 100 can be switched from the first state to a second state.

In some embodiments, the number of 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.

In this embodiment, the number of the dynamic hydrogen recombiners 100 is two, the two dynamic hydrogen recombiners 100 are respectively a first dynamic hydrogen recombiner and a second dynamic hydrogen recombiner, when the metal oxide in the first dynamic hydrogen recombiner is reduced, the hydrogen pipeline 200 connected with the first dynamic hydrogen recombiner and the valve 330 on the gas return pipeline 300 are respectively closed, the valve 330 on the oxygen pipeline connected with the first dynamic hydrogen recombiner is opened, and the hydrogen pipeline 200 connected with the second dynamic hydrogen recombiner and the valve 330 on the gas return pipeline 300 are respectively opened, so that the first dynamic hydrogen recombiner is oxidized, and simultaneously, the second dynamic hydrogen recombiner is dehydrogenated. Similarly, after the metal oxide in the second active hydrogen recombiner is reduced, the second active hydrogen recombiner is oxidized in the above manner, 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 alternately used, and the dehydrogenation process can be continuously carried out.

In another embodiment, when the hydrogen concentration in the mixed gas is high and only two active hydrogen recombiners 100 cannot achieve continuous hydrogen elimination, the number of the active hydrogen recombiners 100 may be two or more, and the two or more active hydrogen recombiners 100 may be used alternately.

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

In some embodiments, the hydrogen elimination system further comprises a steam-water separator, and the gas return line 300 and the hydrogen transportation line 200 are respectively provided with the steam-water separator for eliminating or reducing water vapor in the gas return line 300 and the hydrogen transportation line 200.

The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.

The above-mentioned embodiments only represent several embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.

Claims (13)

1. A dynamic hydrogen recombiner, characterized in that, the dynamic hydrogen recombiner is a reaction tower type structure, the dynamic hydrogen recombiner includes:

the buffer tower section is used for buffering mixed gas, and an air inlet is formed in the outer wall of the buffer tower section;

the reaction tower section is positioned at the upper part of the cache tower section and is communicated with the interior of the cache tower section, and a bearing part is arranged in the reaction tower section; and

and the preheating layer is arranged around the outer wall of the reaction tower section.

2. The active hydrogen recombiner of claim 1 wherein the preheat layer comprises:

the outlet end of the conveying pipeline is connected with the air inlet; and

and the heater is used for heating the reaction tower section and the conveying pipeline simultaneously.

3. The active hydrogen recombiner of claim 2 wherein the delivery conduit comprises:

the straight pipes are arranged at intervals along the circumferential direction of the outer wall of the reaction tower section, and the length direction of the straight pipes is the same as the axial direction of the cache tower section;

the connecting pipes are arc pipes, and the adjacent two straight pipes are connected in sequence through the connecting pipes.

4. The active hydrogen recombiner according to claim 3, wherein the heater is a plurality of heating rods, and one heating rod is disposed between two adjacent straight pipes.

5. The active hydrogen recombiner of claim 1 further comprising:

and the heat insulation layer is arranged on the radial outer side of the preheating layer.

6. The active hydrogen recombiner of claim 1 further comprising:

and the heat dissipation tower section is positioned at the upper part of the reaction tower section and is communicated with the reaction tower section, and the heat dissipation tower section is provided with a radiator.

7. The active hydrogen recombiner of claim 6 wherein the heat sink comprises:

and the plurality of radiating fins are arranged on the outer wall of the radiating tower section at intervals.

8. The active hydrogen recombiner of claim 7, wherein an air outlet is formed at an upper portion of the heat-dissipating tower section, and a passive hydrogen recombiner is disposed in the air outlet.

9. The active hydrogen recombiner of claim 1 wherein the carrier is a screen plate, the screen plate being disposed at the bottom of the reactor section.

10. The active hydrogen recombiner of claim 1, wherein a liquid outlet is opened at the bottom of said buffer tower section, and an automatic drain valve is disposed in said liquid outlet.

11. A dehydrogenation system, comprising: a hydrogen delivery line, an oxygen delivery line, and the active hydrogen recombiner of any of claims 1-10, an output of the hydrogen delivery line, an output of the oxygen delivery line, both connected to the active hydrogen recombiner, the active hydrogen recombiner having a first state and a second state;

in a first state, the hydrogen pipeline is communicated with the active hydrogen recombiner, and the oxygen pipeline is not communicated with the active hydrogen recombiner;

and in a second state, the oxygen conveying pipeline is communicated with the active hydrogen recombiner, and the hydrogen conveying pipeline is not communicated with the active hydrogen recombiner.

12. A dehydrogenation system according to claim 11, wherein the number of the active hydrogen recombiners is at least two, and when one of the active hydrogen recombiners is in the first state, the other active hydrogen recombiner is in the second state.

13. A dehydrogenation system according to claim 11, further comprising:

the gas return line is communicated with the upper part of the reaction tower section;

and the gas return pipeline and the hydrogen conveying pipeline are respectively provided with a hydrogen sensor.

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