CN219971852U - Methanol reforming hydrogen production reactor and reaction equipment - Google Patents

Abstract

The utility model provides a methanol reforming hydrogen production reactor and reaction equipment, and relates to the technical field of fuel cells. The methanol reforming hydrogen production reactor comprises a reaction chamber and a hydrogen separation assembly arranged in the reaction chamber, wherein the reaction chamber is divided into a reaction chamber and a separation chamber by the hydrogen separation assembly, a heating and catalyzing assembly for heating and catalyzing reactants is arranged in the reaction chamber, a reactant air inlet and a tail gas exhaust outlet are formed in the chamber wall of the reaction chamber corresponding to the reaction chamber, and a first hydrogen air outlet is formed in the chamber wall corresponding to the separation chamber. The reaction equipment comprises the reactor. In the methanol reforming hydrogen production reactor, the hydrogen separation component can effectively separate temperature transmission between the reaction cavity and the separation cavity, and the heating load of the heating catalytic component is reduced by reducing ineffective heating of the heating catalytic component on hydrogen in the separation cavity, so that heat consumption is reduced, and the preparation cost of hydrogen is reduced.

Description

Methanol reforming hydrogen production reactor and reaction equipment

Technical Field

The utility model relates to the technical field of fuel cells, in particular to a methanol reforming hydrogen production reactor and reaction equipment.

Background

Research and development of clean energy is vital in the next decades, and fuel cells are receiving increasing attention as one of the important clean energy sources, where hydrogen is an important fuel source for fuel cells as a clean renewable material. At present, methanol is generally used for in-situ reforming to prepare hydrogen, however, a heating component in the existing methanol reforming hydrogen preparation reactor heats the separated hydrogen side while heating the reactant side, and ineffective heating of the hydrogen side can increase the heating load of the heating component, so that heat is wasted, and the preparation cost of hydrogen is increased.

Disclosure of Invention

The utility model aims to provide a methanol reforming hydrogen production reactor and reaction equipment, so as to solve the technical problems that a heating component in the existing methanol reforming hydrogen production reactor is high in heating load, heat is wasted, and hydrogen preparation cost is increased.

In order to solve the problems, the utility model provides a methanol reforming hydrogen production reactor, which comprises a reaction chamber and a hydrogen separation assembly arranged in the reaction chamber, wherein the hydrogen separation assembly divides the reaction chamber into a reaction chamber and a separation chamber, a heating catalytic assembly for heating and catalyzing reactants is arranged in the reaction chamber, a reactant air inlet and a tail gas outlet are arranged on the chamber wall of the reaction chamber corresponding to the reaction chamber, and a first hydrogen air outlet is arranged on the chamber wall corresponding to the separation chamber.

Optionally, the separation chamber is located above the reaction chamber.

Optionally, the hydrogen separation component comprises a ceramic substrate, wherein the ceramic substrate is provided with separation holes, and the walls of the separation holes are covered with a hydrogen separation layer.

Optionally, the heating catalytic assembly comprises a heat exchange tube, and the outer wall of the heat exchange tube is covered with a catalyst layer.

Optionally, the heat exchange tube comprises a tube body and helical fins wound on the tube body.

Optionally, the heat exchange tubes are straight tubes and are distributed in a rectangular array in the reaction cavity; the reactant air inlet is positioned at one side of the extending direction of the heat exchange tube, and the tail gas exhaust outlet is positioned at the other side of the extending direction of the heat exchange tube.

Optionally, the reactant air inlets are multiple groups, the number of the reactant air inlets in each group is multiple and the reactant air inlets are distributed at intervals along the vertical direction, and the multiple groups of reactant air inlets are arranged in one-to-one correspondence with the multiple rows of heat exchange tubes; the reactor also comprises a plurality of air inlet assemblies, each air inlet assembly comprises an air inlet pipe and a plurality of air inlet connectors arranged on one side of the pipe wall of the air inlet pipe, and a plurality of air inlet connectors of the same air inlet assembly are connected with a corresponding group of a plurality of reactant air inlets in a one-to-one correspondence manner.

Optionally, the reactor further comprises an exhaust assembly, wherein the exhaust assembly comprises an exhaust pipe and a plurality of exhaust joints arranged on one side of the pipe wall of the exhaust pipe; the exhaust gas exhaust ports are arranged at intervals along the horizontal direction, and the exhaust connectors are connected with the exhaust gas exhaust ports in one-to-one correspondence.

Optionally, the tail gas exhaust port is located at a middle position in the height direction of the reaction cavity.

The utility model also provides a reaction device for preparing hydrogen by reforming methanol, which comprises:

the reactor is characterized in that a reactant air inlet of the reactor is connected with a gas mixing pipe;

the methanol storage tank is used for containing methanol, and a methanol outlet of the methanol storage tank is communicated with an air inlet end of the gas mixing pipe;

the steam storage tank is used for containing water steam, and a steam outlet of the steam storage tank is communicated with the air inlet end of the air mixing pipe;

the hydrogen storage tank is used for containing hydrogen, and a hydrogen inlet of the hydrogen storage tank is communicated with a first hydrogen outlet of the reactor;

the carbon monoxide storage tank is used for containing carbon monoxide and is provided with a carbon monoxide air inlet; the method comprises the steps of,

the separation device is used for separating hydrogen and carbon monoxide in tail gas, and a tail gas air inlet of the separation device is communicated with the tail gas exhaust port, a second hydrogen air outlet is communicated with the hydrogen air inlet, a carbon monoxide air outlet is communicated with the carbon monoxide air inlet, and a reactant air outlet is communicated with the reactant air inlet.

According to the methanol reforming hydrogen production reactor provided by the utility model, the hydrogen separation component is blocked between the reaction chamber and the separation chamber by adopting the method for separating hydrogen in situ, and the reaction chamber, the hydrogen separation component and the separation chamber form a sandwich laminated structure, so that the hydrogen separation component can effectively block the temperature and pressure transmission between the reaction chamber and the separation chamber, on one hand, the ineffective heating of the hydrogen in the separation chamber by the heating catalytic component can be reduced, on the other hand, the heating load of the heating catalytic component is reduced on the basis of ensuring the reaction temperature in the reaction chamber, the heat consumption is correspondingly reduced, the operation cost of the heating catalytic component and the reactor is reduced, and the preparation cost of the hydrogen is further reduced; on the other hand, the invalid pressure transmission from the reaction cavity to the separation cavity can be reduced, and the pressure difference effect between the reaction cavity and the separation cavity can be ensured on the basis of ensuring the reaction pressure in the reaction cavity, so that the forward progress of the reaction is promoted, and the hydrogen production efficiency of the reaction is correspondingly improved.

Drawings

In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only embodiments of the present utility model, and that other drawings can be obtained according to the provided drawings without inventive effort for a person skilled in the art.

FIG. 1 is a schematic diagram of a methanol reforming hydrogen production reactor provided by the utility model;

FIG. 2 is an exploded view of a methanol reforming hydrogen reactor according to the present utility model;

fig. 3 is a flow chart of the methanol reforming hydrogen production reaction device provided by the utility model.

Reference numerals illustrate:

a 10-methanol storage tank; 20-a steam storage tank; a 30-methanol reforming hydrogen production reactor; 40-a hydrogen storage tank; 50-separating means; 51-an exhaust gas inlet; 52-a second hydrogen outlet; 53-carbon monoxide outlet; 54-reactant outlet; a 60-carbon monoxide storage tank; 61-carbon monoxide gas inlet; 70-a gas mixing pipe; 100-reaction chamber; 110-reaction chamber; 120-separation chamber; 130-reactant inlet; 140-exhaust outlet; 150-a first hydrogen outlet; 200-a hydrogen separation assembly; 210-a ceramic substrate; 220-separation wells; 300-heating the catalytic assembly; 310-heat exchange tubes; 311-pipe body; 312-helical fins; 400-an air intake assembly; 410-an air inlet pipe; 420-an air inlet joint; 500-an exhaust assembly; 510-exhaust pipe; 520-exhaust joint.

Detailed Description

In order that the above objects, features and advantages of the utility model will be readily understood, a more particular description of the utility model will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the utility model.

The embodiment provides a reactor 30 for producing hydrogen by reforming methanol, as shown in fig. 1 and 2, which comprises a reaction chamber 100 and a hydrogen separation assembly 200 arranged in the reaction chamber 100, wherein the hydrogen separation assembly 200 divides the reaction chamber 100 into a reaction chamber 110 and a separation chamber 120, a heating and catalyzing assembly 300 for heating and catalyzing reactants is arranged in the reaction chamber 110, a reactant air inlet 130 and a tail gas outlet 140 are arranged on the chamber wall of the reaction chamber 100 corresponding to the reaction chamber 110, and a first hydrogen air outlet 150 is arranged on the chamber wall corresponding to the separation chamber 120.

The methanol reforming hydrogen production reactor 30 provided in this embodiment includes a reaction chamber 100 for providing a reaction place, and a hydrogen separation assembly 200 for simultaneously separating hydrogen and separating the reaction chamber 100 into a reaction chamber 110 and a separation chamber 120 is disposed in the reaction chamber 100, wherein a heating catalytic assembly 300 for heating and catalyzing reactants is disposed in the reaction chamber 110; when the reactor operates, methanol and water vapor mixed in a certain proportion are used as reactants to be sent into the reaction cavity 110 through the reactant air inlet 130, the heating and catalyzing assembly 300 operates to heat and catalyze the reactants in the reaction cavity 110, so that forward progress of a methanol reforming reaction is promoted, main products of the hydrogen production by reforming the methanol and the water vapor comprise carbon monoxide and hydrogen, wherein the hydrogen can enter the separation cavity 120 through the separation of the hydrogen separation assembly 200, and the methanol, the water vapor, the carbon monoxide and the rest of the hydrogen are isolated in the reaction cavity 110 and are discharged as tail gas through the tail gas exhaust port 140, so that the hydrogen production by reforming the methanol is completed.

The hydrogen separation component 200 is blocked between the reaction chamber 100 and the separation chamber, and the reaction chamber 100, the hydrogen separation component 200 and the separation chamber form a sandwich-type laminated structure, so that the hydrogen separation component 200 can effectively block the temperature and pressure transfer between the reaction chamber 110 and the separation chamber 120, on one hand, the ineffective heating of the hydrogen in the separation chamber 120 by the heating catalytic component 300 can be reduced, on the basis of ensuring the reaction temperature in the reaction chamber 100, the heating load of the heating catalytic component 300 is reduced, the heat consumption is correspondingly reduced, the running cost of the heating catalytic component 300 and the reactor is reduced, and the preparation cost of the hydrogen is further reduced; on the other hand, the ineffective pressure transmission from the reaction cavity 110 to the separation cavity 120 can be reduced, and the pressure difference between the reaction cavity 110 and the separation cavity 120 can be ensured on the basis of ensuring the reaction pressure in the reaction cavity 110, so that the forward progress of the reaction is promoted, and the hydrogen production efficiency of the reaction is correspondingly improved.

Specifically, in the present embodiment, as shown in fig. 1, the separation chamber 120 is located above the reaction chamber 110. The gas in the reaction cavity 110 comprises methanol, water vapor, hydrogen and carbon monoxide, wherein the mass fraction of the hydrogen is the smallest, correspondingly, the hydrogen can move towards the upper hydrogen separation assembly 200 under the action of self gravity and has power of passing through the hydrogen separation assembly 200 upwards, the concentration of the hydrogen at the lower side of the hydrogen separation assembly 200 is higher, and the separation efficiency of the hydrogen separation assembly 200 on the hydrogen can be greatly improved on the basis of reducing the difficulty of separating the hydrogen from the reaction cavity 110 by the hydrogen separation assembly 200, so that the hydrogen production efficiency of the reactor is further improved; in addition, hydrogen in the reaction cavity 110 can enter the separation cavity 120 through the hydrogen separation assembly 200 with high efficiency, so that the hydrogen concentration in the reaction cavity 110 can be kept at a low level, the inhibition of high hydrogen concentration on forward reaction is reduced, the forward progress of the reaction is correspondingly promoted, and the hydrogen production efficiency of the reactor is further improved.

Of course, in other embodiments, the separation chamber 120 and the reaction chamber 110 may be located at other positions, and are not limited to being located above the reaction chamber 110.

In this embodiment, as shown in fig. 1 and 2, the hydrogen separation assembly 200 includes a ceramic substrate 210, the ceramic substrate 210 is provided with separation holes 220, and the walls of the separation holes 220 are covered with a hydrogen separation layer. Here, in one specific form of the hydrogen separation assembly 200, the ceramic substrate 210 is used as a matrix to divide the reaction chamber 100 into a reaction cavity 110 and a separation cavity 120, separation holes 220 which can allow the gas in the reaction cavity 110 to flow into the separation cavity 120 are formed in the ceramic substrate 210, and the holes of the separation holes 220 are covered with a hydrogen separation layer which can selectively separate the flowing gas; when the reactor operates, the reaction cavity 110 is in a high-pressure and high-temperature state, methanol, water vapor, hydrogen and carbon monoxide in the reaction cavity flow to the separation hole 220 under the action of pressure difference, the hydrogen separation layer on the wall of the separation hole 220 can select hydrogen in gas, only hydrogen is allowed to enter the separation cavity 120 through the separation hole 220, and other gases are blocked in the reaction cavity 110, so that the selective separation of the hydrogen in the reaction cavity 110 is realized, the hydrogen separation assembly 200 has a simple structure, a good separation effect and low cost, and the disassembly and assembly convenience with the reaction cavity 100 is high, and the structural simplicity, the disassembly and assembly convenience and the cost of the reactor are correspondingly improved. Specifically, the hydrogen separation layer may employ at least one of a metal organic framework layer, a zeolite imidazole ester framework layer, and the like, which have a high selectivity for hydrogen.

Alternatively, in the present embodiment, the heating catalyst assembly 300 includes the heat exchange tube 310, and the outer wall of the heat exchange tube 310 is covered with the catalyst layer. In one specific form of the heating catalytic assembly 300, when the reactor is in operation, a hot working medium is introduced into the heat exchange tube 310, the hot working medium transfers heat to the heat exchange tube 310 through heat convection, and the area where the catalyst layer on the outer wall of the heat exchange tube 310 is located is used as an effective reaction area of reactants in the reaction cavity 110, so that the hot working medium can be used for efficiently heating the effective reaction area in the reaction cavity 110, thereby ensuring the reaction temperature of the effective reaction area, correspondingly ensuring the normal reaction in the reaction cavity 110, and effectively reducing the ineffective dissipation of the heat of the hot working medium; the heating catalyst assembly 300 in this embodiment adopts the heat exchange tube 310 and covers the outer wall of the heat exchange tube 310 with a catalyst layer, which not only can ensure the hydrogen production reaction of methanol reforming with high efficiency and low heat loss, but also can reduce the heat loss of the heating catalyst assembly 300, thereby reducing the heating load of the heating catalyst assembly 300 and correspondingly reducing the energy loss and the running cost of the reactor. Specifically, the catalyst layer may be attached to the outer wall of the heat exchange tube 310 by spraying or in-situ growth, etc.

Specifically, in the present embodiment, as shown in fig. 1 and 2, the heat exchange tube 310 includes a tube body 311 and helical fins 312 wound around the tube body 311. When the coverage area of the catalyst layer is fixed, the arrangement of the spiral fins 312 can effectively increase the specific surface area of the heat exchange tube 310, so that the volume of the heating catalytic assembly 300 is reduced, the volume limitation on the reaction cavity 110 is correspondingly reduced, the applicable size of the heating catalytic assembly 300 can be increased, the overall size of the reaction chamber 100 can be reduced on the basis of ensuring the hydrogen production efficiency, the compactness of the reactor is improved, and the space occupation of the reactor is reduced; in addition, the spiral fins 312 have no sharp angles, and can perform a flow guiding function on the reactant, so that the smoothness of the flow of the reactant in the reaction cavity 110 is ensured, and the occurrence of vortex formation and larger flow resistance of the reactant in the reaction cavity 110 is reduced. Of course, in some embodiments, plate-like fins may be provided outside the tube body 311, and are not limited to the helical fins 312.

In this embodiment, as shown in fig. 1, the heat exchange tubes 310 are straight tubes and have a plurality of heat exchange tubes 310 arranged in a rectangular array in the reaction chamber 110; the reactant inlet 130 is located at one side of the extension direction of the heat exchange tube 310, and the exhaust outlet 140 is located at the other side of the extension direction of the heat exchange tube 310. Firstly, the straight tubular heat exchange tubes 310 are arranged in the reaction cavity 110 in a rectangular array, so that the effective reaction areas represented by the catalyst layers are fully and uniformly distributed in all spaces of the reaction cavity 110, the effective utilization of the internal space of the reaction cavity 110 is correspondingly improved, the forward reaction sufficiency in the reaction cavity 110 is further ensured, and the hydrogen production efficiency of the reactor is improved; secondly, the reactant inlet 130 and the tail gas outlet 140 are located at two ends of the extending direction of the heat exchange tube 310, so that the flowing direction of the reactant entering the reaction cavity 110 from the reactant inlet 130 is consistent with the extending direction of the heat exchange tube 310, the reactant can stably flow along the spiral path along the heat exchange tube 310 and is discharged along the spiral path to the tail gas outlet 140 under the guiding action of the spiral fin 312, and the reactant can fully contact with the spiral fin 312 and the outer wall surface of the tube body 311, so that the reaction sufficiency is improved, the flowing stability of the reactant in the reaction cavity 110 is also improved, the generation of vortex is reduced, and the hydrogen production efficiency of the reactor is further improved.

Specifically, in the present embodiment, the gap distance between two adjacent heat exchange tubes 310 may be 10-40mm along the horizontal direction, and the minimum distance between the heat exchange tubes 310 and the hydrogen separation assembly 200 may be 10-20mm.

Specifically, in this embodiment, as shown in fig. 1, the reactant inlets 130 are multiple groups, and the number of reactant inlets 130 in each group is multiple and the reactant inlets 130 are arranged at intervals along the vertical direction, and the multiple groups of reactant inlets 130 are arranged in one-to-one correspondence with the multiple rows of heat exchange tubes 310; the reactor further comprises a plurality of air inlet assemblies 400, wherein each air inlet assembly 400 comprises an air inlet pipe 410 and a plurality of air inlet connectors 420 arranged on one side of the pipe wall of the air inlet pipe 410, and the plurality of air inlet connectors 420 of the same air inlet assembly 400 are connected with a corresponding group of a plurality of reactant air inlets 130 in a one-to-one correspondence manner. Among the plurality of heat exchange tubes 310 arranged in a rectangular array, the heat exchange tubes 310 are arranged in rows along the horizontal direction and in columns along the vertical direction, the heat exchange tubes 310 are arranged in a plurality of columns, a plurality of groups of reactant air inlets 130 positioned at one end of the heat exchange tubes 310 are arranged in one-to-one correspondence with the plurality of columns of heat exchange tubes 310, and a plurality of reaction area air inlets of each group are arranged in a column; when the reactor is operated, the reactants are introduced into the gas inlet pipe 410 of each gas inlet assembly 400, the reactants in the gas inlet pipe 410 can flow into the reaction cavity 110 through the gas inlet joints 420 and the plurality of reactant gas inlets 130 of the same group at the same time, and the flowing reactants can flow to the heat exchange tube 310 along the extending direction of the heat exchange tube 310 at different positions in the height direction, so that the reactants are fully distributed in different areas at one end of the heat exchange tube 310 to be fully and uniformly contacted with the catalyst layer on the surface of the heat exchange tube 310, and one end of each heat exchange tube 310 is provided with one group of reactant gas inlets 130, thereby ensuring the full utilization of all the heat exchange tubes 310, correspondingly further improving the positive reaction sufficiency of the reactants and further improving the hydrogen production efficiency of the reactor.

As shown in fig. 1 and 2, the number of the heat exchange tubes 310 is three, and the three heat exchange tubes 310 are uniformly distributed at intervals along the horizontal direction, so that the three heat exchange tubes 310 are distributed in a single row and a three-column manner; the number of the air inlet assemblies 400 is three, each air inlet assembly 400 comprises an air inlet pipe 410 extending vertically, eight air inlet connectors 420 are arranged on one side, facing the reaction cavity 110, of each air inlet pipe 410, and the eight air inlet connectors 420 are arranged at intervals along the axial direction of the air inlet pipe 410; the side walls of the reaction chamber 110 are provided with three rows of reactant inlets 130, the three rows of reactant inlets 130 are in one-to-one correspondence with the three rows of heat exchange tubes 310, and eight reactant inlets 130 in each row are in one group and are in one-to-one correspondence connection with eight air inlet connectors 420 of a corresponding air inlet assembly 400.

Specifically, the air intake assembly 400 may further include a main pipe, and one ends of the plurality of air intake pipes 410 are all connected to the main pipe, so that when in use, reactant can be supplemented to the plurality of air intake pipes 410 simultaneously only by connecting the main pipe with an external air supply assembly; of course, the plurality of intake pipes 410 may be connected to the air supply unit. Similarly, the heating catalytic assembly 300 may also include a main heating pipe, one ends of the pipe bodies 311 of the plurality of heat exchange pipes 310 are all communicated with the main heating pipe, and when in use, the heat working medium can be conveyed to the plurality of heat exchange pipes 310 simultaneously only by connecting the main heating pipe with an external heating assembly; of course, as shown in fig. 2, the plurality of heat exchange tubes 310 may be disposed independently, and the plurality of heat exchange tubes 310 may be connected to an external heat supply unit when in use.

In this embodiment, as shown in fig. 1 and 2, the reactor further includes an exhaust assembly 500, and the exhaust assembly 500 includes an exhaust pipe 510 and a plurality of exhaust joints 520 provided at one side of a pipe wall of the exhaust pipe 510; the exhaust ports 140 are multiple, and the exhaust ports 140 are arranged at intervals along the horizontal direction, and the exhaust connectors 520 are connected with the exhaust ports 140 in a one-to-one correspondence. The reactant entering the reaction cavity 110 flows to one side of the tail gas exhaust port 140 along the heat exchange tube 310, so that the tail gas in different areas in the horizontal direction of the reaction cavity 110 can be exhausted into the corresponding exhaust joint 520 through the tail gas exhaust port 140 in the corresponding area and enter and are exhausted into the exhaust pipe 510, thereby ensuring that the tail gas in different areas in the reaction cavity 110 can be smoothly exhausted in a short path, and correspondingly reducing the situation that the tail gas stays in a local area at the tail end of the reaction cavity 110 and cannot be exhausted to occupy the effective reaction space in the reaction cavity 110, so that the hydrogen production efficiency of the reactor is reduced; in addition, the plurality of exhaust joints 520 can be exhausted through the single exhaust pipe 510, and the exhaust pipe 510 has a small number, a simple structure, and low cost.

Preferably, in this embodiment, as shown in fig. 1, the exhaust port 140 is located at a middle position in the height direction of the reaction chamber 110. The single exhaust gas outlet 140 is located at the middle position of the reaction cavity 110 in the height direction, and the distances between each position of the tail end of the reaction cavity 110 and the exhaust gas outlet 140 in the corresponding region are smaller in the height direction, accordingly, the exhaust gas can be converged towards the middle and flow out through the corresponding exhaust gas outlet 140, thereby further ensuring smooth exhaust of the exhaust gas.

The embodiment also provides a reaction device for producing hydrogen by reforming methanol, as shown in fig. 3, which comprises the reactor, a methanol storage tank 10, a steam storage tank 20, a hydrogen storage tank 40, a carbon monoxide storage tank 60 and a separation device 50, wherein a reactant air inlet 130 of the reactor is connected with a gas mixing pipe 70; the methanol storage tank 10 is used for containing methanol, and a methanol outlet of the methanol storage tank 10 is communicated with an air inlet end of the gas mixing pipe 70; the steam storage tank 20 is used for containing steam, and a steam outlet of the steam storage tank 20 is communicated with an air inlet end of the air mixing pipe 70; the hydrogen storage tank 40 is used for containing hydrogen, and a hydrogen inlet of the hydrogen storage tank 40 is communicated with a first hydrogen outlet 150 of the reactor; the carbon monoxide storage tank 60 is used for containing carbon monoxide and is provided with a carbon monoxide air inlet 61; the separation device 50 is used for separating hydrogen and carbon monoxide in the tail gas, and the tail gas inlet 51 of the separation device 50 is communicated with the tail gas outlet 140, the second hydrogen gas outlet 52 is communicated with the hydrogen gas inlet, the carbon monoxide gas outlet 53 is communicated with the carbon monoxide gas inlet 61, and the reactant gas outlet 54 is communicated with the reactant gas inlet 130. Wherein, an air pump can be installed on the communication pipeline between the first hydrogen outlet 150 and the hydrogen inlet, and the air pump pumps the separation cavity 120, so that the hydrogen in the separation cavity 120 can quickly enter the hydrogen storage tank 40, thereby improving the storage efficiency of the hydrogen, and increasing the pressure difference between the separation cavity 120 and the reaction cavity 110, so as to promote the separation of the hydrogen in the reaction cavity 110 by the hydrogen separation assembly 200, correspondingly improving the separation efficiency of the hydrogen and promoting the normal phase reaction in the reaction cavity 110.

At first, methanol is stored in the methanol storage tank 10, water vapor is stored in the steam storage tank 20, when the reactor runs, the heating catalytic assembly 300 in the reactor runs, the methanol storage tank 10 and the steam storage tank 20 respectively convey methanol and water vapor to the gas mixing pipe 70 through the methanol gas outlet and the steam gas outlet at preset flow rates, methanol and water vapor with certain flow rates are mixed in the gas mixing pipe 70 and then enter the reaction cavity 110 through the reactant gas inlet 130 as reactants, and the reactants produce carbon monoxide and hydrogen under the heating and catalytic effects of the heating catalytic assembly 300, wherein part of hydrogen can enter the separation cavity through the separation of the hydrogen separation assembly 200 and then enter the hydrogen storage tank 40 through the first hydrogen gas outlet 150 and the hydrogen gas inlet; the reaction zone, carbon monoxide and residual hydrogen flowing into the tail end in the reaction cavity 110 flow out through the tail gas exhaust port 140, then enter the separation device 50 through the tail gas inlet 51, the separation device 50 carries out secondary separation on the hydrogen and the carbon monoxide in the tail gas, the separated hydrogen flows out through the second hydrogen outlet 52 and flows into the hydrogen storage tank 40 through the hydrogen inlet, and thus the hydrogen produced by the methanol reforming reaction is completely separated and stored in the hydrogen storage tank 40; the carbon monoxide separated by the separation device 50 flows out through the carbon monoxide outlet 53 thereof and flows into the carbon monoxide storage tank 60 through the carbon monoxide inlet 61, so that the carbon monoxide produced by the reforming reaction of the methanol is separated and stored in the carbon monoxide storage tank 60; the remaining methanol and water vapor in the separation device 50 are discharged through the reactant outlet 54, and then flow back into the reaction cavity 110 again through the reactant inlet 130, so that the recycling of the reactant is realized, the consumption of the reactant is reduced, and the hydrogen production efficiency of the reactor is further improved.

The reaction apparatus for reforming hydrogen with methanol can provide reactants required for the reaction through the methanol storage tank 10 and the steam storage tank 20, perform the methanol reforming reaction through the reactor and perform the primary separation of hydrogen in the product, perform the secondary separation of hydrogen in the tail gas of the reactor and the separation of carbon monoxide through the separation device 50, thereby completely separating hydrogen and storing the separated hydrogen into the hydrogen storage tank 40, and simultaneously storing the separated carbon monoxide into the carbon monoxide storage tank 60, and methanol and steam in the tail gas can be refluxed to the reactor for recycling, thereby fully utilizing the reactants, reducing the consumption of the reactants, and obtaining all hydrogen and carbon monoxide in the product. Meanwhile, the reaction equipment adopts the reactor, and has all the beneficial effects of the reactor, and the description is omitted here.

Finally, it is further noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element.

The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims (10)

1. The utility model provides a methanol reforming hydrogen manufacturing reactor, its characterized in that includes reaction chamber (100) and locates hydrogen separation subassembly (200) in reaction chamber (100), hydrogen separation subassembly (200) will divide into reaction chamber (110) and separation cavity (120) in reaction chamber (100), be equipped with in reaction chamber (110) and be used for playing heating and catalytic action's heating catalytic module (300) to the reactant, just reaction chamber (100) with the corresponding chamber wall of reaction chamber (110) is equipped with reactant air inlet (130) and tail gas vent (140), with the corresponding chamber wall of separation cavity (120) is equipped with first hydrogen gas outlet (150).

2. A methanol reforming hydrogen production reactor as defined in claim 1, wherein the separation chamber (120) is located above the reaction chamber (110).

3. The methanol reforming hydrogen production reactor (30) as defined in claim 1, wherein the hydrogen separation assembly (200) comprises a ceramic substrate (210), the ceramic substrate (210) being provided with separation holes (220), and the walls of the separation holes (220) being covered with a hydrogen separation layer.

4. A methanol reforming hydrogen production reactor as in any one of claims 1-3, characterized in that the heating catalyst assembly (300) comprises a heat exchange tube (310) and the outer wall of the heat exchange tube (310) is covered with a catalyst layer.

5. A reactor for reforming hydrogen production from methanol as defined in claim 4, wherein the heat exchange tube (310) comprises a tube body (311) and helical fins (312) wound around the tube body (311).

6. The reactor for producing hydrogen by reforming methanol according to claim 4, wherein the heat exchange tubes (310) are straight and have a plurality of heat exchange tubes, and the plurality of heat exchange tubes (310) are arranged in the reaction chamber (110) in a rectangular array; the reactant inlet (130) is positioned at one side of the extending direction of the heat exchange tube (310), and the tail gas outlet (140) is positioned at the other side of the extending direction of the heat exchange tube (310).

7. The reactor for reforming and producing hydrogen from methanol according to claim 6, wherein the reactant inlets (130) are provided in a plurality of groups, the reactant inlets (130) in each group are provided in a plurality of groups and are arranged at intervals in a vertical direction, and the plurality of groups of reactant inlets (130) are provided in one-to-one correspondence with the plurality of rows of heat exchange tubes (310); the reactor further comprises a plurality of air inlet assemblies (400), each air inlet assembly (400) comprises an air inlet pipe (410) and a plurality of air inlet connectors (420) arranged on one side of the pipe wall of the air inlet pipe (410), and the plurality of air inlet connectors (420) of the same air inlet assembly (400) are connected with a corresponding group of a plurality of reactant air inlets (130) in a one-to-one correspondence mode.

8. A methanol reforming hydrogen production reactor as in any one of claims 1-3, further comprising an exhaust assembly (500), the exhaust assembly (500) comprising an exhaust pipe (510) and a plurality of exhaust connectors (520) provided on a side of a pipe wall of the exhaust pipe (510); the exhaust gas exhaust ports (140) are multiple, the exhaust gas exhaust ports (140) are distributed at intervals along the horizontal direction, and the exhaust connectors (520) are connected with the exhaust gas exhaust ports (140) in a one-to-one correspondence mode.

9. The reactor for producing hydrogen by reforming methanol according to claim 8, wherein the off-gas outlet (140) is located at a central position in a height direction of the reaction chamber (110).

10. A methanol reforming hydrogen production reaction apparatus, characterized by comprising:

the reactor of any of claims 1-9, wherein a gas mixing tube (70) is connected to a reactant inlet (130) of the reactor;

the methanol storage tank (10) is used for containing methanol, and a methanol outlet of the methanol storage tank (10) is communicated with an air inlet end of the gas mixing pipe (70);

the steam storage tank (20) is used for containing water steam, and a steam outlet of the steam storage tank (20) is communicated with an air inlet end of the air mixing pipe (70);

a hydrogen storage tank (40) for containing hydrogen, wherein a hydrogen inlet of the hydrogen storage tank (40) is communicated with a first hydrogen outlet (150) of the reactor;

a carbon monoxide storage tank (60) for containing carbon monoxide and provided with a carbon monoxide inlet (61); the method comprises the steps of,

the separation device (50) is used for separating hydrogen and carbon monoxide in tail gas, a tail gas inlet (51) of the separation device (50) is communicated with the tail gas outlet (140), a second hydrogen gas outlet (52) is communicated with the hydrogen gas inlet, a carbon monoxide outlet (53) is communicated with the carbon monoxide inlet (61), and a reactant outlet (54) is communicated with the reactant inlet (130).